JP2015178639A - Method for producing solid fuel from lignocellulosic material - Google Patents
Method for producing solid fuel from lignocellulosic material Download PDFInfo
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- JP2015178639A JP2015178639A JP2015123361A JP2015123361A JP2015178639A JP 2015178639 A JP2015178639 A JP 2015178639A JP 2015123361 A JP2015123361 A JP 2015123361A JP 2015123361 A JP2015123361 A JP 2015123361A JP 2015178639 A JP2015178639 A JP 2015178639A
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- solid fuel
- lignocellulosic material
- hydrothermal treatment
- treatment
- hemicellulose
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- 239000004449 solid propellant Substances 0.000 title claims abstract description 38
- 239000012978 lignocellulosic material Substances 0.000 title claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 238000010335 hydrothermal treatment Methods 0.000 claims abstract description 36
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 230000018044 dehydration Effects 0.000 claims abstract description 21
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 21
- 238000007906 compression Methods 0.000 claims abstract description 17
- 230000006835 compression Effects 0.000 claims abstract description 16
- 150000002772 monosaccharides Chemical class 0.000 claims abstract description 6
- 229920001542 oligosaccharide Polymers 0.000 claims abstract description 6
- 150000002482 oligosaccharides Chemical class 0.000 claims abstract description 6
- 150000001875 compounds Chemical class 0.000 claims abstract description 5
- 239000002994 raw material Substances 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 7
- 229920002488 Hemicellulose Polymers 0.000 abstract description 33
- 238000001035 drying Methods 0.000 abstract description 15
- 238000005903 acid hydrolysis reaction Methods 0.000 abstract description 14
- 238000000034 method Methods 0.000 abstract description 11
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 19
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 17
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 description 13
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 description 13
- 239000000463 material Substances 0.000 description 10
- 238000000855 fermentation Methods 0.000 description 9
- 230000004151 fermentation Effects 0.000 description 9
- 238000000354 decomposition reaction Methods 0.000 description 8
- 241000219927 Eucalyptus Species 0.000 description 7
- 239000007857 degradation product Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- 239000002028 Biomass Substances 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 239000000446 fuel Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 238000007654 immersion Methods 0.000 description 4
- 238000005259 measurement Methods 0.000 description 4
- 238000011002 quantification Methods 0.000 description 4
- 240000007472 Leucaena leucocephala Species 0.000 description 3
- 235000010643 Leucaena leucocephala Nutrition 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- HEBKCHPVOIAQTA-NGQZWQHPSA-N d-xylitol Chemical compound OC[C@H](O)C(O)[C@H](O)CO HEBKCHPVOIAQTA-NGQZWQHPSA-N 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000000523 sample Substances 0.000 description 3
- 239000012488 sample solution Substances 0.000 description 3
- 238000005979 thermal decomposition reaction Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical group N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- 238000011088 calibration curve Methods 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000003480 eluent Substances 0.000 description 2
- 230000002255 enzymatic effect Effects 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- PKAUICCNAWQPAU-UHFFFAOYSA-N 2-(4-chloro-2-methylphenoxy)acetic acid;n-methylmethanamine Chemical compound CNC.CC1=CC(Cl)=CC=C1OCC(O)=O PKAUICCNAWQPAU-UHFFFAOYSA-N 0.000 description 1
- HLLSOEKIMZEGFV-UHFFFAOYSA-N 4-(dibutylsulfamoyl)benzoic acid Chemical compound CCCCN(CCCC)S(=O)(=O)C1=CC=C(C(O)=O)C=C1 HLLSOEKIMZEGFV-UHFFFAOYSA-N 0.000 description 1
- WQZGKKKJIJFFOK-QTVWNMPRSA-N D-mannopyranose Chemical compound OC[C@H]1OC(O)[C@@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-QTVWNMPRSA-N 0.000 description 1
- 241001233195 Eucalyptus grandis Species 0.000 description 1
- 241001442228 Eucalyptus grandis x Eucalyptus urophylla Species 0.000 description 1
- 229920001131 Pulp (paper) Polymers 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 125000002777 acetyl group Chemical group [H]C([H])([H])C(*)=O 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229910001860 alkaline earth metal hydroxide Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 239000002738 chelating agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000011121 hardwood Substances 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000004730 pulsed amperometry Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 229920001221 xylan Polymers 0.000 description 1
- 150000004823 xylans Chemical class 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
Description
本発明は、リグノセルロース物質を原料とする燃料の製造法に関する。さらに詳しく述
べれば、リグノセルロース物質を水熱処理してヘミセルロースの大部分を酸加水分解によ
り除去した後、乾燥させることにより、エネルギー密度の高い燃料を製造する方法に関す
る。
The present invention relates to a method for producing a fuel using a lignocellulosic material as a raw material. More specifically, the present invention relates to a method for producing a fuel having a high energy density by hydrothermally treating a lignocellulosic material to remove most of hemicellulose by acid hydrolysis and then drying it.
