WO2021049359A1 - 有機溶媒可溶性リグニンの回収システム及び回収方法 - Google Patents
有機溶媒可溶性リグニンの回収システム及び回収方法 Download PDFInfo
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- WO2021049359A1 WO2021049359A1 PCT/JP2020/032892 JP2020032892W WO2021049359A1 WO 2021049359 A1 WO2021049359 A1 WO 2021049359A1 JP 2020032892 W JP2020032892 W JP 2020032892W WO 2021049359 A1 WO2021049359 A1 WO 2021049359A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
- C08L97/00—Compositions of lignin-containing materials
- C08L97/005—Lignin
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
- C08H6/00—Macromolecular compounds derived from lignin, e.g. tannins, humic acids
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/02—Monosaccharides
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/14—Preparation of compounds containing saccharide radicals produced by the action of a carbohydrase (EC 3.2.x), e.g. by alpha-amylase, e.g. by cellulase, hemicellulase
Definitions
- the present invention relates to a recovery system and a recovery method for organic solvent-soluble lignin.
- the present application claims priority based on Japanese Patent Application No. 2019-164255 filed in Japan on September 10, 2019, the contents of which are incorporated herein by reference.
- Non-edible biomass includes cellulose, which is the most abundant on the earth, but most of it exists as lignocellulose, which is a complex with aromatic polymers lignin and hemicellulose.
- ethanol production using lignocellulose-based biomass as a raw material it was obtained in a pretreatment step of thermochemically pretreating the biomass raw material, a saccharification step of enzymatically treating the biomass after the pretreatment step to produce a saccharified solution, and a saccharification step. It comprises a fermentation step of adding a microbial culture solution to a saccharified solution to perform ethanol fermentation, and a purification step of separating ethanol from the fermented solution obtained in the fermentation step by distillation or the like.
- lignin remains as a solid, there is a problem that a large amount of fermentation residue is generated. This fermentation residue is generally processed by a boiler in an annexed factory, methane fermentation, etc., and is not effectively used at present.
- lignin-based products black liquor, lignin sulfonate
- technology for effective utilization has been developed for many years.
- lignin is affected by sulfonation or chloride, so that it is difficult to use, and most of them are limited to fuel use as a boiler heat source.
- Patent Document 1 discloses a method for producing a lignin decomposition product by treating a lignin-containing biomass with a mixed solvent having a molar ratio of water to alcohol of 1/1 to 20/1.
- Patent Document 2 discloses a method for producing low molecular weight lignin by heating lignin-containing biomass in the presence of an acid catalyst in a mixed solvent of hydrocarbon and alcohol.
- Patent Document 3 lignin-containing biomass is pretreated by combining hydrothermal treatment and pulverization treatment, and the enzymatic saccharification residue generated when the pretreated biomass is enzymatically saccharified is further hydrothermally treated by autoclave, and the treated product thereof.
- a method for producing a lignin decomposition product by dissolving the solid substance in an organic solvent after obtaining the solid substance from the solid-liquid separation of the above.
- a lignin-containing biomass is saccharified with an enzyme to obtain a saccharified residue, and the saccharified residue is heated in a mixed solvent containing water and an organic solvent having a solubility in water at 20 ° C. of 90 g / L or more.
- a method for producing a lignin decomposition product by treating to obtain a heat treatment liquid containing a lignin decomposition product and then solid-liquid separation of the heat treatment liquid to remove insoluble matter is disclosed.
- the lignin obtained by using the methods described in Patent Documents 1 to 4 and the like is in the state of a solution dissolved or dispersed in a solvent.
- a stirring tank or the like provided with a heating jacket and volatilizing the solvent over time by heating and concentrating.
- lignin precipitates as a tar-like adherent, and it is difficult to stably obtain solid lignin.
- the present invention has been made in view of the above circumstances, and provides a recovery system and a recovery method for organic solvent-soluble lignin, which can stably obtain solid lignin.
- a recovery system for organic solvent-soluble lignin An extract containing an organic solvent-soluble lignin extracted from a solid containing lignin with a mixed solvent of an organic solvent and water is dried to form a thin-film dry product containing a solid organic solvent-soluble lignin.
- a recovery system equipped with a thin film dryer (2) The recovery system according to (1), wherein the thin film dryer has a scraping mechanism configured to scrape the dried product.
- the recovery system according to (3) further comprising a volatile tank upstream of the thin film dryer and downstream of the extraction device.
- a separation device configured to separate water and an organic solvent from the volatile components discharged from the thin film dryer and the volatile tank is further provided downstream of the thin film dryer (4).
- the collection system described in. (6) The recovery system according to (5), wherein the separation device is a distillation device. (7) Further provided with a pipe configured to send the distillate obtained by the distillation apparatus to the extraction apparatus.
- the recovery system according to (6), wherein the distillation apparatus has a control unit that controls a reboiler heating amount and a recirculation amount so that the content ratio of water and an organic solvent in the distillation solution is within a predetermined range.
- a method for recovering organic solvent-soluble lignin Including a drying step of drying an extract containing an organic solvent-soluble lignin extracted from a solid containing lignin with a mixed solvent of an organic solvent and water to form a thin-film dried product containing a solid organic solvent-soluble lignin. , Recovery method. (9) The recovery method according to (8), further comprising a collection step of collecting the dried product after the drying step. (10) The recovery method according to (8) or (9), further comprising an extraction step of mixing the solid substance with the mixed solvent and separating the extract before the drying step.
- a reuse step of reusing the distillation solution obtained in the distillation step in the extraction step is further included.
- the supply amount of the distillate and the supply amount of water are controlled so as to be the content ratio of water and the organic solvent in the mixed solvent used in the extraction step (15). ) Described in the collection method.
- organic solvent-soluble lignin recovery system and recovery method According to the organic solvent-soluble lignin recovery system and recovery method according to the above aspect, it is possible to provide a recovery system and recovery method for organic solvent-soluble lignin that can stably obtain solid lignin.
- FIG. 1 It is a schematic block diagram which shows the recovery system of organic solvent-soluble lignin which concerns on 4th Embodiment of this invention. It is a vertical sectional view of the disc dryer in Example 1. FIG. It is a side view of the disc dryer in Example 1. FIG. It is a graph which shows the time-dependent change of the volatilization rate of the organic solvent (acetone or ethanol) in the extract in Example 2.
- the organic solvent-soluble lignin recovery system according to the embodiment of the present invention (hereinafter, may be abbreviated as “recovery system of the present embodiment”) and the method for recovering the organic solvent-soluble lignin (hereinafter, “the recovery system of the present embodiment”). (Sometimes abbreviated as “collection method”) will be described in detail. In the present specification and claims, the meanings of various terms are defined as follows.
- Examples of the solid substance containing lignin used as a raw material in the recovery system and recovery method of the present embodiment include lignocellulosic biomass.
- the lignocellulosic biomass is, for example, at least one selected from the group consisting of woody plants (also called woody biomass), herbaceous plants (also called herbaceous biomass), their processed products, and their wastes. If there is, the type does not matter. Further, the lignocellulosic biomass may be crushed, and may have any shape such as a block, a chip, or a powder.
- the solid containing lignin a residue generated in the process of producing bioethanol, biobutanol, a biochemical product or the like from cellulose and hemicellulose in lignocellulose-based biomass may be used.
- the residue it is preferable that the lignocellulosic biomass is a saccharification residue that remains after being pretreated by a dilute sulfuric acid cooking method and further decomposing the obtained pretreatment raw material by an enzymatic saccharification method.
- woody plant examples include sugi, cypress, karamatsu, pine, rice pine, rice sugi, hemlock, poplar, white birch, willow, eucalyptus, oak, oak, oak, castanopsis, beech, acacia, bamboo, and sasa.
- woody plant examples include Japanese cypress and Japanese oak. Among them, Sugi is preferable as a woody plant from the viewpoint of stability of properties.
- the bark, branches, fruit bunches, fruit husks, etc. of the above-mentioned woody plants can also be used.
- processed materials such as plywood, fiberboard, and laminated wood using the above-mentioned woody plants can also be used.
- members that have been dismantled after being used in buildings can also be used.
- processed products of lignocellulosic biomass such as paper and used paper can also be used.
