JP5748979B2 - Ethanol production apparatus and production method using the same - Google Patents
Ethanol production apparatus and production method using the same Download PDFInfo
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- JP5748979B2 JP5748979B2 JP2010229750A JP2010229750A JP5748979B2 JP 5748979 B2 JP5748979 B2 JP 5748979B2 JP 2010229750 A JP2010229750 A JP 2010229750A JP 2010229750 A JP2010229750 A JP 2010229750A JP 5748979 B2 JP5748979 B2 JP 5748979B2
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims description 95
- 238000004519 manufacturing process Methods 0.000 title claims description 25
- 238000000855 fermentation Methods 0.000 claims description 20
- 230000004151 fermentation Effects 0.000 claims description 20
- 238000004821 distillation Methods 0.000 claims description 17
- 239000002994 raw material Substances 0.000 claims description 17
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 14
- 238000007664 blowing Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- 108090000790 Enzymes Proteins 0.000 claims description 9
- 102000004190 Enzymes Human genes 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 6
- 239000002918 waste heat Substances 0.000 claims description 5
- 230000001476 alcoholic effect Effects 0.000 claims description 3
- 230000002068 genetic effect Effects 0.000 claims 1
- 108090000623 proteins and genes Proteins 0.000 claims 1
- 229940088598 enzyme Drugs 0.000 description 7
- 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 6
- 239000008103 glucose Substances 0.000 description 6
- 239000010794 food waste Substances 0.000 description 5
- 240000007594 Oryza sativa Species 0.000 description 4
- 235000007164 Oryza sativa Nutrition 0.000 description 4
- 235000009566 rice Nutrition 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 235000014663 Kluyveromyces fragilis Nutrition 0.000 description 3
- 244000253911 Saccharomyces fragilis Species 0.000 description 3
- 235000018368 Saccharomyces fragilis Nutrition 0.000 description 3
- 229920002472 Starch Polymers 0.000 description 3
- 238000011109 contamination Methods 0.000 description 3
- 235000013305 food Nutrition 0.000 description 3
- 229940031154 kluyveromyces marxianus Drugs 0.000 description 3
- 235000019698 starch Nutrition 0.000 description 3
- 239000008107 starch Substances 0.000 description 3
- 239000004382 Amylase Substances 0.000 description 2
- 102000013142 Amylases Human genes 0.000 description 2
- 108010065511 Amylases Proteins 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 108010059892 Cellulase Proteins 0.000 description 2
- 108010073178 Glucan 1,4-alpha-Glucosidase Proteins 0.000 description 2
- 102100022624 Glucoamylase Human genes 0.000 description 2
- 102000004139 alpha-Amylases Human genes 0.000 description 2
- 108090000637 alpha-Amylases Proteins 0.000 description 2
- 229940024171 alpha-amylase Drugs 0.000 description 2
- 235000019418 amylase Nutrition 0.000 description 2
- 229940106157 cellulase Drugs 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000006798 recombination Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 235000013311 vegetables Nutrition 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000001888 Peptone Substances 0.000 description 1
- 108010080698 Peptones Proteins 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- UYJXRRSPUVSSMN-UHFFFAOYSA-P ammonium sulfide Chemical compound [NH4+].[NH4+].[S-2] UYJXRRSPUVSSMN-UHFFFAOYSA-P 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 235000014633 carbohydrates Nutrition 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 235000010980 cellulose Nutrition 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 235000019319 peptone Nutrition 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 235000014347 soups Nutrition 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M43/00—Combinations of bioreactors or fermenters with other apparatus
- C12M43/02—Bioreactors or fermenters combined with devices for liquid fuel extraction; Biorefineries
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- 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
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- Life Sciences & Earth Sciences (AREA)
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- Chemical & Material Sciences (AREA)
- Zoology (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
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- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
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Description
本発明は、炭水化物に属するデンプン質原料やセルロース質原料を用いた連続発酵蒸留によるバイオエタノールの製造装置及び製造方法に関し、特に焼却炉と連結することで食品廃棄物、野菜等の余剰生産物等の廃棄物処理とバイオエタノール製造との一体化に好適な装置及び方法に係る。 The present invention relates to a bioethanol production apparatus and production method by continuous fermentation distillation using starchy raw materials and cellulosic raw materials belonging to carbohydrates, and in particular, surplus products such as food waste and vegetables by being connected to an incinerator. The present invention relates to an apparatus and method suitable for the integration of waste disposal and bioethanol production.