地球温暖化防止対策を背景に、再生可能なバイオマス由来のエネルギーが注目されている
。バイオマスは、主にリグノセルロース物質からなり、そのまま固体燃料として活用した
り、セルロース、ヘミセルロース、リグニンに分離後、さらにエタノール、ブタノール等
に変換して液体燃料として活用する取り組みが世界中で行なわれている。近年、リグノセ
ルロース物質を半炭化してエネルギー密度の高い固体燃料に変える技術はトレファクショ
ンと呼ばれ、特に注目されている（特許文献１、２）。トレファクションでは、通常、含
水状態にあるリグノセルロース物質を一旦乾燥させ、その後、加熱処理を行い、リグノセ
ルロース物質中で比較的発熱量の低いヘミセルロースを熱分解して除去し、さらに圧密化
して化学的、物理的にエネルギー密度を高めることで、固体燃料としての価値を高める。
トレファクションでは、燃料の軽量化、疎水化も達成され、輸送性、貯蔵性に優れた固体
燃料としての価値も高まることになる。しかしながら、熱分解されたヘミセルロースの活
用法は十分ではなく、製造工程内の補助燃料として使用される程度であった。
Renewable biomass-derived energy has attracted attention against the background of global warming prevention measures. Biomass is mainly composed of lignocellulosic substances and is used as a solid fuel as it is, or after being separated into cellulose, hemicellulose, and lignin, and then converted into ethanol, butanol, etc. and used as a liquid fuel around the world. Yes. In recent years, a technique of semi-carbonizing a lignocellulosic material into a solid fuel having a high energy density is called trefaction and has attracted particular attention (Patent Documents 1 and 2). Usually, the lignocellulosic material that is in a water-containing state is once dried and then subjected to heat treatment to thermally decompose and remove hemicellulose having a relatively low calorific value in the lignocellulosic material. By increasing the energy density physically and physically, the value as a solid fuel is increased.
In the treatment, the weight of the fuel is reduced and the hydrophobicity is achieved, and the value as a solid fuel excellent in transportability and storage is also increased. However, the utilization method of thermally decomposed hemicellulose is not sufficient, and it is only used as an auxiliary fuel in the production process.
リグノセルロース物質中のヘミセルロースは、熱分解だけでなく、酸加水分解でも分解、
除去できることが知られている。ヘミセルロース、例えばキシランを酸加水分解すると、
糖の形を残したまま低分子化され、キシロオリゴ糖、キシロース等として分離、活用する
ことができるという利点がある。また、さらに反応を進めることで、フルフラールに変換
させ、フルフラールとして活用することも可能である。したがって、前記トレファクショ
ンのようにリグノセルロース物質を固体燃料として活用しつつ、ヘミセルロース分解物も
有効利用するのであれば、ヘミセルロースの分解方法は熱分解ではなく、酸加水分解する
のが得策といえる。また、リグノセルロース物質は通常、含水状態にあるので、酸加水分
解では熱分解時のようにわざわざ乾燥させる必要もなく、効率的と考えられる。
Hemicellulose in lignocellulosic material is decomposed not only by thermal decomposition but also by acid hydrolysis.
It is known that it can be removed. When acid hydrolysis of hemicellulose, such as xylan,
There is an advantage that it is reduced in molecular weight while leaving the sugar form, and can be separated and utilized as xylooligosaccharide, xylose and the like. Further, by further proceeding with the reaction, it can be converted into furfural and utilized as furfural. Therefore, if the lignocellulosic material is used as a solid fuel as in the above-described trephination, and the hemicellulose decomposition product is also effectively used, it can be said that the hemicellulose decomposition method is not thermal decomposition but acid hydrolysis. In addition, since the lignocellulosic substance is usually in a water-containing state, it is considered that the acid hydrolysis is efficient because it does not need to be dried as in the case of thermal decomposition.
含水状態のリグノセルロース物質をそのまま、あるいはさらに加水して加熱すれば、ヘミ
セルロース中のアセチル基が脱離して酢酸が生成し、自動的に酸性状態となり、酸加水分
解が進むことが知られている（特許文献３）。水熱処理は、上記のように熱分解に比べて
利点がある反面、水熱処理後のリグノセルロース物質は含水率が高く、固体燃料化する際
の乾燥負荷が高いという欠点も有していた。
It is known that if water-containing lignocellulosic material is heated as it is or after further addition of water, the acetyl group in hemicellulose is eliminated and acetic acid is generated, which automatically becomes acidic and acid hydrolysis proceeds. (Patent Document 3). Hydrothermal treatment has advantages over pyrolysis as described above, but lignocellulosic material after hydrothermal treatment has a high moisture content and has a drawback of high drying load when converted to solid fuel.
本発明は、リグノセルロース物質からヘミセルロースを除去してエネルギー密度の高い固
体燃料を製造するに際し、ヘミセルロースの分解方法を水熱処理による酸加水分解とする
ことで、ヘミセルロース分解物の有効利用を実現し、従来の前記課題を解決するものであ
る。
In the present invention, when producing a solid fuel having a high energy density by removing hemicellulose from a lignocellulosic material, the decomposition method of hemicellulose is acid hydrolysis by hydrothermal treatment, thereby realizing effective utilization of the hemicellulose decomposition product, It solves the conventional problem.
本発明者らは、リグノセルロース物質を水熱処理してヘミセルロースを酸加水分解した
後、脱水、圧縮処理を施し、その後乾燥処理すれば、トレファクション時並の乾燥負荷で
エネルギー密度の高い固体燃料を製造でき、さらにはヘミセルロース分解物としてキシロ
オリゴ糖、キシロース、フルフラール等の有価物も同時に製造できることを見出し、本発
明を完成するに至った。
The present inventors hydrolyzed the lignocellulosic material to hydrolyze hemicellulose, and then subjected to dehydration and compression treatment, followed by drying treatment to produce a solid fuel with a high energy density at the same dry load as in the refracting process. It has been found that valuable materials such as xylooligosaccharides, xylose and furfural can be simultaneously produced as hemicellulose degradation products, and the present invention has been completed.