- herbaceous plants examples include bamboo, palm palm; rice (including rice straw), wheat (including straw), sugar cane (including bagasse), Yoshi, Japanese pampas grass, corn (including corn stover, corn cob, and corn hull).
- Gramineae plants such as sorghum (including sweet sorghum), switchgrass, erianthus, napiergrass; yatrofa, cashew and the like.
- a herbaceous plant (herbaceous biomass) is preferable, and a gramineous plant is more preferable.
- lignin is a natural polymer that is one of the three major principal components of herbaceous biomass.
- bagasse contains 5% by mass or more and 30% by mass or less of lignin.
- the basic skeleton of lignin is composed of aromatic nuclei (benzene nuclei), and lignin is classified into G nuclei, S nuclei and H nuclei based on its structure.
- the G nucleus has one methoxy group (-OCH 3 ) at the ortho position of the phenol skeleton portion
- the S nucleus has two methoxy groups at the ortho position
- the H nucleus is It does not have a methoxy group at the ortho position.
- lignin in herbaceous biomass such as bagasse contains all of H nucleus, G nucleus and S nucleus as a basic skeleton.
- the lignin derived from coniferous trees has a G nucleus as a basic skeleton
- the lignin derived from broad-leaved trees has a G nucleus and an S nucleus as a basic skeleton.
- the "organic solvent-soluble lignin” is a lignin that is soluble in an organic solvent, and specifically, in an extraction step described later, from a solid substance containing lignin (lignocellulose-based biomass, etc.). The lignin contained in the extract extracted by the mixed solvent of an organic solvent and water is shown.
- cellulose includes hexoses having six carbons as constituent units. Therefore, when cellulose is hydrolyzed, it produces a hexose monosaccharide consisting of 6 carbon atoms (glucose or the like) or a hexose oligosaccharide (cellobiose or the like) in which a plurality of the monosaccharides are linked.
- Hemicellulose includes pentose (C5 sugar) having five carbons such as xylose and six carbons such as mannose, arabinose, and 4-O-methylglucuronic acid as constituent units (hexose). It contains complex polysaccharides such as glucomannan and glucuronoxylan, which are composed of C6 sugar). Therefore, when hemicellulose is hydrolyzed, it is a monosaccharide of pentasaccharide consisting of 5 carbons, an oligosaccharide of pentasaccharide in which a plurality of monosaccharides are linked, a monosaccharide of hexasaccharide consisting of 6 carbons, and the like.
- a plurality of monosaccharides linked to each other produce an oligosaccharide of hexacarbonate, and an oligosaccharide in which a plurality of monosaccharides of pentasaccharide and a plurality of monosaccharides of hexasaccharide are linked.
- composition ratio and the amount of monosaccharide or oligosaccharide produced from hemicellulose or cellulose differ depending on the pretreatment method and the type of lignocellulosic biomass used as a raw material.
- the recovery system of the present embodiment was configured to dry an extract containing an organic solvent-soluble lignin extracted from a solid containing lignin with a mixed solvent of an organic solvent and water to form a thin film-like dried product. Equipped with a thin film dryer.
- FIG. 1A schematically shows a change in the solution when a solution containing water, an organic solvent and an organic solvent-soluble lignin is dried by a conventional heat concentration method.
- water 1 the organic solvent 2 and the organic solvent-soluble lignin 3 are uniformly dispersed.
- the organic solvent 2 is volatilized and removed in advance while the mixed solvent is gradually volatilized and removed over time.
- FIG. 1B schematically shows a change in the solution when a solution containing water, an organic solvent and an organic solvent-soluble lignin is dried by a thin film dryer.
- water 1 and the organic solvent 2 are volatilized from the solution before the above-mentioned aggregation and precipitation of lignin develops and dried, and a thin film-like dried product containing the organic solvent-soluble lignin 3 is efficient.
- the recovery system of the present embodiment can stably recover solid organic solvent-soluble lignin that does not contain water and does not recondense.
- FIG. 2 is a schematic configuration diagram showing a recovery system for organic solvent-soluble lignin according to the first embodiment of the present invention.
- the recovery system of the present embodiment will be described in detail below with reference to FIG.
- the recovery system 100 shown in FIG. 2 includes a thin film dryer 10.
- the thin film dryer 10 volatilizes the volatile component 6 (mainly the mixed solvent) from the extract 4 and contains the solid content (mainly the solid organic solvent-soluble lignin 3a) contained in the extract 4. ) Is formed to form a thin film-like dried product.
- the thin film dryer 10 include those having a member including a heat transfer surface.
- the member including the heat transfer surface is configured so that the heat transfer surface is heated by steam or the like. Further, the member including the heat transfer surface is formed into a thin film by applying the extract thinly on the heat transfer surface and volatilizing the volatile components from the extract before the above-mentioned aggregation and precipitation of lignin appears. A dried product can be formed.
- the thin-film dried product means a dried product having a thickness of 300 ⁇ m or less.
- the shape of the heat transfer surface is not particularly limited, and may be a flat surface or a three-dimensional surface. In the case of a flat surface, for example, a substantially circular shape (including a perfect circle), a hollow substantially circular shape (including a hollow perfect circle), a fan shape, an annular fan shape, a polygonal shape and the like can be mentioned.
- a circular shape (including a perfect circular shape), a hollow substantially circular shape (including a hollow perfect circular shape), a fan shape, or an annular fan shape is preferable.
- the material of the heat transfer surface may be any material that easily conducts heat, but is preferably a material having excellent wear resistance that can withstand the scraping operation by the scraping mechanism described later, for example, hard chrome plating or electroless. Examples thereof include steel materials that have been subjected to electrolytic nickel plating or the like.
- the thin film dryer 10 preferably has a scraping mechanism.
- the scraping mechanism is configured to scrape the dried product. Since the thin film dryer has a scraping mechanism, it is possible to scrape and recover the thin film-like dried material formed on the heat transfer surface such as the disk surface or the drum surface. Further, by the scraping operation, the thin film-like dried product is crushed, and the powdery organic solvent-soluble lignin can be recovered. Specific examples of the scraping mechanism include a scraper and the like.
- the scraper may be blade-shaped (also referred to as knife-shaped or blade-shaped) or spatula-shaped.
- the scraping mechanism means a mechanism for peeling the dried product from the surface by rubbing it on the surface on which the dried product is located.
- the thin film dryer further has a rotating shaft member in addition to the scraping mechanism.
- the rotating shaft member is configured so that the member including the heat transfer surface is heated by a method of supplying steam or the like into the shaft, and the member including the heat transfer surface rotates around the center of the heat transfer surface. There is. Since the thin film dryer has a scraping mechanism and a rotating shaft member, the extract can be efficiently dried and the dried product can be recovered continuously while the member including the heat transfer surface is rotated once. Organic solvent-soluble lignin can be recovered.
- the thin film dryer is configured to collect the feed pipe configured to add the extract on the heat transfer surface and the extract that did not adhere to the heat transfer surface, circulate it, and supply it to the feed pipe.
- Other known configurations may be provided, such as a circulation mechanism (for example, a mechanism including a circulation tank and a pipe), a collection port configured to take out the dried product to the outside of the dryer, and the like.
- Examples of the shape of the feed pipe include an opening type such as a faucet and a hose outlet, a shower type, and a spray type.
- the thin film dryer may be configured to be directly immersed in a liquid storage tank (or a liquid pool portion) containing an extract while rotating a part of the heat transfer surface instead of the feed pipe.
- the thin film dryer include a conduction heat transfer dryer such as a disc dryer (disc dryer) (see FIGS. 6A and 6B) and a drum dryer (drum dryer).
- the disc dryer is configured to spray an extract on a steam-heated disc surface (one or both sides) to volatilize and dry the volatile components during one revolution of the disc.
- the drum dryer is configured so that the extract is attached to the surface of the drum heated by steam (the outer wall surface of the drum), and the liquid component is volatilized and dried during one rotation of the drum.
- Disc dryers and drum dryers are usually equipped with a scraper for collecting thin film dried products.
- the disc dryer and the drum dryer are classified into a normal pressure type and a vacuum type according to the operating pressure, and any type can be used.
- the drum dryer is classified into a double drum type, a twin drum type, and a single drum type according to the number of drums, and any of the classifications can be used.
