JPH0419833B2 - - Google Patents
Info
- Publication number
- JPH0419833B2 JPH0419833B2 JP58172234A JP17223483A JPH0419833B2 JP H0419833 B2 JPH0419833 B2 JP H0419833B2 JP 58172234 A JP58172234 A JP 58172234A JP 17223483 A JP17223483 A JP 17223483A JP H0419833 B2 JPH0419833 B2 JP H0419833B2
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- fermentation
- dioxide gas
- liquefied carbon
- liquefied
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 208
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 104
- 239000001569 carbon dioxide Substances 0.000 claims description 104
- 238000000855 fermentation Methods 0.000 claims description 63
- 230000004151 fermentation Effects 0.000 claims description 63
- 238000000034 method Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 18
- 150000002894 organic compounds Chemical class 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 12
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 90
- 239000007789 gas Substances 0.000 description 60
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 24
- 238000000605 extraction Methods 0.000 description 16
- 238000000926 separation method Methods 0.000 description 15
- 239000000243 solution Substances 0.000 description 15
- 238000010438 heat treatment Methods 0.000 description 14
- 238000001704 evaporation Methods 0.000 description 13
- 230000008020 evaporation Effects 0.000 description 13
- 244000005700 microbiome Species 0.000 description 9
- 239000002028 Biomass Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 238000004821 distillation Methods 0.000 description 7
- 238000002309 gasification Methods 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 150000001298 alcohols Chemical class 0.000 description 5
- 239000001913 cellulose Substances 0.000 description 5
- 229920002678 cellulose Polymers 0.000 description 5
- 239000011550 stock solution Substances 0.000 description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- 241000209094 Oryza Species 0.000 description 4
- 235000007164 Oryza sativa Nutrition 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 229920005610 lignin Polymers 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 235000009566 rice Nutrition 0.000 description 4
- 239000010902 straw Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- -1 for example Chemical compound 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- 239000003112 inhibitor Substances 0.000 description 3
- 239000003949 liquefied natural gas Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 235000000346 sugar Nutrition 0.000 description 3
- 238000009279 wet oxidation reaction Methods 0.000 description 3
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 235000005985 organic acids Nutrition 0.000 description 2
- 238000010298 pulverizing process Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 150000008163 sugars Chemical class 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 230000001476 alcoholic effect Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- KYKAJFCTULSVSH-UHFFFAOYSA-N chloro(fluoro)methane Chemical compound F[C]Cl KYKAJFCTULSVSH-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002255 enzymatic effect Effects 0.000 description 1
- 239000012213 gelatinous substance Substances 0.000 description 1
- 235000011187 glycerol Nutrition 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 235000018102 proteins Nutrition 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 235000002639 sodium chloride Nutrition 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 150000005846 sugar alcohols Polymers 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 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
Description
【発明の詳細な説明】
〔発明の利用分野〕
本発明は、発酵生成物から、価値ある低分子量
有機化合物を抽出する方法又は製造方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method for extracting or producing valuable low molecular weight organic compounds from fermentation products.
従来、発酵法により有価物を製造する場合、そ
の発酵生成物中には、有価物及び水以外に、菌体
とか高分子物質のような種種雑多なものが含まれ
ており、そこから有価物を効率よく取出すことは
非常に困難なことであつた。
Conventionally, when producing valuables by fermentation, the fermented product contains a variety of miscellaneous things such as bacterial cells and polymeric substances in addition to valuables and water, from which valuables are extracted. It was extremely difficult to extract it efficiently.
また、石油のコストアツプと石油資源の有限論
より近年、石油エネルギーの代替エネルギーとし
てバイオマスからのエタノール製造が注目されて
いる。バイオマスからのエタノールはクリーンで
あると共に従来廃棄物として処理されていたオガ
屑、稲わら等から生産されることから石油資源の
乏しい我国のエネルギー対策としても将来的に考
えて極めて有望である。 Furthermore, due to the rising cost of oil and the limited availability of oil resources, the production of ethanol from biomass has attracted attention in recent years as an alternative energy to oil. Ethanol from biomass is clean and can be produced from sawdust, rice straw, etc., which were previously treated as waste, so it is extremely promising as an energy solution for Japan, which is poor in petroleum resources.
オガ屑、稲わらなどのバイオマスからの低級ア
ルコールの製造は材料中のセルロースを酵素糖化
した後で発酵処理するが、材料中のセルロースは
リグニンで包まれたような状態になつており、こ
のリグニンを除去する必要がある。このリグニン
の除去にはオゾンによる分解処理などの方法もあ
るが、より効果的な脱リグニン法の開発が望まれ
ている。 To produce lower alcohols from biomass such as sawdust and rice straw, the cellulose in the material is fermented after enzymatic saccharification, but the cellulose in the material is wrapped in lignin, and this lignin needs to be removed. Although there are methods to remove this lignin, such as decomposition treatment using ozone, it is desired to develop a more effective delignification method.
次に、発酵過程における主問題点は(a)生成物阻
害（アルコールと炭酸ガス）、(b)反応熱にある。
現在、アルコール発酵に使われる酵母はアルコー
ルに対する耐性が小さいため、得られる発酵液の
アルコール濃度は８〜12％程度である。したがつ
て、高濃度アルコール耐性菌の探索が進められて
いる。 Next, the main problems in the fermentation process are (a) product inhibition (alcohol and carbon dioxide) and (b) heat of reaction.
Currently, the yeast used for alcoholic fermentation has low tolerance to alcohol, so the alcohol concentration of the resulting fermented liquid is around 8-12%. Therefore, the search for bacteria resistant to high alcohol concentrations is underway.
また、アルコール発酵は例えばエタノールの場
合、下記に示す反応により進行するとされてお
り、
C6H12O6→2C2H5OH＋2CO2 (2)
エタノールと同モルの炭酸ガスが同時に生成す
る。一部は溶存し、一部はガスとして系外に出
る。炭酸ガスによる酵母機能の低下は周知の通り
である。 Furthermore, in the case of ethanol, for example, alcohol fermentation is said to proceed through the following reaction: C 6 H 12 O 6 →2C 2 H 5 OH + 2CO 2 (2) The same mole of carbon dioxide gas as ethanol is simultaneously produced. Some of it dissolves, and some of it exits the system as a gas. It is well known that yeast function is reduced by carbon dioxide gas.