本願発明は以下の発明を包含する。
（１）リグノセルロース物質を水熱処理し、ついで脱水、圧縮処理し、さらに乾燥処理す
るリグノセルロース物質を原料とする固体燃料の製造方法。
（２） 前記水熱処理時の液比が０．５〜８．０である（１）記載のリグノセルロース物
質を原料とする固体燃料の製造方法。
（３）前記水熱処理時および／または脱水、圧縮処理時に発生するガスからフルフラール
を製造する（１）〜（２）記載のリグノセルロース物質を原料とする固体燃料の製造方法
。
（４）前記水熱処理時および／または脱水、圧縮処理時に発生する液から、各種オリゴ糖
、単糖のうち、少なくとも１つ以上の化合物を製造する（１）〜（３）記載のリグノセル
ロース物質を原料とする固体燃料の製造方法。
The present invention includes the following inventions.
(1) A method for producing a solid fuel using a lignocellulosic material as a raw material, wherein the lignocellulosic material is hydrothermally treated, then dehydrated and compressed, and further dried.
(2) A method for producing a solid fuel using a lignocellulosic material as a raw material according to (1), wherein the liquid ratio during the hydrothermal treatment is 0.5 to 8.0.
(3) A method for producing a solid fuel using a lignocellulosic material as a raw material according to (1) to (2), wherein furfural is produced from the gas generated during the hydrothermal treatment and / or dehydration and compression treatment.
(4) The lignocellulosic material according to any one of (1) to (3), wherein at least one compound of various oligosaccharides and monosaccharides is produced from the liquid generated during the hydrothermal treatment and / or dehydration and compression treatment. A method for producing a solid fuel that uses as a raw material.
本発明者によれば、リグノセルロース物質を水熱処理してヘミセルロースを酸加水分解
し、その後脱水、圧縮処理し、さらに乾燥処理すれば、トレファクションと同様にエネル
ギー密度が高い固形燃料が得られる上に、ヘミセルロース分解物としてキシロオリゴ糖、
キシロース、フルフラール等の有価物を同時に製造できることが可能となった。
According to the present inventor, if the lignocellulosic material is hydrothermally treated to acid-hydrolyze hemicellulose, and then dehydrated and compressed, and further dried, a solid fuel having a high energy density can be obtained as in the case of the torsion. And xylooligosaccharides as hemicellulose degradation products,
It became possible to produce valuable materials such as xylose and furfural simultaneously.
本発明で使用されるリグノセルロース物質は、木材、非木材のいずれでもよいが、ヘミセ
ルロース分解物の利用価値が高いという理由で、広葉樹材が好適である。広葉樹としては
、ユーカリ・グロブラス、ユーカリ・グランディス、ユーカリ・ユーログランディス、ユ
ーカリ・ペリータ、ユーカリ・ブラシアーナ、アカシア・メランシ、アカシア・マンギュ
ーム、アカシア・アウリカルフォルミス等を挙げることができ、原料調達の持続性という
観点からは植林木が好ましく、植林に適したこれらの材が特に好ましいが、限定されるも
のではない。言うまでもなく、と広葉樹、針葉樹、非木材をそれぞれ単独で使用すること
もできるし、組み合わせて使用することもできるし、その組み合わせは限定されるもので
はない。また、樹皮、靱皮部等のどの部位であっても原料として使用できる。
The lignocellulosic material used in the present invention may be either wood or non-wood, but hardwood is preferred because of the high utility value of hemicellulose degradation products. Examples of broad-leaved trees include eucalyptus globulas, eucalyptus grandis, eucalyptus eurograndis, eucalyptus perita, eucalyptus brushana, acacia melanci, acacia mangum, and acacia auricular formis. From the standpoint of sex, afforestation trees are preferred, and these materials suitable for afforestation are particularly preferred, but are not limited. Needless to say, broad-leaved trees, coniferous trees, and non-woods can be used alone or in combination, and the combination is not limited. Moreover, it can be used as a raw material at any site such as a bark or a bast portion.
本発明では、まずリグノセルロース物質を水に浸漬した後、ついで脱水し、リグノセル
ロース物質に付着した異物を除去しながら、リグノセルロース物質の含水率を高める操作
を行なう。浸漬用の装置としては、特に限定されるものではないが、一般のチップウォッ
シャーが好適に用いられる。浸漬用の水としては工場用水、黒液エバポレーターからの回
収水等、特に限定されるものではないが、できる限り無色透明で、蒸留水に近いものが好
ましい。この際に、必要に応じて界面活性剤、キレート剤等の薬剤も添加することができ
る。浸漬後の脱水機としては、特に限定されるものではないが、ドレーナー型の脱水機が
好適に用いられる。浸漬、脱水後のリグノセルロース物質は、少なくとも自重の５０％以
上の水を含む状態になるように、浸漬、脱水条件が加減される。リグノセルロース物質中
の含水率が低すぎると、リグノセルロース物質中の水の存在が不均一となり、次工程の水
熱処理時のヘミセルロースの酸加水分解反応が均一に行なわれないためである。
In the present invention, first, the lignocellulosic material is immersed in water, then dehydrated, and the moisture content of the lignocellulosic material is increased while removing foreign substances adhering to the lignocellulosic material. The dipping apparatus is not particularly limited, but a general chip washer is preferably used. The water for immersion is not particularly limited, such as factory water and water recovered from black liquor evaporator, but is preferably as colorless and transparent as possible and close to distilled water. At this time, agents such as surfactants and chelating agents can be added as necessary. The dehydrator after the immersion is not particularly limited, but a drainer type dehydrator is preferably used. Immersion and dehydration conditions are adjusted so that the lignocellulosic material after immersion and dehydration contains at least 50% of its own weight of water. This is because if the water content in the lignocellulose material is too low, the presence of water in the lignocellulosic material becomes non-uniform, and the acid hydrolysis reaction of hemicellulose during the hydrothermal treatment in the next step is not performed uniformly.