- the single drum type includes a dip type, a spray type, a splash type, an upper roll type (single stage, multiple stages), a side roll type, a lower roll type, etc. depending on the liquid supply method, but any of these types can be used. .. Among them, as the thin film dryer, a disc dryer (disc dryer) is preferable because it saves space and can efficiently recover solid organic solvent-soluble lignin.
- the surface area of the heat transfer surface, the number of rotations of the rotating shaft member, and the flow rate per hour when the extract is added to the heat transfer surface are determined by the composition of the extract to be dried, the amount of the extract, and the like. Therefore, it is a matter that can be appropriately designed by those skilled in the art.
- the solid organic solvent-soluble lignin 3a dried by the thin film dryer 10 can be recovered via the pipe 11, while the volatile component 6 is discharged to the outside of the device via the pipe 12. ..
- FIG. 3 is a schematic configuration diagram showing a recovery system for organic solvent-soluble lignin according to the second embodiment of the present invention.
- the recovery system 200 shown in FIG. 3 is different from the recovery system 100 shown in FIG. 2 in that an extraction device 20 and a solid-liquid separation device 30 are further provided upstream of the thin film dryer 10.
- an extraction device 20 and a solid-liquid separation device 30 are further provided upstream of the thin film dryer 10.
- the same reference numerals are used for the same components as those shown in FIG. 2, and the description thereof will be omitted.
- the recovery system 200 may further include an extraction device 20 upstream of the thin film dryer 10.
- the extraction device 20 is configured to separate the extract 4 containing the organic solvent-soluble lignin from the solid substance 5 containing lignin with a mixed solvent of the organic solvent 2 and water 1.
- the recovery system 200 can obtain an extract 4 containing an organic solvent-soluble lignin from a solid substance 5 containing lignin.
- Examples of the extraction device 20 include known extraction devices such as a rotocell type extraction device, an extraction device including a batch type stirring tank, and a line mixer type extraction device using a screw feeder or the like.
- the organic solvent used as the mixed solvent one having an affinity for water (hydrophilicity) is preferable.
- the solubility in water at 20 ° C. is preferably 90 g / L or more, more preferably 100 g / L or more, still more preferably 120 g / L or more.
- the organic solvent preferably has an SP value of 8 or more and 23 or less, more preferably 8 or more and 16 or less, and further preferably 9 or more and 15 or less, from the viewpoint of improving the extraction rate of the organic solvent-soluble lignin.
- the "SP value” means a solubility parameter (SP value), and the method of Fedors (Reference 1: “Fedors RF," A Method for Estimating Both the Solubility Parameters and Molar Volumes “. of liquids ”, Polymer Engineering and Science, Vol. 14, No. 2, p147-154, 1974.”), and the value ⁇ [(cal / cm 3 ) 1 / 2 ], which is obtained from the square root of the ratio of the total evaporation energy ( ⁇ ei) of the atom or atomic group of the chemical structure of the compound to the total molar volume ( ⁇ vi).
- organic solvent examples include alcohols, nitriles, ethers, and ketones. These organic solvents may be used alone or in combination of two or more.
- alcohols examples include methanol, ethanol, diethylene glycol, n-propanol, isopropanol, 2-butanol, isobutanol, t-butyl alcohol and the like.
- nitriles examples include acetonitrile and the like.
- ethers examples include dioxane, tetrahydrofuran (THF) and the like.
- ketones include acetone, methyl ethyl ketone and the like.
- organic solvent methanol, ethanol, THF, or acetone is preferable, and acetone is more preferable, because the extraction rate of the organic solvent-soluble lignin is excellent. Since these organic solvents have low solubility of biomass saccharified products such as glucose and xylose and do not dissolve cellulose, hemicellulose, etc., lignin can be efficiently extracted.
- the ratio of water to the organic solvent is preferably more than 0/100 and 40/60 or less, more preferably 10/90 or more and 40/60 or less, and further preferably 20/80 or more and 40/60 or less. .. When the ratio is within the above range, the organic solvent-soluble lignin can be extracted more efficiently.
- the water in the mixed solvent also contains the water contained in the solid matter containing lignin.
- an organic solvent preferably acetone or ethanol
- the extraction can be performed under the condition that the ratio of water to the organic solvent is within the above range.
- the amount of the mixed solvent added can be 2 times or more and 20 times or less in terms of mass ratio with respect to the dry mass of the solid containing lignin, and can be 5 times or more and 15 times or less, and is not limited thereto.
- the extraction time can be, for example, 30 minutes or more and 240 minutes or less, and is not limited thereto.
- the extraction temperature (temperature condition until the organic solvent-soluble lignin dissolves in the organic solvent and the extract is obtained) can be carried out under mild temperature conditions equal to or lower than the boiling point of the organic solvent used, for example, room temperature. It can be carried out under the conditions (specifically, about 15 ° C. or higher and 35 ° C. or lower). Other conditions such as the stirring speed can be appropriately set according to the mixing amount of the solid substance containing lignin and the mixed solvent.
- the mixed solution of the solid substance 5 containing lignin and the mixed solvent obtained in the extraction device 20 is sent to the subsequent solid-liquid separation device 30 via the pipe 21 as necessary to separate the extract solution 4. Be liquefied.
- the recovery system 200 may further include a solid-liquid separation device 30 upstream of the thin film dryer 10 and downstream of the extraction device 20.
- the solid-liquid separation device 30 is configured to separate the extract 4 containing the organic solvent-soluble lignin from the mixture of the solid substance 5 containing lignin and the mixed solvent. By providing the solid-liquid separation device 30 in the recovery system 200, the extract 4 containing the organic solvent-soluble lignin can be obtained.
- the solid-liquid separation device 30 a known device capable of separating solid content and liquid content can be used, and examples thereof include, but are not limited to, a filter, a vibrating sieve, a centrifuge, and a screw press.
- the extract 4 obtained by the solid-liquid separator 30 is sent to the subsequent thin film dryer 10 via the pipe 31.
- FIG. 4 is a schematic configuration diagram showing a recovery system for organic solvent-soluble lignin according to the third embodiment of the present invention.
- the recovery system 300 shown in FIG. 4 is different from the recovery system 200 shown in FIG. 3 in that a volatile tank 40 is further provided upstream of the thin film dryer 10 and downstream of the extraction device 20 and the solid-liquid separation device 30.
- the extract 4 obtained by the solid-liquid separation device 30 is sent to the subsequent volatilization tank 40 via the pipe 31.
- the volatile tank 40 is configured to volatilize the volatile component 7 from the extract 4 and concentrate the extract 4 to produce a concentrated solution of the extract (hereinafter, may be simply referred to as "concentrated solution"). Has been done.
- the recovery system 300 can recover the organic solvent-soluble lignin more efficiently while suppressing the energy consumption as compared with the case where the organic solvent-soluble lignin is dried only by the thin film dryer. ..
- the volatile tank 40 may be a batch type or a continuous type. Further, in order to heat the extract, the volatilization tank 40 may be provided with a hot water circulation type jacket, a heating wire, a steam tube, or the like on the outside of the apparatus. As the heat source for heating, known sources such as electricity, steam, and combustion gas can be used. As the stirring method of the volatile tank 40, a shelf (tray) or the like may be provided in the tank in order to increase the volatile area, or a multi-effect can method having a multi-stage layer may be used.
- the treatment temperature in the volatile tank 40 can be, for example, 10 ° C. or higher and 100 ° C. or lower, and 30 ° C. or higher and 80 ° C. or lower.
- the treatment time in the volatile tank 40 can be the time immediately before the above-mentioned aggregation and precipitation of lignin starts in the extract. As shown in Examples described later, the time until immediately before the start of aggregation and precipitation of the above-mentioned lignin can be set using the content of the organic solvent as an index with respect to the total mass of water and the organic solvent in the extract.
- the time required to volatilize a part of the mixed solvent until the content of the organic solvent is 50% by mass or more and 60% by mass or less, preferably 51% by mass or more and 57% by mass, more preferably 53% by mass or more and 55% by mass or less. can do.
- the extract can be concentrated until just before the above-mentioned aggregation and precipitation of lignin begins, as compared with the case where the organic solvent-soluble lignin is dried only by the thin film dryer.
- Organic solvent-soluble lignin can be recovered more efficiently while suppressing energy consumption.
- the specific treatment time for the content of such an organic solvent can be appropriately set according to the treatment temperature and the treatment amount of the extract.