反応熱は系の温度を上昇し、酵母の性能を低下
させる。アルコール中の雑菌を少なくする意味に
おいても、現在の30℃程度で行つている発酵工程
を45〜50℃に高めても発酵できる微生物を探索す
ることが重要であるとされている。 The heat of reaction increases the temperature of the system and reduces yeast performance. In order to reduce the number of bacteria in alcohol, it is considered important to search for microorganisms that can ferment even if the fermentation process, which is currently carried out at around 30 degrees Celsius, is raised to 45 to 50 degrees Celsius.
そして、濃縮工程では、上述したごとく、発酵
液のアルコール濃度が８〜12％程度であるため、
これを95％、あるいは燃料用としては、99.5％以
上までに濃縮する必要がある。現状では、蒸留法
によつているが、例えば、最新鋭のアルコール蒸
留プラントでも、発酵原液から1galのエタノール
を蒸留するのに、20000Btuのエネルギーを使う。
これは上記全プロセスにおける消費エネルギーの
60〜80％であり、この蒸留に代る濃縮技術の開発
が重要視されている。しかして、アルコールがエ
タノールの場合には、エタノール濃度が95.6％以
上になると水とエタノールとの共沸現象が生じ、
95.6％以上のエタノールを得るためベンゼン共沸
蒸留法などを行い蒸留操作を複雑にしていた。 In the concentration step, as mentioned above, since the alcohol concentration of the fermented liquid is about 8 to 12%,
This needs to be enriched to 95%, or 99.5% or more for fuel use. Currently, it depends on the distillation method, but even in the latest alcohol distillation plant, for example, it takes 20,000 Btu of energy to distill 1 gal of ethanol from the fermentation stock solution.
This is the energy consumption in all the above processes.
60 to 80%, and the development of concentration technology to replace this distillation is important. However, when the alcohol is ethanol, an azeotropic phenomenon between water and ethanol occurs when the ethanol concentration exceeds 95.6%.
In order to obtain more than 95.6% ethanol, benzene azeotropic distillation was used, making the distillation process complicated.
本発明は、前記従来技術の問題点を解決するた
めになされたものであり、その第１の目的は、発
酵生成物から有価物を効率良く抽出するための抽
出溶媒を提供することにある。第２の目的は、該
抽出を発酵と合せて、効率良く有価物を製造する
ための製造方法を提供することにある。
The present invention was made to solve the problems of the prior art, and its first purpose is to provide an extraction solvent for efficiently extracting valuables from fermentation products. The second objective is to provide a production method for efficiently producing valuable substances by combining the extraction with fermentation.
本発明を概説すれば、本発明は、低分子量有機
化合物の製造方法に関する発明であつて、二酸化
炭素の発生を伴う発酵法により低分子量有機化合
物を製造する方法において、二酸化炭素が液化炭
酸ガス又は超臨界炭酸ガスとなる圧力及び温度条
件下で発酵を行い、同発酵槽内でその発酵生成物
から該低分子量有機化合物を、該液化炭酸ガス又
は超臨界炭酸ガスで抽出、濃縮して分離する工程
を包含することを特徴とする。
To summarize the present invention, the present invention relates to a method for producing a low-molecular-weight organic compound. Fermentation is carried out under pressure and temperature conditions that produce supercritical carbon dioxide gas, and the low molecular weight organic compound is extracted and concentrated from the fermentation product in the same fermenter using the liquefied carbon dioxide gas or supercritical carbon dioxide gas to separate it. It is characterized by including a process.
まず、本発明で使用可能な液化ガスの例として
は、メタン、エタン、エチレン、アンモニア、フ
ロンの液化ガス、液化炭酸ガス、超臨界の炭酸ガ
ス若しくはエタンガス等があるが、無害性、可燃
性、腐食性及び化学的安定性の観点からは、液化
炭酸ガス及び超臨界すなわち臨界温度以上、かつ
臨界圧力以上の状態にある炭酸ガスが最適なもの
である。したがつて、以下の説明を、これら炭酸
ガスを例にして説明する。 First, examples of liquefied gas that can be used in the present invention include methane, ethane, ethylene, ammonia, liquefied chlorofluorocarbon gas, liquefied carbon dioxide, supercritical carbon dioxide, or ethane gas, but they are harmless, flammable, From the viewpoint of corrosivity and chemical stability, liquefied carbon dioxide gas and supercritical carbon dioxide gas, that is, carbon dioxide gas in a state of at least the critical temperature and at least the critical pressure, are optimal. Therefore, the following explanation will be made using these carbon dioxide gases as an example.
また、本発明の目的物である低分子量有機化合
物としては、分子量が150程度までの、アルコー
ル、例えばエタノール、ブタノール、また２，３
−ブチレングリコール及びグリセリンのような多
価アルコール、ケトン例えばアセトン、アルデヒ
ド例えばアセトアルデヒドがある。その他糖類、
有機酸等もあるが、液化炭酸ガス及び超臨界炭酸
ガス中には、糖類、有機酸、たん白質、塩類等で
は不溶性であるので不適当である。 In addition, the low molecular weight organic compounds which are the objects of the present invention include alcohols with a molecular weight of up to about 150, such as ethanol, butanol, and 2,3
- polyhydric alcohols such as butylene glycol and glycerin, ketones such as acetone, aldehydes such as acetaldehyde. Other sugars,
Although organic acids and the like are also available, sugars, organic acids, proteins, salts, etc. are insoluble in liquefied carbon dioxide gas and supercritical carbon dioxide gas, so they are not suitable.