本発明では、次いで水熱処理が行われる。本発明の水熱処理は、含水状態のリグノセルロ
ース物質をそのまま、あるいは加水した後、加温して行なわれる。加温は、通常、蒸気を
直接添加して行なうが、特に限定されるものではなく、場合によっては間接加熱等も実施
可能である。水熱処理時の液比は０．５〜８．０、好ましくは１．０〜４．０、温度は１
４０〜２００℃、好ましくは１５０〜１８０℃、処理時間は処理温度にもよるが、１０分
〜８時間、好ましくは３０分〜５時間である。液比が０．５よりも低い場合には、ヘミセ
ルロースの酸加水分解反応が不均一となるため適さず、８．０よりも高い場合にはその後
の脱水、乾燥処理時の負荷が高くなりすぎる上に、ろ液中のヘミセルロース分解物の濃度
が低くなり、これらを分離、精製し、有効通行活用する際にも大きな負荷が掛かるため適
さない。温度は１４０℃より低い場合には、ヘミセルロースの酸加水分解が不十分となり
、２００℃より高い場合にはセルロースの分解が起こる頻度が高くなるので適さない。処
理時間が１０分より少ない場合には、ヘミセルロースの酸加水分解が不十分となり、８時
間より長い場合には水熱処理用の反応容器が巨大なものとなり、経済的でないので適さな
い。なお、水熱処理時のヘミセルロースの酸加水分解速度を上げる手段として、酢酸、硫
酸、亜硫酸等の酸を添加することも可能であるが、固体燃料としての品質を損なう場合が
あるのでできるだけ酸を添加しないのが好ましい実施形態である。水熱処理で用いる装置
は、特に限定されるものではないが、製紙パルプ製造用の加圧型チップビンや蒸解釜のよ
うな耐圧容器が好適に用いられる。なお、水熱処理時に発生するガスには、ヘミセルロー
スの分解物であるフルフラールが多く含まれることから、このガスを分離し、蒸留処理し
てフルフラールを別途、製造するのも本発明の好ましい実機形態である。
In the present invention, hydrothermal treatment is then performed. The hydrothermal treatment of the present invention is performed by heating the water-containing lignocellulose material as it is or after adding water. Heating is usually performed by directly adding steam, but is not particularly limited, and indirect heating or the like can be performed depending on circumstances. The liquid ratio during hydrothermal treatment is 0.5 to 8.0, preferably 1.0 to 4.0, and the temperature is 1.
40 to 200 ° C., preferably 150 to 180 ° C., and the treatment time depends on the treatment temperature, but is 10 minutes to 8 hours, preferably 30 minutes to 5 hours. If the liquid ratio is lower than 0.5, the acid hydrolysis reaction of hemicellulose becomes non-uniform, which is not suitable. If it is higher than 8.0, the load during the subsequent dehydration and drying process becomes too high. In addition, the concentration of hemicellulose degradation products in the filtrate is lowered, and these are not suitable because they are separated and purified, and a large load is applied when they are used effectively. If the temperature is lower than 140 ° C., acid hydrolysis of hemicellulose is insufficient, and if it is higher than 200 ° C., the frequency of cellulose decomposition is increased, which is not suitable. When the treatment time is less than 10 minutes, acid hydrolysis of hemicellulose is insufficient, and when the treatment time is longer than 8 hours, the reaction vessel for hydrothermal treatment becomes huge, which is not economical and is not suitable. As a means to increase the acid hydrolysis rate of hemicellulose during hydrothermal treatment, it is possible to add acids such as acetic acid, sulfuric acid, and sulfurous acid. However, the quality of the solid fuel may be impaired. It is a preferred embodiment that does not. The apparatus used in the hydrothermal treatment is not particularly limited, but a pressure vessel such as a pressurized chip bin or a digester for producing paper pulp is preferably used. In addition, since the gas generated during hydrothermal treatment contains a large amount of furfural, which is a decomposition product of hemicellulose, it is also a preferable practical form of the present invention that the gas is separated and separately distilled to produce furfural. is there.