- the organic solvent-soluble lignin 3 with respect to the total mass of the extract. Extract containing 4.5% by mass, water: 34.0% by mass, and organic solvent: 62.5% by mass is treated at 30 ° C. or higher and 80 ° C. or lower for 0.01 hours or more and 24 hours. It can be as follows.
- the concentrated liquid obtained in the volatile tank 40 is sent to the subsequent thin film dryer 10 via the pipe 41.
- FIG. 5 is a schematic configuration diagram showing a recovery system for organic solvent-soluble lignin according to the fourth embodiment of the present invention.
- the recovery system 400 shown in FIG. 5 is different from the recovery system 300 shown in FIG. 4 in that a distillation apparatus (distillation column) 50 is further provided as a separation device downstream of the thin film dryer 10.
- a distillation apparatus (distillation column) 50 is further provided as a separation device downstream of the thin film dryer 10.
- the separation device is configured to separate water and the organic solvent from the volatile components discharged from the thin film dryer and the volatile tank.
- the recovery system of the present embodiment can recover the regenerated solvent 8 consisting only of water and an organic solvent or an organic solvent by providing a separation device. Further, the recovered regenerated solvent 8 can be reused in the extraction device 20.
- the separation device may be any device that can recover water and an organic solvent from volatile components, and examples thereof include a distillation device (distillation column).
- the distillation apparatus may be of a simple distillation method, may have a structure provided with a shelf (tray) inside, or may have a structure filled with a filling material.
- the distillate from the top of the tower which is rich in low boiling point components, is taken out of the device via the pipe 52a and condensed by a condenser 53 or the like.
- the condensed column top distillate is returned to a distillation apparatus via a pipe 52b via a recirculation pump or the like in a constant amount via a regulator for adjusting the recirculation amount and a control valve or the like.
- the recirculation pump, regulator and control valve may be collectively referred to as a recirculation amount adjusting mechanism 55.
- the remaining column top distillate is extracted at a constant flow rate as a regenerating solvent 8 reused in the extraction device 40 via a regulator and a control valve (not shown) for adjusting the flow rate of the remaining column top distillate. ..
- the regulator and control valve that adjust the flow rate of the remaining column top fraction may be collectively referred to as a regenerated solvent flow rate adjustment mechanism (not shown).
- the setting of the extraction flow rate can be changed by the regeneration solvent flow rate adjusting mechanism according to the amount of the regeneration solvent 8 used in the extraction device.
- the regenerated solvent 8 referred to here may be a mixed solvent of an organic solvent and water, or may be a solvent composed only of the organic solvent, but since it is not necessary to newly use the supply water, the organic solvent And water are preferably mixed solvents.
- heating steam is supplied to the reboiler 58 at a constant flow rate by a regulator and a control valve that regulate the flow rate of the reboiler heating steam, and a constant amount of heat is supplied to the distillation apparatus 50.
- the regulator and the regulating valve may be generally referred to as a reboiler heating amount adjusting mechanism 59.
- a large amount of water-rich vapor generated from the reboiler is generated from this heat source, and the inside of the tower is brought into contact with the reflux liquid from above on each tray, and the distillation operation is performed while exchanging heat and substances.
- the amount of steam generated is adjusted by the amount of reboiler fired by the amount of steam for heating the reboiler of the heat source.
- the distillation apparatus 50 preferably has a control unit 51 that controls the reboiler heating amount and the recirculation amount so that the content ratio of water and the organic solvent in the distillation solution is within a predetermined range.
- the control unit 51 controls the reboiler heating amount and the recirculation amount so that the content ratio of water and the organic solvent in the distillation solution is within a predetermined range.
- the mechanism 59 is controlled to control the amount of recirculation and the amount of reboiler heating, respectively. Specifically, by controlling the recirculation amount adjusting mechanism 55 to increase the recirculation amount, the content ratio of the organic solvent in the regenerated solvent 8 can be increased, while by decreasing the recirculation amount, the recirculation amount can be increased. The content ratio of the organic solvent in the regenerated solvent 8 can be reduced. Further, by controlling the reboiler heating amount adjusting mechanism 59 to increase the reboiler heating amount, the water content ratio in the regenerated solvent 8 can be increased, while the reboiler heating amount is decreased. As a result, the water content ratio in the regenerated solvent 8 can be reduced.
- the ratio of water to the organic solvent may be in the range exemplified in the above extraction device in terms of mass ratio, or the water content in the solid containing lignin used as a raw material.
- the content ratio of water and the organic solvent such that the ratio of water to the organic solvent in the mixed solvent in the extraction device 20 is within the range exemplified in the above extraction device in terms of mass ratio. There may be.
- the content ratio of water and the organic solvent in the distillate does not need to be supplied water, the water content in the solid matter containing lignin used as a raw material is taken into consideration, and the content ratio in the extraction device 20 is taken into consideration.
- the content ratio of water and the organic solvent is such that the ratio of water to the organic solvent in the mixed solvent is in the range exemplified in the above-mentioned extraction device in terms of mass ratio.
- the content ratio of such water and the organic solvent is, for example, 40 parts by mass of a solid containing lignin having a water content of 50% by mass with respect to the total mass of the solid: 40 parts by mass of water with respect to the organic solvent.
- Such a range may be stored in the control unit in advance, or the control unit may calculate the ratio of water to the organic solvent in the mixed solvent while operating the extraction device 20 based on the value. ..
- the recovery system 400 may further include a pipe 54 configured to send the distillate obtained by the distillation apparatus 50 to the extraction apparatus 20. By providing the pipe 54, the recovery system 400 can send the regenerated solvent 8 recovered in the distillation device 50 to the extraction device and reuse it.
- the recovery system of the present embodiment is not limited to the recovery system shown in FIGS. 2 to 5, and a part of the configurations shown in FIGS. 2 to 5 is changed or deleted within a range that does not impair the effect of the present invention. Or, other configurations may be added to those described above.
- a saccharification device may be provided upstream of the extraction device.
- the saccharification device is not particularly limited, and a known saccharification device can be used. Specific examples thereof include saccharification devices such as a stirring type, a ventilation stirring type, a bubble tower type, a fluidized bed type, and a packed bed type.
- the saccharification device may be provided with a temperature control device such as a hot water circulation type jacket on the outside of the device in order to keep the temperature inside the device constant.
- a second solid-liquid separation device may be provided downstream of the saccharification device and upstream of the extraction device.
- the second solid-liquid separation device include the same devices as those exemplified in the above-mentioned “solid-liquid separation device”.
- a pretreatment device may be provided upstream of the saccharification device.
- the pretreatment apparatus is preferably a reaction vessel used in the dilute sulfuric acid cooking method.
- the reaction vessel used in the dilute sulfuric acid cooking method is not particularly limited as long as it is a steam supply type, but has, for example, a heating pressure device such as an autoclave having acid resistance or a heating pressure vessel having acid resistance.
- a heating pressure device such as an autoclave having acid resistance or a heating pressure vessel having acid resistance.
- the screw feeder is integrated to perform continuous processing.
- the recovery method of the present embodiment includes a drying step. By including a drying step, the recovery method of the present embodiment can stably recover solid organic solvent-soluble lignin that does not contain water and does not recondense.
- drying method examples include a method using the above-mentioned thin film dryer.
- the drying time may be a short time such that lignin does not precipitate, and can be appropriately selected depending on the drying temperature and the like.
- the drying time can be 2 seconds or more and 60 seconds or less, and 2.5 seconds or more. It can be 30 seconds or less.
- the drying temperature can be set to a temperature condition such that the temperature of the heat transfer surface of the member having the heat transfer surface of the thin film dryer is, for example, 80 ° C. or higher and 130 ° C. or lower.
- volatile components discharged in the drying process can be used in the reuse process described later.
- the recovery method of the present embodiment may further include a collection step after the drying step.
- Examples of the collection method include a method using the above-mentioned scraping mechanism. That is, the collection process can also be said to be a scraping process. By scraping and recovering the thin-film dried product formed on the heat transfer surface of the thin-film dryer, the thin-film dried product can be crushed and the powdered organic solvent-soluble lignin can be recovered. it can.
- the drying step and the collecting step are alternately and continuously performed.
- the drying step and the collecting step are alternately and continuously performed.
- the recovery method of the present embodiment may further include an extraction step before the drying step.