本発明で使用する液化炭酸ガスと水との相互溶
解性は非常に小さく、かつ密度も異なるため、発
酵生成液との分離が容易である。また、酵素及び
微生物は液化炭酸ガス中に不溶性であり、分離
（沈降）が可能である点でも、該抽出溶媒は有用
なものである。更に抽出物との沸点差が大である
点でも有利である。 Since the mutual solubility of the liquefied carbon dioxide used in the present invention and water is very low and their densities are also different, it is easy to separate them from the fermentation product liquid. The extraction solvent is also useful in that enzymes and microorganisms are insoluble in liquefied carbon dioxide and can be separated (sedimented). It is also advantageous in that it has a large boiling point difference with the extract.
本発明の抽出装置は、前記のように、その必須
の設備として、混合器、分離槽、蒸発槽、熱交換
器、循環ポンプ及びそれらの連結機器を包含す
る。 As described above, the extraction apparatus of the present invention includes, as its essential equipment, a mixer, a separation tank, an evaporation tank, a heat exchanger, a circulation pump, and their connecting equipment.
それ故、本発明の抽出装置には、所望により他
の設備を付加してもよい。例えば、該分離槽から
流出する高圧液を利用して水タービンを回転さ
せ、その動力によつて該循環ポンプを駆動させる
設備を包含させてもよい。 Therefore, other equipment may be added to the extraction apparatus of the present invention as desired. For example, a facility may be included in which a water turbine is rotated using the high pressure liquid flowing out from the separation tank, and the circulating pump is driven by the power generated by the water turbine.
なお、上記タービンの動力を昇圧ポンプに伝達
する方式として、タービンとポンプに直結せるプ
ロペラシヤフト、又はタービンで発生した動力を
発電機で電力に変換後、その電力をポンプに接続
する電動機に供給してポンプを回転させる方法等
があり、動力の伝達方法は特定の方法に限定され
ない。 The power of the turbine can be transmitted to the boost pump by a propeller shaft that is directly connected to the turbine and the pump, or by converting the power generated by the turbine into electricity with a generator and then supplying that electricity to the electric motor connected to the pump. The power transmission method is not limited to a specific method.
前記したように、本発明の抽出装置は、発酵生
成物からエタノールを液化炭酸ガスで抽出する場
合に使用するのが特に好ましい。 As described above, the extraction apparatus of the present invention is particularly preferably used when ethanol is extracted from a fermentation product using liquefied carbon dioxide gas.
バイオマスからの低級アルコールの製造プロセ
スは、一般に(1)原料→(2)前処理→(3)糖化→(4)発酵
→(5)濃縮→(6)製品の各工程からなる。 The process for producing lower alcohols from biomass generally consists of the following steps: (1) raw materials → (2) pretreatment → (3) saccharification → (4) fermentation → (5) concentration → (6) product.
低級アルコール、例えばエタノール又はブタノ
ール、特にエタノールの製造装置は、前記概説し
たように、前述した抽出装置と、脱リグニン処理
槽とを結合した点に特徴がある。 The apparatus for producing lower alcohols, such as ethanol or butanol, particularly ethanol, is characterized in that, as outlined above, the above-mentioned extraction apparatus and delignification treatment tank are combined.
本発明の製造装置では、抽出溶媒がある液化ガ
スを蒸発槽でガス化し、それを再び液化するのに
液化燃料ガスの気化熱を利用している。そして気
化した燃料ガスを燃料として300℃前後の水蒸気
を発生させ、それを用いて湿式酸化法により脱リ
グニン処理を行うものである。この水蒸気の源と
なる水は、任意の仕方で準備してよい。例えば該
蒸発槽に内蔵させた加熱部、該加熱部に水を流過
させ、その水を該燃焼器に導入して水蒸気を発生
させる手段の各設備を包含させてよく、本発明の
装置では、それが好適である。 In the production apparatus of the present invention, the liquefied gas containing the extraction solvent is gasified in the evaporation tank, and the heat of vaporization of the liquefied fuel gas is used to liquefy it again. The vaporized fuel gas is then used as fuel to generate water vapor at around 300°C, which is used to perform delignification treatment using a wet oxidation method. The water source of this steam may be prepared in any manner. For example, the apparatus of the present invention may include a heating section built into the evaporation tank and means for causing water to flow through the heating section and introducing the water into the combustor to generate steam. , which is preferred.
液化燃料ガスの例としては、LNG及びLPGが
ある。 Examples of liquefied fuel gases include LNG and LPG.
本発明の要点は、前記概説したように、発酵
と、その目的有価物である低分子量有機化合物の
発酵生成物からの液化炭酸ガス又は超臨界炭酸ガ
スによる抽出を、同一設備内で並行して行う点に
ある。したがつて、目的とする低分子量有機化合
物は、該液化炭酸ガス又は超臨界炭酸ガス中に溶
解するものでなければならない。 The main point of the present invention is that, as outlined above, fermentation and extraction of the target valuable product, a low molecular weight organic compound, from the fermentation product using liquefied carbon dioxide gas or supercritical carbon dioxide gas can be carried out in parallel in the same equipment. It is in the point of doing. Therefore, the target low molecular weight organic compound must be soluble in the liquefied carbon dioxide gas or supercritical carbon dioxide gas.