本発明では、リグノセルロース物質を水熱処理した後は、脱水、圧縮処理が行なわれる。
本発明では、必要に応じ、脱水、圧縮処理の前に希釈水を添加し、洗浄効果を付与するこ
とも可能である。本発明で使用する装置としては、特に限定されるものではないが、スト
レーナー型の脱水機と圧搾タイプの脱水機の組み合わせがよく、後者の脱水機としては脱
水量、圧力を制御しやすいという理由でプラグスクリュ−型のものが好適に用いられる。
本発明では、前記脱水、圧縮処理時にヘミセルロース分解物が溶出した廃液を分離、活用
できるという特徴がある。分離した廃液は、フラッシュタンクに送ることでガス層と液層
に分けることができ、ガス層に多く含まれるフルフラールは蒸留処理により、比較的簡単
に分離、精製し、製品化できる。一方、液層に多く含まれるヘミセルロース分解物である
、各種オリゴ糖やキシロース、マンノース等の単糖を常法で簡単に分離、製造し、製品化
できる。
In the present invention, after the lignocellulosic material is hydrothermally treated, dehydration and compression are performed.
In the present invention, if necessary, it is possible to add a dilution water before the dehydration and compression treatment to give a cleaning effect. The apparatus used in the present invention is not particularly limited, but a combination of a strainer-type dehydrator and a compression-type dehydrator is good, and the latter dehydrator is easy to control the dehydration amount and pressure. A plug screw type is preferably used.
The present invention is characterized in that the waste liquid from which the hemicellulose decomposition product is eluted during the dehydration and compression processes can be separated and utilized. The separated waste liquid can be separated into a gas layer and a liquid layer by sending it to a flash tank, and furfural contained in a large amount in the gas layer can be separated, purified and commercialized relatively easily by distillation. On the other hand, monosaccharides such as various oligosaccharides, xylose and mannose, which are hemicellulose degradation products contained in a large amount in the liquid layer, can be easily separated, produced and commercialized by conventional methods.
本発明では、前記脱水、圧縮処理した後、乾燥処理が行なわれる。本発明の乾燥処理条件
は、乾燥後の固形燃料の水分が５％以下になる条件であれば特に限定されないが、固形燃
料の熱量向上の観点からは、窒素雰囲気下で実施するのが好ましい。本発明の乾燥処理に
用いられる装置は特に限定されるものではないが、ロータリーキルンタイプのものが乾燥
効率がよく、好適に用いられる。なお、固形燃料の用途によっては、乾燥処理前にペレッ
トのように成型することも可能である。
In the present invention, after the dehydration and compression treatment, the drying treatment is performed. The drying treatment conditions of the present invention are not particularly limited as long as the moisture of the solid fuel after drying is 5% or less, but from the viewpoint of improving the calorific value of the solid fuel, it is preferably carried out in a nitrogen atmosphere. Although the apparatus used for the drying process of this invention is not specifically limited, A rotary kiln type | mold has good drying efficiency, and is used suitably. Depending on the use of the solid fuel, it can be molded like a pellet before the drying treatment.
以下に、実施例及び比較例を挙げて本発明をより具体的に説明するが、もちろん本発明は
これらの実施例に限定されるものではない。特に示さない限り、キシロースの定量、キシ
ロオリゴ糖の定量、フルフラールの定量は以下の方法で行なった。
Hereinafter, the present invention will be described more specifically with reference to examples and comparative examples. However, the present invention is not limited to these examples. Unless otherwise indicated, xylose, xylooligosaccharide, and furfural were quantified by the following methods.
［キシロースの定量］
試料溶液中のキシロースの定量は、ＤＩＯＮＥＸ社製糖分析システム（ＩＣＳ５０００）
を用いた。カラムはＣａｒｂｏ Ｐａｃ ＰＡ−１ （２×２５０ｍｍ）を用い、２０ｍ
Ｍ ＮａＯＨ溶液を溶離液とし、０．２５ｍｌ／ｍｉｎの流速で測定した。なお、検出に
は、パルスアンペロメトリー検出器を用い、キシロース標品を用いて検量線を作成して、
ろ液中のキシロース含有量を求めた。
[Quantification of xylose]
The quantification of xylose in the sample solution was performed by DONEEX's sugar analysis system (ICS5000).
Was used. The column was Carbo Pac PA-1 (2 × 250 mm), 20 m
M NaOH solution was used as an eluent, and measurement was performed at a flow rate of 0.25 ml / min. For detection, use a pulse amperometry detector, create a calibration curve using a xylose standard,
The xylose content in the filtrate was determined.
［キシロオリゴ糖の定量］
試料溶液に最終濃度が４質量％となるように硫酸を添加し、１２０℃で１時間の条件で加
水分解を行った後、キシロースの定量を行なった。この値から加水分解を行う前の試料中
のキシロース含有量を差し引いた値をキシロオリゴ糖の含有量として算出した。
[Quantification of xylooligosaccharides]
Sulfuric acid was added to the sample solution so as to have a final concentration of 4% by mass, hydrolysis was performed at 120 ° C. for 1 hour, and then xylose was quantified. A value obtained by subtracting the xylose content in the sample before hydrolysis from this value was calculated as the xylooligosaccharide content.