- the recovery method of the present embodiment can obtain an extract containing organic solvent-soluble lignin from a solid substance containing lignin.
- the extraction step is a step of mixing a solid containing lignin with a mixed solvent of an organic solvent and water, and separating an extract containing an organic solvent-soluble lignin.
- the extraction method may be a method of mixing and stirring a solid substance containing lignin with a mixed solvent of an organic solvent and water to dissolve the organic solvent-soluble lignin in the organic solvent.
- extraction device a method of mixing and stirring a solid substance containing lignin with a mixed solvent of an organic solvent and water to dissolve the organic solvent-soluble lignin in the organic solvent.
- the illustrated device can be used.
- extraction conditions such as the composition of the mixed solvent used, the amount of the mixed solvent added, the extraction time and the extraction temperature are the same as those exemplified in the above "extraction device".
- the mixed solution is dissolved by allowing it to stand for a predetermined time.
- examples thereof include a method in which the missing solid content is precipitated and transferred to the lower layer, and after the liquid content is transferred to the upper layer, only the liquid component of the upper layer is extracted.
- a method of separating an extract containing an organic solvent-soluble lignin from the mixture by using a solid-liquid separation method can be mentioned. Of these, a method of separating the extract containing the organic solvent-soluble lignin from the mixture by using a solid-liquid separation method is preferable.
- the recovery method of the present embodiment may further include a solid-liquid separation step after the extraction step and before the drying step.
- Solid-liquid separation process In the solid-liquid separation step, an extract containing organic solvent-soluble lignin is separated from a mixture of a solid containing lignin and a mixed solvent of an organic solvent and water by a solid-liquid separation method.
- the recovery method of the present embodiment can easily and efficiently separate the extract from the mixture.
- a method for solid-liquid separation a known method for separating solid content and liquid content can be used.
- a method of filtering with a filter, a vibrating sieve or the like, a centrifugal separation method, a separation method using a screw press, or the like can be used. These are, but are not limited to.
- the recovery method of the present embodiment may further include a volatilization step before the drying step and after the extraction step (after the solid-liquid separation step).
- volatilization process In the volatilization step, a part of the mixed solvent contained in the extract is volatilized.
- the recovery method of the present embodiment includes a volatilization step, so that the organic solvent-soluble lignin can be recovered more efficiently while suppressing energy consumption as compared with the case where the organic solvent-soluble lignin is dried only by the above-mentioned drying step. Can be done.
- the volatile component obtained by volatilizing a part of the mixed solvent contained in the extract in the volatilization step can be used in the reuse step described later.
- the recovery method of the present embodiment may further include a separation step after the drying step.
- the separation step water and the organic solvent are separated from the volatile components discharged in the drying step and the volatilization step.
- the recovery method of the present embodiment can recover a regenerated solvent consisting only of water and an organic solvent or an organic solvent from a volatile component.
- the recovered regenerated solvent can be reused in the above-mentioned extraction step.
- the method for separating water and the organic solvent by the distillation method is the same as that exemplified in the above-mentioned "separation device".
- the separation method examples include a distillation method and the like. That is, when the separation method is a distillation method, the separation step can also be said to be a distillation step.
- the recovery method of the present embodiment may further include a reuse step after the distillation step.
- the distillation solution (also referred to as a regenerated solvent) obtained in the distillation step is reused in the extraction step.
- the reboiler heating amount and the recirculation amount are controlled so that the content ratio of water and the organic solvent is within a predetermined range.
- the method of controlling the reboiler heating amount and the recirculation amount so that the content ratios of water and the organic solvent are within a predetermined range is the same as that exemplified in the above-mentioned "separation device".
- the content ratio of water and the organic solvent in the mixed solution used in the extraction step is the mass ratio of the water content to the organic solvent exemplified in the above "extractor".
- the supply amount of the distillation solution (regeneration solvent) obtained in the distillation step and the supply amount of water are controlled.
- the supply amount of the distillate (regenerated solvent) can be changed by the regenerated solvent flow rate adjusting mechanism described above.
- the water supply amount can be changed by a regulator and a control valve (these may be collectively referred to as a "supply water flow rate adjusting mechanism") for adjusting the flow rate of the supply water.
- a regulator and a control valve which may be collectively referred to as a "supply water flow rate adjusting mechanism" for adjusting the flow rate of the supply water.
- the supply amount of water is substantially 0). Is preferable.
- the recovery method of the present embodiment may further include other steps in addition to the above steps.
- the recovery method of the present embodiment may further include a saccharification step before the extraction step.
- a saccharification reaction is carried out using an enzyme using cellulose and hemicellulose contained in a solid substance containing lignin (lignocellulose-based biomass) as substrates.
- the recovery method of the present embodiment can effectively utilize the residue (saccharification residue) after removing the useful component contained in the lignocellulosic biomass.
- the enzyme referred to here is mainly a saccharifying enzyme.
- examples of the "saccharifying enzyme” include cellulase that decomposes cellulose, hemicellulose that decomposes hemicellulose, and amylase that decomposes starch.
- the cellulase may be any cellulase that decomposes cellulose into monosaccharides such as glucose or oligosaccharides, for example, endoglucanase (EG), cellobiohydrolase (CBH), and ⁇ -glucosidase ( ⁇ ).
- EG endoglucanase
- CBH cellobiohydrolase
- ⁇ ⁇ -glucosidase
- BGL has at least one activity of each activity, and an enzyme mixture having each of these activities is preferable from the viewpoint of enzyme activity.
- the hemicellulase may be any one that decomposes hemicellulose into monosaccharides such as xylose or oligosaccharides, and for example, at least one activity of each activity of xylanase, xylosidase, mannanase, galactosidase, glucuronidase, and arabinofuranosidase. From the viewpoint of enzyme activity, it is preferable that the enzyme mixture has each of these activities.
- saccharifying enzymes such as cellulase and hemicellulase is not limited, and for example, Trichoderma, Acremonium, Aspergillus, Bacillus, Pseudomonas.
- Saccharifying enzymes such as cellulases and hemicellulase derived from microorganisms such as the genus Penicillium, Aeromonus, Irpex, Sporotichum, and Humicola can be used.
- the saccharification temperature is preferably 45 ° C. or higher and 70 ° C. or lower, more preferably 45 ° C. or higher and 55 ° C. or lower, and particularly preferably 50 ° C.
- the saccharification time is preferably 12 hours or more and 120 hours or less, more preferably 24 hours or more and 96 hours or less, and further preferably 24 hours or more and 72 hours or less.
- the recovery method of the present embodiment may further include a second solid-liquid separation step before the extraction step and after the saccharification step.
- the saccharification treatment product obtained in the saccharification step is solid-liquid separated and separated into a saccharification solution which is a liquid fraction and a saccharification residue which is a solid fraction to obtain a saccharification residue. obtain.
- the recovery method of the present embodiment can easily separate the saccharified solution and the saccharified residue by including the second solid-liquid separation step. Examples of the method for solid-liquid separation include the same methods as those exemplified in the above-mentioned “solid-liquid separation step”.
- the saccharified solution obtained in the second solid-liquid separation step may be refined by removing impurities from the saccharified solution and sold as molasses, or an organic solvent produced by microbial fermentation of the saccharified solution. It may be used to produce a useful ingredient different from soluble lignin.
- the useful component different from the organic solvent-soluble lignin means a compound produced by ingesting monosaccharides and oligosaccharides obtained by decomposing herbaceous biomass by microorganisms such as yeast.
- useful components include alcohols such as ethanol, butanol, 1,3-propanediol, 1,4-butanediol, and glycerol; pyruvic acid, succinic acid, malic acid, inosinic acid, citric acid, lactic acid, and the like.
- the compound obtained by fermentation is a monomer such as lactic acid, it may be converted into a polymer by polymerization.
- ethanol is preferable as a useful component different from the organic solvent-soluble lignin.
- the recovery method of the present embodiment may further include a pretreatment step before the saccharification step.
- the pretreatment step is a step of pretreating a solid substance (lignocellulose-based biomass) containing lignin in order to efficiently carry out the saccharification reaction in the subsequent saccharification step.
- the recovery method of the present embodiment can efficiently carry out the subsequent saccharification step.
- Examples of the pretreatment method for lignocellulosic biomass include a steaming method using only steam, a method using an ionic liquid, and a crushing method using a mill. Further, in the pretreatment step, an acid or an alkali may be appropriately mixed, if necessary.
