JPS63269988A - Production of butanol - Google Patents
Production of butanolInfo
- Publication number
- JPS63269988A JPS63269988A JP10315987A JP10315987A JPS63269988A JP S63269988 A JPS63269988 A JP S63269988A JP 10315987 A JP10315987 A JP 10315987A JP 10315987 A JP10315987 A JP 10315987A JP S63269988 A JPS63269988 A JP S63269988A
- Authority
- JP
- Japan
- Prior art keywords
- butanol
- yeast
- fermentation
- tank
- producing bacteria
- 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.)
- Pending
Links
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000000855 fermentation Methods 0.000 claims abstract description 34
- 230000004151 fermentation Effects 0.000 claims abstract description 34
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims abstract description 27
- 238000011081 inoculation Methods 0.000 claims abstract description 4
- 241000894006 Bacteria Species 0.000 claims description 19
- 230000002062 proliferating effect Effects 0.000 abstract 1
- 230000035755 proliferation Effects 0.000 abstract 1
- 229940041514 candida albicans extract Drugs 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 239000012138 yeast extract Substances 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 150000001720 carbohydrates Chemical class 0.000 description 4
- 235000014633 carbohydrates Nutrition 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 230000005764 inhibitory process Effects 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 208000035404 Autolysis Diseases 0.000 description 2
- 206010057248 Cell death Diseases 0.000 description 2
- 241000193403 Clostridium Species 0.000 description 2
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 2
- 241000235070 Saccharomyces Species 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- DNZWLJIKNWYXJP-UHFFFAOYSA-N butan-1-ol;propan-2-one Chemical compound CC(C)=O.CCCCO DNZWLJIKNWYXJP-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000008103 glucose Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 235000012907 honey Nutrition 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000028043 self proteolysis Effects 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 235000013619 trace mineral Nutrition 0.000 description 2
- 239000011573 trace mineral Substances 0.000 description 2
- 241000193401 Clostridium acetobutylicum Species 0.000 description 1
- 241000423302 Clostridium acetobutylicum ATCC 824 Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000002054 inoculum Substances 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000013028 medium composition Substances 0.000 description 1
- 235000013379 molasses Nutrition 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 230000003313 weakening effect Effects 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明はブタノール生産濃度の窩いブタノール発酵によ
るブタノールの製造方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to a method for producing butanol by fermentation of butanol in a butanol production concentration.
ブタノールを発酵法により生産することはバイオテクノ
ロジーレターズ（Ｂｉｏｔｅｃｈｎｏｌｏｇｙ Ｌｅｔ
ｔｅｒｓ）ｖｏｌ、２ （／ぢ５ ） ｐ、 ２４１〜
２４６ （１９８０）や特開昭５９−２１６５９１号公
報などに見られるように一般的によく知られている。The production of butanol by fermentation is described in Biotechnology Letters.
ters) vol, 2 (/ぢ5) p, 241~
246 (1980) and Japanese Unexamined Patent Publication No. 59-216591.
従来、アセトン・ブタノール発酵として知られているよ
うに、炭水化物あるいは廃糖みつを原料に、クロストリ
ジウム・アセトブチリカム、クロストリジウム・サツカ
ロパーブチルアセトニカムなどにより、嫌気性条件下に
１回分発酵を行い。Traditionally known as acetone-butanol fermentation, carbohydrates or waste molasses are used as raw materials for one-time fermentation using Clostridium acetobutylicum, Clostridium satucaloperbutylacetonicum, etc. under anaerobic conditions.
アセトンと共にブタノール、さらには少量のエタノール
を回収し、ていた。Along with acetone, butanol and even a small amount of ethanol were recovered.
この従来の発酵方法は、ブタノール濃度が１．５（ｗ／
ｖ ）％を越えると発酵が停止するため、ブタノールを
高濃問に含む培養液が得られないことが大きな問題点で
ありまた発酵速度が遅いことも問題点の１つであった。This conventional fermentation method requires a butanol concentration of 1.5 (w/
If the concentration exceeds v)%, fermentation will stop, so a major problem is that a culture solution containing a high concentration of butanol cannot be obtained, and another problem is that the fermentation rate is slow.