そこで、既述の発酵過程における問題点につい
てみると、まず(a)の生成物阻害に関して、最も簡
単な解決方法は、生成した阻害物例えばアルコー
ルを系外に取出し、該阻害物濃度が増加しないよ
うにすればよい。これにより運転の連続化が可能
となり、微生物の機能を最大限に発揮できる。本
発明によれば、阻害物は液化炭酸ガス又は超臨界
炭酸ガス中に溶解することにより系外に取出され
る。次に、(b)の反応熱に関して、炭酸ガスは、発
酵過程で生成し、かつ常温、高圧下で液化するこ
とができる。したがつて、常温付近で発酵を行う
ことができるため、微生物機能に及ぼす影響は極
めて小である。更に圧力に関しては、一般に、微
生物の発酵機能に及ぼす圧力の影響は、その反応
系がガスの授受を伴わない限り、少ないと考えら
れている。本発明による発酵過程では炭酸ガスが
生成するので、この濃度が高くなると発酵反応は
進行しなくなる。そこで、液化炭酸ガスの水に対
する溶解性が問題となる。そのため、本発明者等
は、水と液化炭酸ガスとの相互溶解性について測
定した。SUSパイプ（内径10.8mm、長さ400mm）
を用い、21℃、57atgで測定を行つた。その結果、
液化炭酸ガスに対する水の溶解度（水のｇ／液化
炭酸ガスのｇ）は、0.0013であつた。他方、水に
対する液化炭酸ガスの溶解度（液化炭酸ガスの
ｇ／水のｇ）は、0.00077であつた。この0.00077
なる値は、大気圧、25℃における炭酸ガスの溶解
度0.001446のほぼ1/2程度で極めて小さい。また
流動層方式のアルコール発酵プラントにおいて、
バイオリアクターで生成する炭酸ガスを槽内かく
はんのために循環使用しているので、高圧化の影
響は小と推定される。 Therefore, looking at the problems in the fermentation process mentioned above, first of all, regarding (a) product inhibition, the simplest solution is to remove the generated inhibitors, such as alcohol, from the system and prevent the concentration of the inhibitors from increasing. Just do it like this. This enables continuous operation and maximizes the functionality of microorganisms. According to the present invention, the inhibitors are removed from the system by dissolving them in liquefied carbon dioxide or supercritical carbon dioxide. Next, regarding the heat of reaction (b), carbon dioxide gas is generated during the fermentation process and can be liquefied at room temperature and under high pressure. Therefore, since fermentation can be carried out at around room temperature, the effect on microbial functions is extremely small. Furthermore, regarding pressure, it is generally believed that the influence of pressure on the fermentation function of microorganisms is small unless the reaction system involves exchange of gas. Since carbon dioxide gas is generated in the fermentation process according to the present invention, when the concentration of carbon dioxide gas becomes high, the fermentation reaction will not proceed. Therefore, the solubility of liquefied carbon dioxide gas in water becomes a problem. Therefore, the present inventors measured the mutual solubility of water and liquefied carbon dioxide. SUS pipe (inner diameter 10.8mm, length 400mm)
Measurements were carried out at 21°C and 57atg using the result,
The solubility of water in liquefied carbon dioxide (g of water/g of liquefied carbon dioxide) was 0.0013. On the other hand, the solubility of liquefied carbon dioxide in water (g of liquefied carbon dioxide/g of water) was 0.00077. This 0.00077
This value is extremely small, approximately 1/2 of the solubility of carbon dioxide, 0.001446, at atmospheric pressure and 25°C. In addition, in a fluidized bed alcohol fermentation plant,
Since the carbon dioxide gas produced in the bioreactor is recycled for stirring inside the tank, the impact of high pressure is estimated to be small.
更に、上記値0.0013は極めて小さいので、目的
生成物を高濃度で得ることができる。 Furthermore, since the above value of 0.0013 is extremely small, the desired product can be obtained in high concentration.
本発明においては、生成する二酸化炭素のみで
抽出を行つてもよいが、液化炭酸ガス又は超臨界
炭酸ガスを添加して発酵を行つてもよい。更に、
該分離した低分子量有機化合物を含有する液か
ら、該液化炭酸ガス又は超臨界炭酸ガスをガス化
して分離する工程を包含していてもよい。この分
離工程は沸点差が大きいため容易である。 In the present invention, extraction may be performed using only the carbon dioxide produced, but fermentation may also be performed with the addition of liquefied carbon dioxide or supercritical carbon dioxide. Furthermore,
The method may include a step of gasifying and separating the liquefied carbon dioxide or supercritical carbon dioxide from the separated liquid containing the low molecular weight organic compound. This separation step is easy due to the large difference in boiling points.
以下、本発明を実施例により具体的に説明する
が、本発明はこれら実施例に限定されない。
EXAMPLES Hereinafter, the present invention will be specifically explained with reference to Examples, but the present invention is not limited to these Examples.
なお、添付図面において、第１図は、本発明の
抽出装置の１例の系統図、第２図は、本発明の低
級アルコール製造装置の１例の系統図、第３図及
び第４図は、本発明によるエタノール製造方法の
１例の工程図である。 In the accompanying drawings, FIG. 1 is a system diagram of an example of the extraction device of the present invention, FIG. 2 is a system diagram of an example of the lower alcohol production device of the present invention, and FIGS. , is a process diagram of an example of the ethanol production method according to the present invention.
実施例 １
第１図に示した本発明の抽出装置の１例におい
て、符号２はポンプ、４は混合器、７は分離層、
８は発酵生成液と、目的物を含有する液化炭酸ガ
ス液との境界面、１０はバルブ、１１は蒸発槽、
１２は加熱部材、１３は目的物液、１５はバル
ブ、１７は熱交換器、１９はポンプ、２１はバル
ブ、２３は水タービン、その他は管路を意味す
る。Example 1 In one example of the extraction apparatus of the present invention shown in FIG. 1, 2 is a pump, 4 is a mixer, 7 is a separation layer,
8 is an interface between the fermentation product liquid and the liquefied carbon dioxide liquid containing the target product, 10 is a valve, 11 is an evaporation tank,
12 is a heating member, 13 is a target liquid, 15 is a valve, 17 is a heat exchanger, 19 is a pump, 21 is a valve, 23 is a water turbine, and the others are pipes.