- the acid is selected from sulfuric acid (including dilute sulfuric acid), hydrochloric acid, nitric acid, phosphoric acid and the like, and these may be used alone or in combination. Of these, sulfuric acid, which is inexpensive and easily available for industrial use, is particularly preferable.
- the alkali is selected from sodium hydroxide, potassium hydroxide, and ammonia, and these may be used alone or in combination. Above all, as a pretreatment method, a dilute sulfuric acid cooking method using dilute sulfuric acid is preferable.
- Example 1 ⁇ Preparation of extract containing organic solvent-soluble lignin> Napiergrass: 165 kg-dry, which is a herbaceous biomass, is pretreated by a dilute sulfuric acid cooking method, saccharified using a saccharifying enzyme (mixture of cellulase and hemicellulase), and then the obtained saccharified solution is centrifuged. Solid-liquid separation was performed using a machine to obtain a saccharified residue: 29 kg-dry. Then, the obtained saccharified residue was dried to obtain a dried saccharified residue.
- a saccharifying enzyme mixture of cellulase and hemicellulase
- the obtained dried saccharified residue 3.5 kg-dry was added to 31.5 kg each of a mixed solvent of acetone or ethanol and water (mixing ratio: 60/40 by mass ratio), and at room temperature (20 ° C.). After stirring for 30 minutes, solid-liquid separation was performed using a centrifuge to obtain an extract and an extraction residue.
- the disk dryer By setting the rotation speed of the disk dryer to 20 rpm, the disk rotates once in about 3 seconds, and the solvent in the extract applied to the surface of the disk volatilizes before the above-mentioned aggregation and precipitation of lignin appears, resulting in a solid state.
- the organic solvent-soluble lignin (powder) of the above was able to be recovered.
- Example 2 ⁇ Examination of solvent volatilization conditions for organic solvent-soluble lignin-containing extract> An extract containing an organic solvent-soluble lignin was prepared using the same method as in Example 1. The composition of the extract was 20% by mass of the organic solvent-soluble lignin and 80% by mass of the solvent with respect to the total mass of the extract. The composition of the solvent is 60% by mass of acetone or ethanol (48% by mass with respect to the total mass of the extract) and 40% by mass of water (32% by mass with respect to the total mass of the extract) with respect to the total mass of the solvent. )Met.
- FIG. 7 is a graph showing the change over time in the volatilization rate of the organic solvent (acetone or ethanol) in the extract. Precipitates were observed on the liquid surface when the volatility of acetone was 15% by mass and that of ethanol was 31% by mass. At this time, the content of acetone in the extract remaining in the beaker was 55% by mass with respect to the total mass of the extract remaining in the beaker. The content of ethanol in the extract remaining in the beaker was 53% by mass with respect to the total mass of the extract remaining in the beaker.
- the organic solvent acetone or ethanol
- organic solvent-soluble lignin recovery system and recovery method of the present embodiment it is possible to provide a recovery system and recovery method for organic solvent-soluble lignin that can stably obtain solid lignin.
Abstract
Description
本願は、2019年9月10日に、日本に出願された特願2019-164255号に基づき優先権を主張し、その内容をここに援用する。
(1) 有機溶媒可溶性リグニンの回収システムであって、
リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された有機溶媒可溶性リグニンを含む抽出液を乾燥し、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を形成するように構成された薄膜式乾燥機を備える、回収システム。
(2) 前記薄膜式乾燥機は、前記乾燥物を掻き取るように構成された掻き取り機構を有する、(1)に記載の回収システム。
(3) 前記薄膜式乾燥機の上流に、前記固形物から前記混合溶媒により前記抽出液を分離するように構成された抽出装置を更に備える、(1)又は(2)に記載の回収システム。
(4) 前記薄膜式乾燥機の上流であって前記抽出装置の下流に、揮発槽を更に備える、(3)に記載の回収システム。
(5) 前記薄膜式乾燥機の下流に、前記薄膜式乾燥機及び前記揮発槽から排出された揮発性成分から水及び有機溶媒を分離するように構成された分離装置を更に備える、(4)に記載の回収システム。
(6) 前記分離装置が蒸留装置である、(5)に記載の回収システム。
(7) 前記蒸留装置で得られた蒸留液を前記抽出装置に送液するように構成された配管を更に備え、
前記蒸留装置は、前記蒸留液中の水及び有機溶媒の含有量比が所定の範囲となるようにリボイラー焚き上げ量及び還流量を制御する制御部を有する、(6)に記載の回収システム。
リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された有機溶媒可溶性リグニンを含む抽出液を乾燥し、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を形成させる乾燥工程を含む、回収方法。
(9) 前記乾燥工程後に、前記乾燥物を収集する収集工程を更に含む、(8)に記載の回収方法。
(10) 前記乾燥工程前に、前記固形物と前記混合溶媒とを混合し、前記抽出液を分離する抽出工程を更に含む、(8)又は(9)に記載の回収方法。
(11) 前記乾燥工程前であって前記抽出工程後に、前記抽出液に含まれる前記混合溶媒の一部を揮発させる揮発工程を更に含む、(10)に記載の回収方法。