ブタノール発酵においては、ブタノール濃度を高く維持
することが難しいがこれは、ブタノール生産菌に対する
ブタノールの阻害によるものと考えられる。またブタノ
ール生産菌は、絶対嫌気性菌であるため、槽内の嫌気度
（酸化還元電位ＯＲＰが−２００ｍＶ以下など）の厳し
い条件を必要とするが、従来の発酵槽では特別の工夫は
されておらず、又実施する場合には、Ｎ２ガス等を吹込
む付加装置を必要とする。さらにまた、実用上では、炭
水化物、廃糖ミツに、補助源として、窒素分（Ｎ）リン
分（乃を添加するにすぎず、経済性の面からもさらに、
微量成分が添加されることはなく、総じて実験室レイル
に比べ培地組成は貧弱であり、こレラの点モ、ブタノー
ル阻害に対するブタノール生産菌の抵抗力を弱める一因
であった。In butanol fermentation, it is difficult to maintain a high butanol concentration, and this is thought to be due to butanol's inhibition of butanol-producing bacteria. In addition, butanol-producing bacteria are obligate anaerobic bacteria, so they require strict anaerobic conditions in the tank (oxidation-reduction potential ORP of -200 mV or less, etc.), but in conventional fermenters, no special measures have been taken. However, if it is carried out, an additional device for blowing in N2 gas or the like is required. Furthermore, in practical terms, nitrogen (N) and phosphorus (乃) are simply added to carbohydrates and waste sugar honey as auxiliary sources, and from an economical point of view,
No trace components were added, and the medium composition was generally poorer than that of laboratory rail, which contributed to the weakening of the butanol-producing bacteria's resistance to butanol inhibition.
本発明は上記のような従来の発酵方法の欠点を改良した
培養液中のブタノール濃度が高く、嫌気条件達成のため
の補助設備が省除され、加温エネルギーの節減が計れか
つ系外からの微量元素源が不要なブタノール発酵による
ブタノールの製造方法を提供することを目的とするもの
である。The present invention improves the above-mentioned drawbacks of the conventional fermentation method by having a high butanol concentration in the culture solution, eliminating the need for auxiliary equipment to achieve anaerobic conditions, saving heating energy, and eliminating the need for energy from outside the system. The object of the present invention is to provide a method for producing butanol by butanol fermentation that does not require a trace element source.
〔問題点を解決するための手段〕
本発明はブタノール発酵プロセスにおいて、ブタノール
生産菌の接種に先立ち、酵母を接種し、これを培養増殖
させ、これにより発酵槽内を嫌気状態で、高められた温
度下に保つとともに所定時間酵母の自己分解を起させた
後、ブタノール生産菌を接種してブタノール発酵を行な
うことを特徴とするブタノールの製造方法を提案するも
のである。[Means for Solving the Problems] In the butanol fermentation process, the present invention inoculates yeast before inoculating butanol-producing bacteria and grows the yeast in culture, thereby creating an anaerobic state in the fermenter. The present invention proposes a method for producing butanol, which is characterized by maintaining the yeast at a temperature and allowing autolysis to occur for a predetermined period of time, and then inoculating butanol-producing bacteria to carry out butanol fermentation.
本発明では１発酵槽の嫌気条件を、ブタノール生産菌の
接種に先立ち、酵母（サツカロマイセス・セルビセ）の
接種培養で、達成させ、その生育により培地中の酸素（
ｏ２）の消去及び酸化還元電位の低下を進めると同時に
、その際に発生する発酵熱をその′＝！ま利用して、発
酵槽内温度をブタノール生産菌の至適温間（３７℃）ま
で上げる。この時点で酵母はその高温で生育できず、死
んでいく、一方、死んだ酵母は徐々に分解され、その中
に含まれる微量成分（実験室レベルでの酵母エキスと同
等物）は、結果としてはブタノール生産菌に対し、多量
の微量成分（酵母エキス）を添加した形となり、ブタノ
ール生産菌の活性上昇、ブタノール耐性の向上に寄与す
る。In the present invention, anaerobic conditions in one fermenter are achieved by inoculating and culturing yeast (Saccharomyces cervicae) prior to inoculating butanol-producing bacteria, and its growth causes oxygen in the medium to
At the same time, the fermentation heat generated at that time is eliminated by the elimination of o2) and the reduction of the redox potential. The temperature inside the fermenter is raised to the optimum temperature (37°C) for butanol-producing bacteria. At this point the yeast cannot grow at that high temperature and dies, while the dead yeast is gradually decomposed and the trace components it contains (equivalent to yeast extract at laboratory level) are removed as a result. is a form in which a large amount of a trace ingredient (yeast extract) is added to the butanol-producing bacteria, contributing to increasing the activity of the butanol-producing bacteria and improving butanol tolerance.