［フルフラールの定量］
試料溶液中のフルフラールの定量にはＡｇｉｌｅｎｔ Ｔｅｃｈｎоｌоｇｉｅｓ社製Ｈ
ＰＬＣシステムを用いた。カラムは、Ｂｉｏ−Ｒａｄ社製Ａｍｉｎｅｘ ＨＰＸ８７Ｐ（
７．８×３００ｍｍ）を用い、５ｍＭ硫酸を溶離液とし、１ｍｌ／ｍｉｎの流速で測定し
た。検出にはＵＶ−Ｖｉｓ検出器を用いた。フルフラールの標品を用い、検量線を作成し
て、試料中の含有量を求めた。
[Quantification of furfural]
For the determination of furfural in the sample solution, H manufactured by Agilent Technologies
A PLC system was used. The column was manufactured by Bio-Rad Aminex HPX87P (
7.8 × 300 mm), 5 mM sulfuric acid was used as an eluent, and measurement was performed at a flow rate of 1 ml / min. A UV-Vis detector was used for detection. Using a furfural sample, a calibration curve was prepared to determine the content in the sample.
実施例１
ユーカリ・ペリータ材チップを絶乾重量で３００ｇ採取し、水道水１０リットルに一晩
浸漬した。その後、チップを取り出して４００メッシュの篩に空け、濾別した。この脱水
後のチップを２．５リットル容量のオートクレーブに入れ、７Ｋ蒸気を注入して１６５℃
まで加温し、１６５℃で６０分間、水熱処理した。７Ｋ蒸気に含まれる水分も加えると、
水熱処理時の液比は２．５であった。水熱処理後、オートクレーブのストレーナーを有す
る廃液コックから廃液を抜き出し、フラッシュタンクに送る一方で、処理後のチップは卓
上プレス機（商品名：ｍｉｎｉ ＴＥＳＴ ＰＲＥＳＳ−１０、ＴＯＹＯＳＥＩＫＩ社製
、条件：１ＭＰａ、５秒）で圧搾脱水した。脱水後のチップは、再度２．５リットル容量
のオートクレーブに入れ、オートクレーブ内の空気を窒素ガスで置換した後、電気ヒータ
ーを用いて間接加熱により１６５℃まで加温し、１６５℃で１００分間加熱処理し、固体
燃料化した。この固形燃料の絶乾重量は２５７ｇであり、対チップあたり８５．８％の収
量であった。この固形燃料の熱量は、熱量分析装置（商品名：１０１３−Ｊ、吉田製作所
（株）製）を用いて測定した結果、４７２２ｃａｌ／ｇであった。
Example 1
Eucalyptus / perita material chips (300 g) were collected in an absolutely dry weight and immersed in 10 liters of tap water overnight. Thereafter, the chips were taken out, emptied through a 400 mesh sieve, and filtered. This dehydrated chip was put into a 2.5 liter autoclave, and 7K steam was injected to 165 ° C.
And hydrothermally treated at 165 ° C. for 60 minutes. Add moisture contained in 7K steam,
The liquid ratio during hydrothermal treatment was 2.5. After the hydrothermal treatment, the waste liquid is extracted from a waste liquid cock having an autoclave strainer and sent to a flash tank. S). The dehydrated chip is again placed in a 2.5 liter autoclave, the air in the autoclave is replaced with nitrogen gas, heated to 165 ° C by indirect heating using an electric heater, and heated at 165 ° C for 100 minutes. Processed to solid fuel. The absolute dry weight of this solid fuel was 257 g, and the yield was 85.8% per chip. The amount of heat of the solid fuel was 4722 cal / g as a result of measurement using a calorimeter (trade name: 1013-J, manufactured by Yoshida Seisakusho Co., Ltd.).
フラッシュタンクに送った水熱処理廃液はガス層と液層に分離し、ガス層は６０℃まで冷
却してドレン化した後、フルフラールを定量した。フルフラール量は、対チップ絶乾重量
あたり０．３％であった。一方、スラッシュタンクで分離した液は、卓上プレス機での圧
搾脱液と合わせて回収液とした。回収液中のキシロオリゴ糖量は、対チップ絶乾重量あた
り５．６％、キシロース量は１．８％であった。結表１に結果を示す。
The hydrothermal treatment waste liquid sent to the flash tank was separated into a gas layer and a liquid layer. The gas layer was cooled to 60 ° C. and drained, and then the furfural was quantified. The amount of furfural was 0.3% based on the dry weight of the chip. On the other hand, the liquid separated in the slush tank was used as the recovered liquid together with the squeezed liquid discharged by the desktop press. The amount of xylooligosaccharides in the recovered solution was 5.6% per chip dry weight, and the amount of xylose was 1.8%. Table 1 shows the results.
実施例２
実施例１において、水熱処理条件を６０分から１００分に変更した以外は実施例１と同
様の操作を行なった。表１に結果を示す。
Example 2
In Example 1, the same operation as in Example 1 was performed except that the hydrothermal treatment condition was changed from 60 minutes to 100 minutes. Table 1 shows the results.
実施例３
実施例１において、水熱処理条件を６０分から１８０分に変更した以外は実施例１と同
様の操作を行なった。表１に結果を示す。
Example 3
In Example 1, the same operation as in Example 1 was performed except that the hydrothermal treatment condition was changed from 60 minutes to 180 minutes. Table 1 shows the results.
実施例４
実施例２において、水熱処理時の液比を２．５から０．５に変更し、水熱処理後、脱液
する前に液比２相当の温水（１００℃）を加えて脱液した以外は実施例２と同様の操作を
行なった。表１に結果を示す。
Example 4
In Example 2, the liquid ratio at the time of hydrothermal treatment was changed from 2.5 to 0.5, and after hydrothermal treatment, the liquid was drained by adding warm water (100 ° C.) corresponding to the liquid ratio 2 before liquid removal. The same operation as in Example 2 was performed. Table 1 shows the results.