(12) 前記揮発工程において、前記抽出液中の水及び有機溶媒の合計質量に対して、有機溶媒の含有量が50質量%以上60質量%未満となるまで前記混合溶媒の一部を揮発させる、(11)に記載の回収方法。
(13) 前記乾燥工程後に、前記乾燥工程及び前記揮発工程で排出された揮発性成分から水及び有機溶媒を分離する分離工程を更に含む、(11)又は(12)に記載の回収方法。
(14) 前記分離工程は、蒸留法により行われる蒸留工程である、(13)に記載の回収方法。
(15) 前記蒸留工程後に、前記蒸留工程で得られた蒸留液を前記抽出工程に再利用する再利用工程を更に含み、
前記蒸留工程において、前記蒸留液中の水及び有機溶媒の含有量比が所定の範囲となるようにリボイラー焚き上げ量及び還流量を制御する、(14)に記載の回収方法。
(16) 前記再利用工程において、前記抽出工程で用いられる前記混合溶媒中の水及び有機溶媒の含有量比となるように、前記蒸留液の供給量及び水の供給量を制御する、(15)に記載の回収方法。
本実施形態の回収システム及び回収方法において原料として用いられるリグニンを含む固形物としては、例えば、リグノセルロース系バイオマスが挙げられる。リグノセルロース系バイオマスとしては、例えば、木本植物(木本系バイオマスともいう)、草本植物(草本系バイオマスともいう)、それらの加工物及びそれらの廃棄物からなる群より選ばれる少なくとも1種であればその種類は問わない。また、リグノセルロース系バイオマスは粉砕されたものを用いることができ、また、ブロック、チップ、粉末等、いずれの形状でもよい。また、リグニンを含む固形物としては、リグノセルロース系バイオマス中のセルロース及びヘミセルロースからバイオエタノール、バイオブタノール又はバイオ化学品等を製造する過程で発生した残渣を用いてもよい。当該残渣である場合、リグノセルロース系バイオマスを希硫酸蒸解法により前処理し、さらに、得られた前処理原料を酵素糖化法により分解した後に残留する糖化残渣であることが好ましい。
一般に、リグニンは、草本系バイオマスの3大主成分の一つの天然高分子である。草本系バイオマスの中でもバガスには、5質量%以上30質量%以下のリグニンが含まれる。
本明細書において、「セルロース」には、6つの炭素を構成単位とする六炭糖が含まれる。よって、セルロースは加水分解を受けると、炭素6つからなる六炭糖の単糖(グルコース等)やその単糖が複数個連結された六炭糖のオリゴ糖(セロビオース等)を生ずる。
本実施形態の回収システムは、リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された有機溶媒可溶性リグニンを含む抽出液を乾燥し、薄膜状の乾燥物を形成するように構成された薄膜式乾燥機を備える。
よって、本実施形態の回収システムは、上記構成の薄膜式乾燥機を備えることで、水を包含せず再凝縮しない固体状の有機溶媒可溶性リグニンを安定的に回収することができる。
薄膜式乾燥機10は、前記抽出液4から揮発性成分6(主に、混合溶媒)を揮発させて、前記抽出液4中に含まれる固形分(主に、固体状の有機溶媒可溶性リグニン3a)からなる薄膜状の乾燥物を形成するように構成されている。薄膜式乾燥機10としては、例えば、伝熱面を含む部材を有するものが挙げられる。伝熱面を含む部材は、当該伝熱面が蒸気等により加温されるように構成されている。さらに、伝熱面を含む部材は、当該伝熱面に前記抽出液を薄く塗布し、前記抽出液から揮発性成分を上述したリグニンの凝集析出が発露する前に揮発させることで、薄膜状の乾燥物を形成することができる。なお、薄膜状の乾燥物とは、その厚みが300μm以下の乾燥物をいう。伝熱面の形状としては、特に限定されず、平面状であってもよく、立体面状であってもよい。平面状である場合には、例えば、略円形状(真円状を含む)、中空略円形状(中空真円状を含む)、扇形状、環状扇形状、多角形状等が挙げられるが、略円形状(真円状を含む)、中空略円形状(中空真円状を含む)、扇形状又は環状扇形状が好ましい。立体面状である場合には、例えば、円柱状、角柱状、角錐状、角錐台状、円錐状、円錐台状等が挙げられるが、円柱状が好ましい。
伝熱面の材質は、熱を伝導しやすいものであればよいが、後述する掻き取り機構による掻き取り操作に耐えうる耐摩耗性に優れる材質であることが好ましく、例えば、硬質クロムメッキや無電解ニッケルメッキ等が施された鋼材等が挙げられる。
掻き取り機構として具体的には、例えば、スクレーパー等が挙げられる。スクレーパーは、刃状(ナイフ状、ブレード状ともいう)であってもよく、へら状であってもよい。なお、掻き取り機構とは、乾燥物が位置する表面上をこすることで、乾燥物を表面から剥がしとる機構を意味する。
回収システム200は、薄膜式乾燥機10の上流に、抽出装置20を更に備えていてもよい。抽出装置20は、リグニンを含む固形物5から有機溶媒2及び水1の混合溶媒により有機溶媒可溶性リグニンを含む抽出液4を分離するように構成されている。回収システム200は、抽出装置20を備えることで、リグニンを含む固形物5から有機溶媒可溶性リグニンを含む抽出液4を得ることができる。
回収システム200は、薄膜式乾燥機10の上流であって抽出装置20の下流に、固液分離装置30を更に備えていてもよい。固液分離装置30は、リグニンを含む固形物5と混合溶媒との混合液から有機溶媒可溶性リグニンを含む抽出液4を分離するように構成されている。回収システム200は、固液分離装置30を備えることで、有機溶媒可溶性リグニンを含む抽出液4を得ることができる。
揮発槽40は、抽出液4から揮発性成分7を揮発させて、抽出液4を濃縮して抽出液の濃縮液(以下、単に「濃縮液」と称する場合がある)を製造するように構成されている。回収システム300は、揮発槽40を備えることで、薄膜式乾燥機のみによって有機溶媒可溶性リグニンを乾燥させる場合よりも、エネルギー消費量を抑えながら、より効率よく有機溶媒可溶性リグニンを回収することができる。
そのような有機溶媒の含有量となる具体的な処理時間としては、処理温度や抽出液の処理量に応じて適宜設定できるが、例えば、抽出液の総質量に対して有機溶媒可溶性リグニン:3.5質量%、水:34.0質量%、及び有機溶媒:62.5質量%を含有する抽出液:40Lを、30℃以上80℃以下で処理する場合において、0.01時間以上24時間以下程度とすることができる。
分離装置は、薄膜式乾燥機及び揮発槽から排出された揮発性成分から水及び有機溶媒を分離するように構成されている。本実施形態の回収システムは、分離装置を備えることで、水及び有機溶媒又は有機溶媒のみからなる再生溶媒8を回収することができる。また、回収された再生溶媒8は、抽出装置20に再利用することができる。
例えば、図2~図5に示す回収システムにおいて、抽出装置の上流に糖化装置を備えていてもよい。糖化装置としては、特別な限定はなく、公知の糖化装置を用いることができる。具体的には、撹拌型、通気撹拌型、気泡塔型、流動層型、充填層型等の糖化装置が挙げられる。また、糖化装置は、装置内の温度を一定に保つために、装置の外側に温水循環式のジャケット等の温度調節装置を備えてもよい。
また、例えば、図2~5に示す回収システムにおいて、糖化装置の下流であって、抽出装置の上流に第2の固液分離装置を備えていてもよい。第2の固液分離装置としては、上記「固液分離装置」において例示されたものと同様のものが挙げられる。
また、例えば、図2~5に示す回収システムにおいて、糖化装置の上流に前処理装置を備えていてもよい。前処理装置としては、希硫酸蒸解法に用いられる反応容器であることが好ましい。希硫酸蒸解法に用いられる反応容器としては、蒸気供給式のものであれば特に限定はないが、例えば、耐酸性を有するオートクレーブのような加熱圧力装置、又は耐酸性を有する加熱圧力容器を有し、さらにスクリューフィーダーが一体となり連続的に処理を行なえる装置等が挙げられる。
本実施形態の回収方法は、乾燥工程を含む。本実施形態の回収方法は、乾燥工程を備えることで、水を包含せず再凝縮しない固体状の有機溶媒可溶性リグニンを安定的に回収することができる。
乾燥工程では、リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された有機溶媒可溶性リグニンを含む抽出液を乾燥し、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を形成させる。
収集工程では、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を収集する。
抽出工程では、リグニンを含む固形物と有機溶媒及び水の混合溶媒とを混合し、有機溶媒可溶性リグニンを含む抽出液を分離する工程である。
固液分離工程では、リグニンを含む固形物と有機溶媒及び水の混合溶媒との混合液から固液分離法により有機溶媒可溶性リグニンを含む抽出液を分離する。本実施形態の回収方法は、固液分離工程を含むことで、前記混合液から前記抽出液を簡便かつ効率よく分離することができる。
揮発工程では、抽出液に含まれる混合溶媒の一部を揮発させる。本実施形態の回収方法は、揮発工程を含むことで、上述した乾燥工程のみによって有機溶媒可溶性リグニンを乾燥させる場合よりも、エネルギー消費量を抑えながら、より効率よく有機溶媒可溶性リグニンを回収することができる。
分離工程では、乾燥工程及び揮発工程で排出された揮発性成分から水及び有機溶媒を分離する。本実施形態の回収方法は、分離工程を含むことで、揮発性成分から水及び有機溶媒又は有機溶媒のみからなる再生溶媒を回収することができる。また、回収された再生溶媒は、上述した抽出工程において再利用することができる。蒸留法による水及び有機溶媒を分離する方法としては、上記「分離装置」において例示されたものと同様である。
再利用工程では、蒸留工程で得られた蒸留液(再生溶媒ともいう)を抽出工程に再利用する。
中でも、新たな水を使用せずにすむことから、供給水を用いずに(すなわち、水の供給量が実質的に0であり)、蒸留液(再生溶媒)の供給量のみを制御することが好ましい。
本実施形態の回収方法は、上記工程に加えて、その他の工程を更に含んでもよい。