ブタノール生産菌の培養において添加される微量成分の
１つである酵母エキスについては、実験室レベルでは、
その添加量を増大させれば、ブタノール生産濃度を上昇
させうる効果があることが確認されているが、実用レベ
ルでは、この酵母エキスはその価格も高く市販薬品４ｏ
ｏｏ円／に！９であり、その添加は、運転コストの増大
につながシ、好ましくない。Regarding yeast extract, which is one of the trace components added in the culture of butanol-producing bacteria, at the laboratory level,
It has been confirmed that increasing the amount of yeast extract added has the effect of increasing the concentration of butanol produced, but at a practical level, this yeast extract is expensive and commercially available.
oo yen/to! 9, and its addition leads to an increase in operating costs, which is undesirable.
本発明はその点の工夫を１発酵槽の嫌気条件の達成並び
に３７℃という高温条件の設定と関連させて、しかも、
酵母が３７℃ではほとんど死滅し、自己分解を引き起こ
すことに着目して１本発明の完成に到ったものである。The present invention combines the improvements in this respect with the achievement of anaerobic conditions in one fermenter and the setting of high temperature conditions of 37°C, and furthermore,
The present invention was completed by focusing on the fact that yeast almost dies at 37°C and causes self-decomposition.
以下に作用効果を整理すると。The effects are summarized below.
（１） ブタノール生産菌の接種に先立ち、酵母（サ
ツカロマイセス・セルビセ＞ を発酵ｍ内に接種し、酵
母の増殖により、槽内の溶存酸素の消去、嫌気度の達成
を図る。酵母は、嫌気性でも生育できるが、発酵槽内の
温度を調整しないために、酵母の発酵熱により（酵母の
至適温度は３０’Ｃ）発酵槽内温度は上昇する。(1) Prior to inoculation of butanol-producing bacteria, yeast (Saccharomyces cervice) is inoculated into the fermentation tank, and the yeast multiplies to eliminate dissolved oxygen in the tank and achieve anaerobic degree. Yeast is anaerobic. However, since the temperature inside the fermenter is not adjusted, the temperature inside the fermenter rises due to the fermentation heat of the yeast (the optimum temperature for yeast is 30'C).
ｒ℃近辺になった所で、温度コントロールを行うと共に
ブタノール生産菌を接種し、ブタノール発酵に入る。When the temperature reaches around r°C, the temperature is controlled and butanol-producing bacteria are inoculated, and butanol fermentation begins.
（２）一方、３７’Ｃでは酵母は徐々に死滅し、自己分
解を起こし、液中に微量成分として酵母エキス分を放出
する。ブタノール生産菌は、これを微量成分として摂取
し、与えられた炭水化物、廃糖ミツをブタノールに変換
していき、その際微量成分の添加効果並びに高い嫌気度
によりブタノール阻害に対して強い抵抗力をもったブタ
ノール発酵が進み、高いブタノール生産濃度が得られる
。(2) On the other hand, at 37'C, yeast gradually dies, undergoes self-decomposition, and releases yeast extract as a trace component into the liquid. Butanol-producing bacteria ingest this as a trace component and convert the provided carbohydrates and waste sugar into butanol. At this time, they develop strong resistance to butanol inhibition due to the added effect of trace components and high anaerobic degree. Butanol fermentation proceeds and a high butanol production concentration is obtained.