実施例５
実施例２において、水熱処理時に加水して液比を２．５から８．０に変更した以外は実
施例２と同様の操作を行なった。表１に結果を示す。
Example 5
In Example 2, the same operation as in Example 2 was performed except that the liquid ratio was changed from 2.5 to 8.0 by adding water during hydrothermal treatment. Table 1 shows the results.
実施例６
実施例２において、ユーカリ・ペリータ材チップをユーカリ・グロブラスに変更した以
外は実施例２と同様の操作を行なった。表１に結果を示す。
Example 6
In Example 2, the same operation as in Example 2 was performed except that the eucalyptus / perita material chip was changed to eucalyptus / globula. Table 1 shows the results.
比較例１
ユーカリ・ペリータ材チップを絶乾質量で３００ｇ採取し、送風乾燥機を用いて１０５
℃で一晩、乾燥させた後、２．５リットル容量のオートクレーブに入れ、オートクレーブ
内の空気を窒素ガスで置換した。その後、電気ヒーターを用いて間接加熱により２４０℃
まで加温し、２４０℃で１００分間加熱処理し、固体燃料化した。この固形燃料の絶乾重
量は２４３ｇであり、対チップあたり８１．０％の収量であった。また、固形燃料の熱量
は、熱量分析装置（商品名：１０１３−Ｊ、吉田製作所（株）製）を用いて測定した結果
、５２９０ｃａｌ／ｇであった。表１に結果を示す。
Comparative Example 1
Extract 300g of Eucalyptus and Perita material chips in an absolutely dry mass and use a blow dryer to remove 105g.
After drying overnight at 0 ° C., the mixture was placed in a 2.5 liter autoclave, and the air in the autoclave was replaced with nitrogen gas. Then, 240 ° C by indirect heating using an electric heater
And heated to 240 ° C. for 100 minutes to form a solid fuel. The absolute dry weight of this solid fuel was 243 g, and the yield was 81.0% per chip. Moreover, the calorific value of the solid fuel was 5290 cal / g as a result of measurement using a calorimetric analyzer (trade name: 1013-J, manufactured by Yoshida Seisakusho Co., Ltd.). Table 1 shows the results.
表１の実施例１〜６と比較例１を比較すると明らかなように、リグノセルロース物質を水
熱処理してヘミセルロースを酸加水分解した後、脱水、圧縮処理によりヘミセルロース分
解物を除去、分離し、乾燥処理すれば、従来のトレファクション技術で製造した固体燃料
と遜色のない固体燃料を製造でき、これに加えて、ヘミセルロース分解物からキシロオリ
ゴ糖、キシロース、フルフラールといった有価物も製造できることがわかる。本発明は、
従来のトレファクションでは利用きしれなかったヘミセルロースの分解物を有価物として
有効利用できるところに特長がある。
As is clear when comparing Examples 1 to 6 and Comparative Example 1 in Table 1, the lignocellulose material was hydrothermally treated to hydrolyze hemicellulose, and then the hemicellulose degradation product was removed and separated by dehydration and compression treatment. It can be seen that if the drying treatment is performed, a solid fuel that is inferior to a solid fuel produced by a conventional trefflection technique can be produced, and in addition, valuable materials such as xylooligosaccharides, xylose, and furfural can be produced from hemicellulose decomposition products. The present invention
It is characterized by the fact that hemicellulose degradation products that could not be used in conventional treffection can be effectively used as valuables.
本願発明は以下の発明を包含する。
（１）リグノセルロース物質の含水率を高める操作を行い、を水熱処理し、ついで脱水、圧縮処理し、さらに乾燥処理するリグノセルロース物質を原料とする固体燃料の製造方法。
（２） 前記水熱処理時の液比が０．５〜８．０である（１）記載のリグノセルロース物
質を原料とする固体燃料の製造方法。
（３）前記水熱処理時および／または脱水、圧縮処理時に発生する液から、各種オリゴ糖
、単糖のうち、少なくとも１つ以上の化合物を製造する（１）または（２）に記載のリグノセルロース物質を原料とする固体燃料の製造方法。
本発明者らは、上記の課題を解決するために鋭意検討した結果、糖化発酵工程から得られる残渣を、機械的処理して糖化発酵することで、工程全体に投入するエネルギーを削減でき、エタノール収率も向上することを見いだし、下記発明を完成した。
即ち、上記課題を解決するため、本発明は以下の（１）〜（４）の方法を採用する。
（１） 木質バイオマスを前処理した後、酵素糖化及びエタノール発酵する第一糖化発酵工程と、該工程から得られる残渣をアルカリ処理し機械的処理した後、糖化発酵する第二糖化発酵工程を有することを特徴とする木質バイオマスからのエタノール製造方法。
（２） 木質バイオマスを前処理した後、酵素糖化及びエタノール発酵する第一糖化発酵工程と、該工程から得られる残渣をアルカリ処理し機械的処理した後、第一糖化発酵工程に返送することを特徴とする木質バイオマスからのエタノール製造方法。
（３） 前記残渣処理工程の機械的処理が、磨砕処理であることを特徴とする（１）または（２）に記載のエタノール製造方法。
（４） 前記残渣処理工程のアルカリ処理が、アルカリ金属またはアルカリ土類金属の水酸化物、硫化物、炭酸塩または亜硫酸塩から選択された１種以上の薬品の水溶液に浸漬させるアルカリ処理であることを特徴とする（１）〜（３）のいずれか１項に記載のエタノール製造方法。
The present invention includes the following inventions.