例えば、本実施形態の回収方法は、抽出工程前に糖化工程を更に含んでもよい。糖化工程ではリグニンを含む固形物(リグノセルロース系バイオマス)に含まれるセルロース及びヘミセルロースを基質として、酵素を用いて、糖化反応を行なう。本実施形態の回収方法は、糖化工程を含むことで、リグノセルロース系バイオマスに含まれる有用成分を取り除いた後の残渣(糖化残渣)を有効活用することができる。ここでいう酵素とは、主に糖化酵素である。
例えば、本実施形態の回収方法は、抽出工程前であって糖化工程後に、第2の固液分離工程を更に含んでもよい。第2の固液分離工程では、糖化工程で得られた糖化処理生成物を固液分離して、液体分画である糖化液と固体分画である糖化残渣とに分けることで、糖化残渣を得る。本実施形態の回収方法は、第2の固液分離工程を含むことで、糖化液と糖化残渣とを簡便に分離することができる。固液分離する方法としては、上記「固液分離工程」において例示された方法と同様のものが挙げられる。
例えば、本実施形態の回収方法は、糖化工程前に、前処理工程を更に含んでもよい。前処理工程では、続く糖化工程において、糖化反応を効率的に行うためにリグニンを含む固形物(リグノセルロース系バイオマス)を前処理する工程である。本実施形態の回収方法は、前処理工程を含むことで、続く糖化工程を効率よく行なうことができる。
<有機溶媒可溶性リグニン含有抽出液の調製>
草本系バイオマスであるネピアグラス:165kg-dryについて、希硫酸蒸解法により前処理を行い、糖化酵素(セルラーゼ及びヘミセルラーゼの混合物)を用いて糖化を行なった後、得られた糖化液を遠心分離機を用いて固液分離し、糖化残渣:29kg-dryを得た。
次いで、得られた糖化残渣を乾燥させて糖化残渣乾燥物を得た。得られた糖化残渣乾燥物:3.5kg-dryを、アセトン又はエタノールと水との混合溶媒(混合比は質量比で60/40)各31.5kgに添加し、室温(20℃)下で30分間攪拌した後、遠心分離機を用いて固液分離し、抽出液と抽出残渣とを得た。
次いで、上記において得られた抽出液をディスクドライヤー(図6A及び図6B参照)を用いて、乾燥させた。乾燥条件は以下に示すとおりである。
回転数:3rpm以上20rpm
蒸気温度:110℃
ディスク直径:540mm
有効面積(両面):0.4m2
対象試料:抽出液
抽出液の塗布速度:15g/秒
<有機溶媒可溶性リグニン含有抽出液の溶媒揮発条件の検討>
実施例1と同様の方法を用いて、有機溶媒可溶性リグニンを含有する抽出液を調製した。抽出液の組成は、抽出液の総質量に対して、有機溶媒可溶性リグニン20質量%、溶媒80質量%であった。また、溶媒の組成は、溶媒の総質量に対してアセトン又はエタノール60質量%(抽出液の総質量に対して48質量%)、水40質量%(抽出液の総質量に対して32質量%)であった。
2:有機溶媒
3:有機溶媒可溶性リグニン
3a:固体状の有機溶媒可溶性リグニン
4:抽出液
5:リグニンを含む固形物
6,7:揮発性成分
8:再生溶媒
9:塔底廃液
10:薄膜式乾燥機
11,12、21,31,41,42,43,52a,52b,52c,54,56a,56b,56c,56d,57:配管
20:抽出装置
30:固液分離装置
40:揮発槽
50:蒸留装置(蒸留塔)
51:制御部
53:凝縮器(コンデンサー)
55:還流量調節機構
58:再沸器(リボイラー)
59:リボイラー焚き上げ量調節機構
100,200,300,400:有機溶媒可溶性リグニンの回収システム
Claims (16)
- 有機溶媒可溶性リグニンの回収システムであって、
リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された抽出液を乾燥し、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を形成するように構成された薄膜式乾燥機を備える、回収システム。 - 前記薄膜式乾燥機は、前記乾燥物を掻き取るように構成された掻き取り機構を有する、請求項1に記載の回収システム。
- 前記薄膜式乾燥機の上流に、前記固形物から前記混合溶媒により前記抽出液を分離するように構成された抽出装置を更に備える、請求項1又は2に記載の回収システム。
- 前記薄膜式乾燥機の上流であって前記抽出装置の下流に、揮発槽を更に備える、請求項3に記載の回収システム。
- 前記薄膜式乾燥機の下流に、前記薄膜式乾燥機及び前記揮発槽から排出された揮発性成分から水及び有機溶媒を分離するように構成された分離装置を更に備える、請求項4に記載の回収システム。
- 前記分離装置が蒸留装置である、請求項5に記載の回収システム。
- 前記蒸留装置で得られた蒸留液を前記抽出装置に送液するように構成された配管を更に備え、
前記蒸留装置は、前記蒸留液中の水及び有機溶媒の含有量比が所定の範囲となるようにリボイラー焚き上げ量及び還流量を制御する制御部を有する、請求項6に記載の回収システム。 - 有機溶媒可溶性リグニンの回収方法であって、
リグニンを含む固形物から有機溶媒及び水の混合溶媒により抽出された抽出液を乾燥し、固体状の有機溶媒可溶性リグニンを含む薄膜状の乾燥物を形成させる乾燥工程を含む、回収方法。 - 前記乾燥工程後に、前記乾燥物を収集する収集工程を更に含む、請求項8に記載の回収方法。
- 前記乾燥工程前に、前記固形物と前記混合溶媒とを混合し、前記抽出液を分離する抽出工程を更に含む、請求項8又は9に記載の回収方法。
- 前記乾燥工程前であって前記抽出工程後に、前記抽出液に含まれる前記混合溶媒の一部を揮発させる揮発工程を更に含む、請求項10に記載の回収方法。
- 前記揮発工程において、前記抽出液中の水及び有機溶媒の合計質量に対して、有機溶媒の含有量が50質量%以上60質量%未満となるまで前記混合溶媒の一部を揮発させる、請求項11に記載の回収方法。
- 前記乾燥工程後に、前記乾燥工程及び前記揮発工程で排出された揮発性成分から水及び有機溶媒を分離する分離工程を更に含む、請求項11又は12に記載の回収方法。
- 前記分離工程は、蒸留法により行われる蒸留工程である、請求項13に記載の回収方法。
- 前記蒸留工程後に、前記蒸留工程で得られた蒸留液を前記抽出工程に再利用する再利用工程を更に含み、
前記蒸留工程において、前記蒸留液中の水及び有機溶媒の含有量比が所定の範囲となるようにリボイラー焚き上げ量及び還流量を制御する、請求項14に記載の回収方法。 - 前記再利用工程において、前記抽出工程で用いられる前記混合溶媒中の水及び有機溶媒の含有量比となるように、前記蒸留液の供給量及び水の供給量を制御する、請求項15に記載の回収方法。
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2013241391A (ja) * | 2011-12-20 | 2013-12-05 | Kao Corp | リグニン分解物の製造方法 |
JP2014015439A (ja) * | 2012-07-11 | 2014-01-30 | Idemitsu Kosan Co Ltd | リグニン分解物の製造方法 |
JP2014189491A (ja) * | 2013-03-26 | 2014-10-06 | Maniwa Bio-Material Kk | リグニンの抽出方法 |
JP2015157792A (ja) * | 2014-02-25 | 2015-09-03 | 国立研究開発法人産業技術総合研究所 | リグニン分解物の製造方法 |
JP2016050200A (ja) * | 2014-08-29 | 2016-04-11 | 日本化薬株式会社 | 低分子リグニンの製造方法 |
WO2017222084A1 (ja) * | 2016-09-09 | 2017-12-28 | 出光興産株式会社 | 二段プロセスによる植物系バイオマス由来生成物の製造方法 |
WO2018047928A1 (ja) * | 2016-09-09 | 2018-03-15 | 出光興産株式会社 | 耐熱性リグニンの製造方法 |
WO2018047772A1 (ja) * | 2016-09-09 | 2018-03-15 | 出光興産株式会社 | リグニン含有樹脂組成物の製造方法及びリグニン含有樹脂成形品 |
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Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2013241391A (ja) * | 2011-12-20 | 2013-12-05 | Kao Corp | リグニン分解物の製造方法 |
JP2014015439A (ja) * | 2012-07-11 | 2014-01-30 | Idemitsu Kosan Co Ltd | リグニン分解物の製造方法 |
JP2014189491A (ja) * | 2013-03-26 | 2014-10-06 | Maniwa Bio-Material Kk | リグニンの抽出方法 |
JP2015157792A (ja) * | 2014-02-25 | 2015-09-03 | 国立研究開発法人産業技術総合研究所 | リグニン分解物の製造方法 |
JP2016050200A (ja) * | 2014-08-29 | 2016-04-11 | 日本化薬株式会社 | 低分子リグニンの製造方法 |
WO2017222084A1 (ja) * | 2016-09-09 | 2017-12-28 | 出光興産株式会社 | 二段プロセスによる植物系バイオマス由来生成物の製造方法 |
WO2018047928A1 (ja) * | 2016-09-09 | 2018-03-15 | 出光興産株式会社 | 耐熱性リグニンの製造方法 |
WO2018047772A1 (ja) * | 2016-09-09 | 2018-03-15 | 出光興産株式会社 | リグニン含有樹脂組成物の製造方法及びリグニン含有樹脂成形品 |
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