〔実施例〕
第１図は本発明の一実施例を説明するための説明図であ
り、第１図において、酵母（サツカロマイセス・セルビ
セ 発研１号あるいは工Ｆ０２０４４など１通常のアル
コール発酵酵母、パン酵母など）は、接種に先立ち、グ
ルコースを含む酵母培地を収容した酵母前培養槽１で前
培養されライン９を通じてブタノール発酵槽６に培地液
量の５〜１０％接種される。なお１機械攪拌装置付のブ
タノール発酵槽６には、予め原料貯槽４よシ原料として
供給された炭水化物、廃糖ミツが収容されている。[Example] Fig. 1 is an explanatory diagram for explaining one embodiment of the present invention. Prior to inoculation, yeast (such as yeast) is precultured in a yeast preculture tank 1 containing a yeast medium containing glucose, and is inoculated into a butanol fermentation tank 6 through a line 9 in an amount of 5 to 10% of the volume of the medium. Note that the butanol fermentation tank 6 equipped with a mechanical stirring device stores carbohydrates and waste sugar honey that have been supplied as raw materials from the raw material storage tank 4 in advance.
その原料の供給に際してまずブタノール発酵槽６の容量
の１／３相当量が原料貯槽４からライン１２でプレート
熱交換型殺菌装置５に入り殺菌され、ついでライン１３
からブタノール発酵槽６に導入される。なお、この時、
グルコースは少なくとも２０１７１以上になるように調
整する。またブタノール発酵槽６には、図には示されて
いないが、Ｎ源、Ｐ源が所定量添加される。酵母を接種
後、槽内の温度。When supplying the raw material, first, an amount equivalent to 1/3 of the capacity of the butanol fermentation tank 6 enters the plate heat exchange type sterilizer 5 from the raw material storage tank 4 through the line 12 and is sterilized, and then is sterilized through the line 13.
is introduced into the butanol fermenter 6. Furthermore, at this time,
Glucose is adjusted to be at least 20171 or higher. Although not shown in the figure, predetermined amounts of an N source and a P source are added to the butanol fermentation tank 6. Temperature inside the tank after inoculating yeast.
ＯＲＰ をモニターしながらブタノール発酵槽６を運
転し、温度が３７℃になった時点で、温度調節装置７を
通して冷水をライン１４．戻りライン１５でブタノール
発酵槽６に循環させ、ブタノール発酵槽６内を３７℃に
保つ。この時点から少なくとも約６時間保持し酵母の自
己分解を促進させる。The butanol fermenter 6 is operated while monitoring the ORP, and when the temperature reaches 37°C, cold water is introduced into the line 14 through the temperature controller 7. It is circulated through the return line 15 to the butanol fermenter 6, and the inside of the butanol fermenter 6 is maintained at 37°C. From this point, hold for at least about 6 hours to promote autolysis of the yeast.
また、ブタノール生産菌（クロストリジウム・アセトブ
チリカムＡＴＣＣ８２４あるいはクロストリジウム・サ
ツカロパーブチルアセトニカムＡＴＣＣ２７０２２）は
１００℃、９０秒のヒートショックを種菌調整装置２で
受け、ブタノール生産菌前培養槽３でライン１１を通じ
てブタノール発酵槽６に培地液量の５〜１０チ接種され
る。この時予めブタノール発酵槽６には前記と同様にし
て、殺菌された原料がブタノール発酵槽６の容量のＶ３
相当量添加されている。（なお、この量の添加量は全量
を一気に入れてもよいが、段階的に入れることも考えら
れる）
このようにして、ブタノール発酵槽６では、嫌気条件が
保たれた中で、しかも酵母の分解物を十分に含んだ、３
７℃条件下で、またｐＨのコントロールを行なう場合は
、ｐ）ｉ＝４．５〜５．０に調整し。In addition, the butanol-producing bacteria (Clostridium acetobutylicum ATCC 824 or Clostridium satucaloperbutylacetonicum ATCC 27022) is subjected to a heat shock at 100°C for 90 seconds in the seed preparation device 2, and the butanol-producing bacteria is passed through the line 11 in the butanol-producing bacteria pre-culture tank 3. The fermenter 6 is inoculated with 5 to 10 liquid volumes of the medium. At this time, the sterilized raw material is placed in the butanol fermentation tank 6 in advance in the same manner as described above.
A considerable amount is added. (Although this amount of addition may be added all at once, it may also be added in stages.) In this way, in the butanol fermenter 6, anaerobic conditions are maintained, and yeast Contains sufficient decomposition products, 3
When controlling the pH under 7°C conditions, adjust p) i to 4.5 to 5.0.