第１図について説明すると、発酵生成物溶液が
管路１から入り、ポンプ２により加圧されて管路
３を経て、混合器４に入る。ここで、溶液は管路
５から流入してくる液化炭酸ガスと混合し、管路
６を通つて分離槽７に流入する。溶液及び液化炭
酸ガスが分離槽７に移動する間に混合器及び管６
内で溶液中の有価物質が液化炭酸ガス中に移行す
る。分離槽７ではある程度の滞留時間をもたせる
ようにすることにより、溶液と液化炭酸ガスとの
比重差により、有価物質を含まない溶液と、それ
を含有せる液化炭酸ガスとに分離する。分離槽内
の８は両液の境界面を示す。水などのように液化
炭酸ガスの比重より大きな溶液では溶液は下部
に、他方液化炭酸ガスは上部になる。分離した液
化炭酸ガスは管路９を通り、バルブ１０によつて
減圧されて蒸発槽１１に流入する。蒸発槽内には
加熱部材１２があり、バルブ１０による減圧と加
熱部材による加熱により、液化炭酸ガスは気化
し、液化炭酸ガス中に溶解していた有価物１３は
蒸発槽の下部に液状となつて分離される。この有
価物１３は管路１４、バルブ１５を経て系外に出
る。有価物は製品として使用される。他方、蒸発
槽で気化した炭酸ガスは管路１６を通り、熱交換
器１７に流入し、ここで冷やされて液化炭酸ガス
となつて管路１８、ポンプ１９、管路２０、バル
ブ２１を経て、管路５から混合器４に流入する。 Referring to FIG. 1, the fermentation product solution enters through line 1, is pressurized by pump 2, passes through line 3, and enters mixer 4. Here, the solution mixes with the liquefied carbon dioxide gas flowing in from the pipe 5 and flows into the separation tank 7 through the pipe 6. While the solution and liquefied carbon dioxide are transferred to the separation tank 7, the mixer and tube 6
Valuable substances in the solution migrate into liquefied carbon dioxide gas. By allowing a certain amount of residence time in the separation tank 7, the solution and liquefied carbon dioxide are separated into a solution that does not contain valuable substances and a liquefied carbon dioxide that contains them, due to the difference in specific gravity between the solution and the liquefied carbon dioxide. 8 in the separation tank indicates the interface between both liquids. In a solution such as water that has a specific gravity greater than that of liquefied carbon dioxide, the solution will be at the bottom, while liquefied carbon dioxide will be at the top. The separated liquefied carbon dioxide gas passes through a pipe 9, is depressurized by a valve 10, and flows into an evaporation tank 11. There is a heating member 12 in the evaporation tank, and by reducing the pressure with the valve 10 and heating with the heating member, the liquefied carbon dioxide is vaporized, and the valuables 13 dissolved in the liquefied carbon dioxide become liquefied at the bottom of the evaporation tank. separated. This valuable material 13 exits the system through a pipe 14 and a valve 15. Valuables are used as products. On the other hand, the carbon dioxide vaporized in the evaporator passes through the pipe 16 and flows into the heat exchanger 17, where it is cooled and becomes liquefied carbon dioxide, which passes through the pipe 18, pump 19, pipe 20, and valve 21. , flows into the mixer 4 from the conduit 5.
また、分離槽で有価物質を除去した高圧の液は
管路２２を通り、水タービン２３に入り、ここで
タービンを回転させた後に管路２４を経て系外に
出る。タービン２３での動力はポンプ１９を回転
させる動力となる。更に、蒸発槽内に装着せる加
熱部材１２には管路２５より水道水などの加熱媒
体が流入し、加熱部材１２を流通する間に管路９
より流出せる液化炭酸ガスと熱交換して温度が下
がり、管路２６より流出する。熱交換器１７には
管路２７より冷却水が流入し、ここで炭酸ガスと
間接的に熱交換し、炭酸ガスを液化させて管路２
８より流出する。管路２７からの冷却水は管路２
８から流出するときは炭酸ガスの液化熱量に相当
する温度上昇となつて流出する。 Further, the high-pressure liquid from which valuable substances have been removed in the separation tank passes through a pipe 22 and enters a water turbine 23, where it rotates the turbine and then exits the system through a pipe 24. The power from the turbine 23 becomes the power for rotating the pump 19. Further, a heating medium such as tap water flows into the heating member 12 installed in the evaporation tank through the pipe 25, and while flowing through the heating member 12, the heating medium flows through the pipe 9.
It exchanges heat with the liquefied carbon dioxide gas that can flow out more, lowers its temperature, and flows out from the pipe 26. Cooling water flows into the heat exchanger 17 from the pipe line 27, where it indirectly exchanges heat with carbon dioxide gas, liquefies the carbon dioxide gas, and supplies it to the pipe line 2.
It flows out from 8. Cooling water from pipe 27 is transferred to pipe 2
When it flows out from 8, it flows out with a temperature rise corresponding to the liquefaction heat amount of carbon dioxide gas.
なお、溶液の比重が液化炭酸ガスの比重より小
さい場合は分離槽内の境界面８より上部は溶液
で、下部は液化炭酸ガス相であり、その際には管
路９は液化炭酸ガス相に設けられ、管路２２は境
界面８より上部に設ける必要がある。 In addition, when the specific gravity of the solution is smaller than the specific gravity of liquefied carbon dioxide gas, the upper part of the boundary surface 8 in the separation tank is the solution, and the lower part is the liquefied carbon dioxide phase, and in this case, the pipe 9 is in the liquefied carbon dioxide phase. The conduit 22 must be provided above the interface 8.
実施例 ２
第２図に、バイオマスからのエタノール製造装
置を例示する。第２図において、符号２，４，
５，７，８，１０〜１４，１６〜１９，２３〜２
６は第１図と同義であり、３１はバイオマス材
料、３２は粉砕機、３３は脱リグニン処理槽、３
４は糖化発酵槽、３７は燃焼器、３９は伝熱管、
その他は管路を意味する。Example 2 FIG. 2 illustrates an apparatus for producing ethanol from biomass. In FIG. 2, symbols 2, 4,
5, 7, 8, 10-14, 16-19, 23-2
6 has the same meaning as in FIG. 1, 31 is a biomass material, 32 is a crusher, 33 is a delignification treatment tank, 3
4 is a saccharification fermenter, 37 is a combustor, 39 is a heat exchanger tube,
Others mean conduits.