(1) A method for producing a solid fuel using a lignocellulosic material as a raw material, wherein the operation is performed to increase the water content of the lignocellulosic material, followed by hydrothermal treatment, followed by dehydration, compression treatment, and drying treatment.
(2) A method for producing a solid fuel using a lignocellulosic material as a raw material according to (1), wherein the liquid ratio during the hydrothermal treatment is 0.5 to 8.0.
( 3 ) The lignocellulose according to (1) or (2) , wherein at least one compound of various oligosaccharides and monosaccharides is produced from the liquid generated during the hydrothermal treatment and / or dehydration and compression treatment. A method for producing a solid fuel using a substance as a raw material.
As a result of intensive studies to solve the above-mentioned problems, the present inventors can reduce the energy input to the entire process by mechanically treating the residue obtained from the saccharification and fermentation process and performing saccharification and fermentation. The inventors found that the yield was improved and completed the following invention.
That is, in order to solve the above problems, the present invention employs the following methods (1) to (4).
(1) It has a first saccharification and fermentation step in which woody biomass is pretreated, followed by enzymatic saccharification and ethanol fermentation, and a second saccharification and fermentation step in which the residue obtained from the step is subjected to alkali treatment and mechanical treatment, followed by saccharification and fermentation. A method for producing ethanol from woody biomass.
(2) After pre-treating woody biomass, first saccharification and fermentation process in which enzymatic saccharification and ethanol fermentation are performed, and the residue obtained from the process is subjected to alkali treatment and mechanical treatment, and then returned to the first saccharification and fermentation process. A method for producing ethanol from woody biomass.
(3) The method for producing ethanol according to (1) or (2), wherein the mechanical treatment of the residue treatment step is a grinding treatment.
(4) The alkali treatment in the residue treatment step is an alkali treatment in which the residue is immersed in an aqueous solution of one or more chemicals selected from alkali metal or alkaline earth metal hydroxides, sulfides, carbonates or sulfites. The ethanol production method according to any one of ( 1) to (3), wherein:
次いで、濾過装置により固液分離を行い、液体分は、経路（ロ）を経由して減圧蒸留装置からなる蒸留分離工程に送られて生成アルコール留分と蒸留残渣留分とに分離され、生成アルコール留分は経路（ニ）を経由してアルコール貯槽に送られる。
Next, solid- liquid separation is performed by a filtration device, and the liquid component is sent to a distillation separation process consisting of a vacuum distillation device via a path (b) to be separated into a product alcohol fraction and a distillation residue fraction. The alcohol fraction is sent to the alcohol storage tank via the route (d).
本願発明は以下の発明を包含する。
（１）リグノセルロース物質の含水率を高める操作を行い、を水熱処理し、ついで脱水、圧縮処理し、さらに乾燥処理するリグノセルロース物質を原料とする固体燃料の製造方法。
（２） 前記水熱処理時の液比が０．５〜８．０である（１）記載のリグノセルロース物
質を原料とする固体燃料の製造方法。
（３）前記水熱処理時および／または脱水、圧縮処理時に発生する液から、各種オリゴ糖
、単糖のうち、少なくとも１つ以上の化合物を製造する（１）または（２）に記載のリグノセルロース物質を原料とする固体燃料の製造方法。
The present invention includes the following inventions.
(1) A method for producing a solid fuel using a lignocellulosic material as a raw material, wherein the operation is performed to increase the water content of the lignocellulosic material, followed by hydrothermal treatment, followed by dehydration, compression treatment, and drying treatment.
(2) A method for producing a solid fuel using a lignocellulosic material as a raw material according to (1), wherein the liquid ratio during the hydrothermal treatment is 0.5 to 8.0.
( 3 ) The lignocellulose according to (1) or (2) , wherein at least one compound of various oligosaccharides and monosaccharides is produced from the liquid generated during the hydrothermal treatment and / or dehydration and compression treatment. A method for producing a solid fuel using a substance as a raw material.
Claims (4)
を特徴とする、リグノセルロース物質を原料とする固体燃料の製造方法。 A method for producing a solid fuel using a lignocellulosic material as a raw material, wherein the lignocellulosic material is hydrothermally treated, then dehydrated and compressed, and further dried.
ノセルロース物質を原料とする固体燃料の製造方法。 2. The method for producing a solid fuel using a lignocellulosic material as a raw material according to claim 1, wherein the liquid ratio during the hydrothermal treatment is 0.5 to 8.0.
することを特徴とする、請求項１〜２記載のリグノセルロース物質を原料とする固体燃料
の製造方法。 3. The method for producing a solid fuel using a lignocellulosic material as a raw material according to claim 1, wherein furfural is produced from a gas generated during the hydrothermal treatment and / or dehydration and compression treatment.
糖のうち、少なくとも１つ以上の化合物を製造することを特徴とする、請求項１〜３記載
のリグノセルロース物質を原料とする固体燃料の製造方法。 The lignocellulose according to any one of claims 1 to 3, wherein at least one compound of various oligosaccharides and monosaccharides is produced from a liquid generated during the hydrothermal treatment and / or dehydration and compression treatment. A method for producing a solid fuel using a substance as a raw material.
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