運転時間５０〜１００時間ブタノール発酵が行なわれる
。Butanol fermentation is carried out for an operating time of 50 to 100 hours.
発酵終了後は、公知の方法で、後処理系統装置群８に入
り、菌体分離、蒸留１分留され、生産物としてライン１
８でブタノールアセトン、エタノールが取り出される。After the fermentation is completed, it enters the post-processing equipment group 8 using a known method, where it is subjected to bacterial cell separation and one fractional distillation, and is sent to the line 1 as a product.
Butanol acetone and ethanol are taken out at step 8.
一方廃棄物はライン１７で系外に排出される。このよう
に本発明の実施例によれば発酵は速かに進みかつブタノ
ール濃度が従来の方法では１５ ｉ／ｌのものが、２３
１１／ｌ程度に達し約力壬生産性が向上した。On the other hand, waste is discharged out of the system via line 17. Thus, according to the embodiment of the present invention, fermentation proceeds rapidly and the butanol concentration is reduced from 15 i/l in the conventional method to 23 i/l.
The productivity has improved to about 11/l.
本発明の方法によれば、従来法に比べ、生産ブタノール
濃度を約１．５倍（２，３ＷＡ−％）上昇させることが
できると共に、嫌気条件達成のための補助設備（Ｎ２ガ
ス吹込み）が省かれ培讐初期の加温エネルギーの節減が
計れる。また、外部より添加される微量元素源が不要に
なり、そのランニングコストを低減できるとともにその
添加設備を削減することができる特有の効果を奏する。According to the method of the present invention, the concentration of butanol produced can be increased approximately 1.5 times (2.3 WA-%) compared to the conventional method, and auxiliary equipment (N2 gas injection) for achieving anaerobic conditions This eliminates the need for heating energy during the initial stage of cultivation. Further, there is no need for a trace element source added externally, which has the unique effect of reducing running costs and reducing addition equipment.
第１図は１本発明の一実施例を説明するための説明図で
ある。
１・・・酵母前培養槽 ２・・・種菌調整装置３・・
・ブタノール生産菌前培養槽
８・・・後処理系統装置群
第１図FIG. 1 is an explanatory diagram for explaining one embodiment of the present invention. 1... Yeast pre-culture tank 2... Inoculum adjustment device 3...
・Butanol-producing bacteria pre-cultivation tank 8...Post-treatment system equipment group Figure 1
Claims (1)
接種に先立ち、酵母を接種し、これを培養増殖させ、こ
れにより発酵槽内を嫌気状態で高められた温度下に保つ
とともに、所定時間酵母の自己分解を起させた後、ブタ
ノール生産菌を接種してブタノール発酵を行なうことを
特徴とするブタノールの製造方法。In the butanol fermentation process, prior to the inoculation of butanol-producing bacteria, yeast is inoculated and cultured to proliferate, thereby maintaining the inside of the fermenter at an elevated temperature in an anaerobic state and allowing the yeast to self-decompose for a predetermined period of time. A method for producing butanol, which comprises inoculating butanol-producing bacteria to carry out butanol fermentation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10315987A JPS63269988A (en) | 1987-04-28 | 1987-04-28 | Production of butanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10315987A JPS63269988A (en) | 1987-04-28 | 1987-04-28 | Production of butanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63269988A true JPS63269988A (en) | 1988-11-08 |
Family
ID=14346725
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10315987A Pending JPS63269988A (en) | 1987-04-28 | 1987-04-28 | Production of butanol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63269988A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9260731B2 (en) | 2011-08-01 | 2016-02-16 | Reliance Industries Limited | Butanol fermentation using acid pretreated biomass |
| US9663759B2 (en) | 2013-07-03 | 2017-05-30 | Butamax Advanced Biofuels Llc | Partial adaptation for butanol production |
-
1987
- 1987-04-28 JP JP10315987A patent/JPS63269988A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9260731B2 (en) | 2011-08-01 | 2016-02-16 | Reliance Industries Limited | Butanol fermentation using acid pretreated biomass |
| US9663759B2 (en) | 2013-07-03 | 2017-05-30 | Butamax Advanced Biofuels Llc | Partial adaptation for butanol production |
| US10308910B2 (en) | 2013-07-03 | 2019-06-04 | Butamax Advanced Biofuels Llc | Partial adaption for butanol production |
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