３１はオガ屑、稲わら等のセルロース系バイオ
マス材料で、３２は稲わら等のごとく粉砕を要す
る材料に対して行う粉砕工程であり、３３は脱リ
グニンを行う湿式酸化プロセスである。ここでセ
ルロースの糖化分解を阻害するリグニンを除去す
る。３４は糖化発酵プロセスでここでセルロース
が酵素の働きによつて糖化し、更に糖からエタノ
ールに変る。ここでのエタノールの濃度は発酵工
学的な特性から10％程度である。約10％濃度のエ
タノール溶液はポンプ２によつて昇圧され、混合
器４に入る。ここで循環ポンプ１９によつて圧入
されてきた液化炭酸ガスと接触し、エタノール成
分は液化炭酸ガス中に移行し、分離槽７で液化炭
酸ガスとエタノールを含有しない液とに分離す
る。分離槽７内の線８は液化炭酸ガスとエタノー
ルを含まない液との境界線を示すもので、上部は
液化炭酸ガス相である。分離槽７からバルブ１０
を通つて蒸発槽１１に入つた液化炭酸ガスはバル
ブ１０による減圧と蒸発槽１１に内蔵せる加熱部
材１２によつて熱を与えられて気化し、液化炭酸
ガスはガスとなり、液化炭酸ガス中に溶け込んで
いたエタノール１３は液体のまま気化した炭酸ガ
スと分離する。この分離したエタノールは、管路
１４を経て系外に出て製品となる。なお、このエ
タノールは約99％の高純度であり、直ちに製品と
して使用される。気化した炭酸ガスは管路１６を
通り、熱交換器１７に入り、ここで管路３５から
供給されるLNG（液化天然ガス）によつて冷やさ
れて液化し、管路１８、ポンプ１９、管路５を通
つて混合器４に入る。熱交換器１７で気化した天
然ガスは管路３６から燃焼器３７に入り、ここで
は管路３８からの空気と混合して燃焼し、燃焼器
に内蔵した伝熱管３９内を流れる水を加熱し、水
蒸気とする。この水蒸気は管路４０を経て湿式酸
化工程３３に供給される。他方燃焼室で伝熱管３
９に熱を奪われた燃焼後のガスは管路４１より系
外に排出される。蒸発槽１１に内蔵された加熱部
材１２には管路２５より加熱源となる水道水が供
給され、管路２６より流出し、熱交換器３７に入
る。炭酸ガスの性質から蒸発槽内のガス温度は約
10℃であり、圧力は約42atm程度である。また、
分離槽で液化炭酸ガスと分離した高圧（約45〜
50atm）の液は水タービン２３で動力を発生させ
た後、管路２４を経て系外に流出する。水タービ
ン２３で発生した動力はポンプ１９の動力源とし
て利用される。 31 is a cellulosic biomass material such as sawdust or rice straw, 32 is a pulverization process performed on a material that requires pulverization such as rice straw, and 33 is a wet oxidation process for delignification. Here, lignin, which inhibits the saccharification and decomposition of cellulose, is removed. 34 is a saccharification and fermentation process in which cellulose is saccharified by the action of enzymes, and the sugar is further converted to ethanol. The concentration of ethanol here is about 10% due to fermentation engineering characteristics. The approximately 10% concentration ethanol solution is pressurized by pump 2 and enters mixer 4 . Here, the ethanol component comes into contact with the liquefied carbon dioxide gas forced in by the circulation pump 19, and moves into the liquefied carbon dioxide gas, and is separated into the liquefied carbon dioxide gas and a liquid not containing ethanol in the separation tank 7. A line 8 in the separation tank 7 indicates a boundary line between liquefied carbon dioxide gas and a liquid not containing ethanol, and the upper part is a liquefied carbon dioxide phase. Separation tank 7 to valve 10
The liquefied carbon dioxide gas that has entered the evaporation tank 11 through the evaporation tank 11 is depressurized by the valve 10 and heated by the heating member 12 built into the evaporation tank 11, and is vaporized, and the liquefied carbon dioxide gas becomes gas. The dissolved ethanol 13 remains liquid and separates from the vaporized carbon dioxide gas. This separated ethanol exits the system through the pipe 14 and becomes a product. This ethanol has a high purity of approximately 99% and can be used immediately as a product. The vaporized carbon dioxide passes through the pipe 16 and enters the heat exchanger 17, where it is cooled and liquefied by LNG (liquefied natural gas) supplied from the pipe 35, and then flows through the pipe 18, the pump 19, and the pipe. It enters mixer 4 through channel 5. The natural gas vaporized in the heat exchanger 17 enters the combustor 37 through the pipe 36, where it is mixed with air from the pipe 38 and combusted, thereby heating the water flowing through the heat transfer pipe 39 built into the combustor. , water vapor. This water vapor is supplied to the wet oxidation process 33 via a pipe 40. Heat transfer tube 3 in the other combustion chamber
The combusted gas, which has had its heat removed by 9, is discharged to the outside of the system through a pipe 41. Tap water, which serves as a heating source, is supplied from a pipe line 25 to a heating member 12 built in the evaporation tank 11, flows out from a pipe line 26, and enters a heat exchanger 37. Due to the nature of carbon dioxide gas, the gas temperature inside the evaporator is approximately
The temperature is 10°C and the pressure is about 42 atm. Also,
High pressure (approximately 45 ~
After the liquid (50 atm) generates power in the water turbine 23, it flows out of the system through the pipe 24. The power generated by the water turbine 23 is used as a power source for the pump 19.
実施例 ３
第３図に、本発明の１実施例であるエタノール
の発酵、抽出プロセスの工程を図示する。本実施
例のプロセスは、原液貯槽５１、原液供給ポンプ
５２、発酵液循環ポンプ５３、発酵タンク５４、
液化炭酸ガスのガス化タンク５５及び凝縮器５６
等からなる。糖質系、デンプン系、セルロース系
原料より得られる発酵原液はポンプ５２により、
連続的に発酵タンク５４に供給される。発酵タン
クは固定化微生物５４′を充てんした形式を例に
示したが、これに限るものではない。発酵タンク
５４は例えば常温、70気圧程度に調整され、上記
発酵原液は発酵タンク５４上部より導入され、充
てん層５４′を通過時に、エタノール発酵が行わ
れ、エタノールと炭酸ガスが生成する。この際、
炭酸ガスは液化する。エタノールと炭酸ガスの生
成は同じポイントで起るため、エタノールの液化
炭酸ガスへの溶解は効率良く行い得る。液化炭酸
ガスの密度は約0.8、発酵液の密度は10％エタノ
ール水溶液と考えれば0.98であるため、生成した
液化炭酸ガスはエタノールを溶解しながら上昇す
る。他方、発酵液は下降する。発酵が一過で不十
分である場合には、発酵液の一部あるいは全部を
ポンプ５３により循環する。発酵タンク５４上部
にたまつた液化炭酸ガスは、液化炭酸ガスのガス
化タンク５５に移送され、ここで加温されて、ガ
ス化する。液化炭酸ガス中に溶解していたエタノ
ールは液化炭酸ガスのガス化タンク５５下部にた
まり、これより取出される。他方、炭酸ガスは凝
縮器５６に移送され、適当な温度の液化炭酸ガス
とし、必要に応じて、その一部あるいは全部が発
酵タンク５４下部より導入される。これは、生成
液化炭酸ガスにより溶解しきれなかつたエタノー
ルを溶解するためと、反応熱による昇温を防止
し、発酵タンク内温度を所定値に保つためであ
る。Example 3 FIG. 3 illustrates the steps of an ethanol fermentation and extraction process according to an example of the present invention. The process of this embodiment includes a stock solution storage tank 51, a stock solution supply pump 52, a fermentation solution circulation pump 53, a fermentation tank 54,
Liquefied carbon dioxide gasification tank 55 and condenser 56
Consists of etc. The fermentation stock solution obtained from carbohydrate-based, starch-based, and cellulose-based raw materials is pumped by a pump 52.
It is continuously supplied to the fermentation tank 54. Although a fermentation tank filled with immobilized microorganisms 54' is shown as an example, the present invention is not limited to this. The fermentation tank 54 is adjusted to, for example, room temperature and about 70 atmospheres, and the fermentation stock solution is introduced from the upper part of the fermentation tank 54, and when it passes through the packed layer 54', ethanol fermentation is performed to produce ethanol and carbon dioxide gas. On this occasion,
Carbon dioxide gas liquefies. Since ethanol and carbon dioxide gas are generated at the same point, ethanol can be efficiently dissolved into liquefied carbon dioxide gas. The density of liquefied carbon dioxide gas is approximately 0.8, and the density of the fermentation liquid is 0.98 when considered as a 10% ethanol aqueous solution, so the liquefied carbon dioxide gas produced rises while dissolving ethanol. On the other hand, the fermentation liquid descends. If the fermentation is temporary and insufficient, part or all of the fermentation liquid is circulated by the pump 53. The liquefied carbon dioxide gas accumulated in the upper part of the fermentation tank 54 is transferred to a liquefied carbon dioxide gasification tank 55, where it is heated and gasified. The ethanol dissolved in the liquefied carbon dioxide gas accumulates at the bottom of the liquefied carbon dioxide gasification tank 55 and is taken out from there. On the other hand, the carbon dioxide gas is transferred to the condenser 56 and turned into liquefied carbon dioxide gas at an appropriate temperature, and part or all of it is introduced from the lower part of the fermentation tank 54 as required. This is to dissolve undissolved ethanol with the produced liquefied carbon dioxide gas, and to prevent temperature rise due to reaction heat and maintain the temperature inside the fermentation tank at a predetermined value.
なお、固定化微生物は、ゼラチン状の物質に微
生物を固定したものであるため、上記、発酵タン
ク５４内への充てん率を増大できる。 In addition, since the immobilized microorganisms are microorganisms immobilized on a gelatinous substance, the filling rate into the fermentation tank 54 can be increased.
以上、固定化微生物を発酵タンク内に充てんす
る方式について述べてきたが、発酵タンク内で通
常の流動層方式で発酵を行わせても良いことは言
うまでもない。 Although the method of filling the fermentation tank with immobilized microorganisms has been described above, it goes without saying that fermentation may be carried out in the fermentation tank using a normal fluidized bed method.
実施例 ４
実施例３における液化炭酸ガスの代りに超臨界
炭酸ガスを使用してエタノール発酵を行つた。Example 4 Ethanol fermentation was carried out using supercritical carbon dioxide instead of liquefied carbon dioxide in Example 3.
第４図にその工程図を示す。第４図において、
５１〜５４′は第３図と同義であり、５７は超臨
界炭酸ガスのガス化タンク、５８は圧縮機、５９
は温度調整器を意味する。 Figure 4 shows the process diagram. In Figure 4,
51 to 54' have the same meaning as in FIG. 3, 57 is a supercritical carbon dioxide gasification tank, 58 is a compressor, and 59
means temperature regulator.
本例において、発酵タンク５４は、常温、73気
圧程度に調整した。また、超臨界炭酸ガスの密度
は、操作圧力及び温度により異なるが、いずれに
しても10％エタノール水溶液の密度より小さいの
で、液化炭酸ガスの場合と同じく５４の上方より
取出しうる。そして、ガス化タンク５７で減圧さ
れてガス化する。ガス化した炭酸ガスは圧縮機５
８に移送され、次に温度調整器５９で、適当な温
度の超臨界炭酸ガスとする。他の工程は実施例３
と同様である。 In this example, the fermentation tank 54 was adjusted to room temperature and approximately 73 atmospheres. Further, the density of supercritical carbon dioxide varies depending on the operating pressure and temperature, but in any case, it is lower than the density of a 10% ethanol aqueous solution, so it can be taken out from above 54 as in the case of liquefied carbon dioxide. Then, the pressure is reduced in a gasification tank 57 and the gas is gasified. The gasified carbon dioxide is transferred to the compressor 5.
8, and then in a temperature regulator 59 to make supercritical carbon dioxide gas at an appropriate temperature. Other steps are Example 3
It is similar to
以上詳細に説明したように、本発明によれば、
発酵生成物から効率良く低分子量化合物を抽出す
ることができる。そして、それを特にエタノール
の発酵法による製造に適用すれば、従来ほとんど
蒸留に必要としたエネルギーを大幅に減少するこ
とができる。例えば、エタノールの１当り、発
酵と濃縮（抽出）に要する熱量と動力から必要エ
ネルギーを試算すると、通常の蒸留法で9500、最
新鋭の蒸留法で5500ｍＪ程度のものが、本発明方
法により発酵時に液化炭酸ガスを用いた場合1500
ｍＪ程度と大幅な省エネとなる。しかも発酵液と
の相互溶解度が極めて小さく、またエタノールと
液化ガスとの分離も容易であるという顕著な効果
が奏せられる。
As explained in detail above, according to the present invention,
Low molecular weight compounds can be efficiently extracted from fermentation products. If this is applied particularly to the production of ethanol by fermentation, the energy that was conventionally required for distillation can be significantly reduced. For example, when calculating the energy required for fermentation and concentration (extraction) per unit of ethanol from the amount of heat and power required for fermentation and concentration (extraction), the amount of energy required during fermentation using the method of the present invention is approximately 9,500 mJ using a normal distillation method and approximately 5,500 mJ using the latest distillation method. 1500 when using liquefied carbon dioxide
This results in significant energy savings of approximately mJ. Moreover, the mutual solubility with the fermentation liquor is extremely low, and the remarkable effects of easy separation of ethanol and liquefied gas are exhibited.
第１図は本発明の抽出装置の１例の系統図、第
２図はバイオマスから低級アルコールを製造する
ための本発明による装置の系統図、第３図及び第
４図は本発明によるエタノール製造方法の１例の
工程図である。
４：混合器、７：分離槽、１１：蒸発槽、１
７：熱交換器、２３：水タービン、３３：脱リグ
ニン処理槽、３４：糖化発酵槽、３７：燃焼器、
５４：発酵タンク、５４′：充てん層（固定化微
生物）、５５：液化炭酸ガスのガス化タンク、５
６：凝縮器、５７：超臨界炭酸ガスのガス化タン
ク、５８：圧縮機、５９：温度調整器。
Figure 1 is a system diagram of an example of the extraction apparatus of the present invention, Figure 2 is a system diagram of an apparatus according to the present invention for producing lower alcohols from biomass, and Figures 3 and 4 are for ethanol production according to the present invention. It is a process diagram of an example of a method. 4: Mixer, 7: Separation tank, 11: Evaporation tank, 1
7: heat exchanger, 23: water turbine, 33: delignification treatment tank, 34: saccharification fermentation tank, 37: combustor,
54: Fermentation tank, 54': Filled layer (immobilized microorganisms), 55: Liquefied carbon dioxide gasification tank, 5
6: Condenser, 57: Supercritical carbon dioxide gasification tank, 58: Compressor, 59: Temperature regulator.
Claims (1)
量有機化合物を製造する方法において、二酸化炭
素が液化炭酸ガス又は超臨界炭酸ガスとなる圧力
及び温度条件下で発酵を行い、同発酵槽内でその
発酵生成物から該低分子量有機化合物を、該液化
炭酸ガス又は超臨界炭酸ガスで抽出、濃縮して分
離する工程を包含することを特徴とする低分子量
有機化合物の製造方法。 ２ 液化炭酸ガス又は超臨界炭酸ガスを添加して
発酵を行う特許請求の範囲第１項記載の低分子量
有機化合物の製造方法。 ３ 該分離した低分子量有機化合物を含有する液
から、該液化炭酸ガス又は超臨界炭酸ガスをガス
化して分離する工程を含む特許請求の範囲第１項
又は第２項記載の低分子量有機化合物の製造方
法。[Scope of Claims] 1. A method for producing a low molecular weight organic compound by a fermentation method involving the generation of carbon dioxide, in which fermentation is carried out under pressure and temperature conditions such that carbon dioxide becomes liquefied carbon dioxide or supercritical carbon dioxide. A method for producing a low molecular weight organic compound, comprising the step of extracting, concentrating and separating the low molecular weight organic compound from the fermentation product in a fermenter using the liquefied carbon dioxide gas or supercritical carbon dioxide gas. 2. The method for producing a low molecular weight organic compound according to claim 1, wherein fermentation is carried out by adding liquefied carbon dioxide gas or supercritical carbon dioxide gas. 3. The low molecular weight organic compound according to claim 1 or 2, which comprises the step of gasifying and separating the liquefied carbon dioxide gas or supercritical carbon dioxide gas from the liquid containing the separated low molecular weight organic compound. Production method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58172234A JPS6066988A (en) | 1983-09-20 | 1983-09-20 | Method for extraction and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58172234A JPS6066988A (en) | 1983-09-20 | 1983-09-20 | Method for extraction and apparatus therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6066988A JPS6066988A (en) | 1985-04-17 |
| JPH0419833B2 true JPH0419833B2 (en) | 1992-03-31 |
Family
ID=15938092
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58172234A Granted JPS6066988A (en) | 1983-09-20 | 1983-09-20 | Method for extraction and apparatus therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6066988A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6225982A (en) * | 1985-07-29 | 1987-02-03 | Mitsubishi Heavy Ind Ltd | Method of concentrating and purifying alcohol |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5656201A (en) * | 1979-09-28 | 1981-05-18 | Little Inc A | Method and device for separating organic liquid solute from mixture with solvent of said solute |
-
1983
- 1983-09-20 JP JP58172234A patent/JPS6066988A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5656201A (en) * | 1979-09-28 | 1981-05-18 | Little Inc A | Method and device for separating organic liquid solute from mixture with solvent of said solute |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6066988A (en) | 1985-04-17 |
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