小麦やトウモロコシ等の食料ともなる原材料を用いたバイオエタノールの製造方法では食料供給に影響を与えることから、厨房等から排出される食品廃棄物からエタノールを製造する方法が提案されている（特許文献１）。
しかし、同公報に記載されているような従来のバイオエタノールの製造方法にあっては、第１に糖化及び培養後にバッチで蒸留処理するものであり、連続的にエタノールを製造できるものではなかった。
第２にバイオエタノールの製造に用いる熱源に外部から購入する燃料や電気が必要であり、多量に発生する培養残渣や蒸留廃液の処理を外部委託に頼っているために高コストの一因になっていた。
Since the production method of bioethanol using raw materials that also serve as food such as wheat and corn affects food supply, a method for producing ethanol from food waste discharged from kitchens has been proposed (patent document) 1).
However, in the conventional method for producing bioethanol as described in the publication, firstly, saccharification and culturing are carried out in a batch, and ethanol cannot be produced continuously. .
Secondly, fuel and electricity purchased from the outside are necessary for the heat source used in the production of bioethanol, and it is a cause of high cost because it relies on outsourcing for the treatment of large amounts of culture residue and distilled waste liquid. It was.
本発明は、製造フローが短く、装置の小型化低コスト化が容易で、食品廃棄物を原料とした場合に焼却炉と一体化が可能なエタノールの製造装置及び製造方法の提供を目的とする。 An object of the present invention is to provide an ethanol production apparatus and a production method that can be integrated with an incinerator when the production flow is short, the size and cost of the apparatus are easily reduced, and food waste is used as a raw material. .
本発明に係るエタノール製造装置は、デンプン質原料又は／及びセルロース質原料投入手段と、糖化処理と耐熱好気性酵母による発酵を連続的に行うための培養タンクと、前記培養タンク中の発酵した培養液に当該発酵を進行させながらエアーを吹き込むためのエアー吹き込み手段と、前記エアーの吹き込みにより排出されるガス中からエタノールを回収するための蒸留手段とを備えたことを特徴とする。 The ethanol production apparatus according to the present invention comprises a starchy material or / and cellulosic material charging means, a culture tank for continuously performing saccharification and fermentation with a thermophilic aerobic yeast, and the fermented culture in the culture tank. An air blowing means for blowing air while advancing the fermentation into the liquid, and a distillation means for recovering ethanol from the gas discharged by blowing the air are provided.
ここでデンプン質原料及びセルロース質原料とは、デンプンやセルロースが含まれている原料を意味し、家庭や外食産業から発生する生ゴミ等の食品廃棄物、食品の加工工程から生じる廃棄物、野菜等の余剰生産物等であってもよく、特に本発明にあっては、米のとぎ汁のような、従来はバイオエタノールの原料にできなかったものも対象にできる。 Here, the starchy raw material and the cellulosic raw material mean a raw material containing starch and cellulose, food waste such as raw garbage generated from households and the restaurant industry, waste generated from food processing, vegetables In particular, in the present invention, it is also possible to target those that could not be conventionally used as raw materials for bioethanol, such as rice broth.
本発明にて特徴的なのは、アルコール発酵に用いる酵母に好気性の菌株を採用することで、エアーを吹き込みながら連続的にエタノールの回収及び蒸留が可能になった点にある。 The feature of the present invention is that the use of an aerobic strain for yeast used for alcoholic fermentation makes it possible to continuously recover and distill ethanol while blowing air.
また、前記培養タンクから発生する培養残渣を焼却する焼却炉と、前記蒸留手段から発生する蒸留廃液を前記焼却炉から発生する排ガスの減温処理に使用することで、焼却装置と連結するとエタノールの製造に伴って発生する培養残渣を燃焼させることで糖化処理及び発酵の熱源に使用でき、蒸留廃液を焼却炉の排ガスの減温処理に用いることができ、装置全体のエネルギー源の省エネルギー化を図るのに効果的である。
ここで、前記培養タンクは熱媒体循環部を有し、当該熱媒体循環部に循環させる熱媒体の熱源として前記焼却炉から発生する廃熱を利用することもできる。
In addition, an incinerator that incinerates the culture residue generated from the culture tank, and a distillation waste solution generated from the distillation means is used for the temperature reduction treatment of the exhaust gas generated from the incinerator, so that when ethanol is connected to the incinerator, By burning the culture residue generated during the production, it can be used as a heat source for saccharification and fermentation, and the distillation waste liquid can be used for reducing the temperature of exhaust gas from the incinerator, thus reducing the energy source of the entire system. It is effective.
Here, the culture tank has a heat medium circulation part, and waste heat generated from the incinerator can be used as a heat source of the heat medium to be circulated in the heat medium circulation part.
上記のようなエタノール製造装置を用いた本発明に係るエタノールの製造方法は、培養タンクにデンプン質原料又は／及びセルロース質原料を投入するステップと、培養タンクに糖化能を有する、酵素又は遺伝子組み換え型耐熱好気性酵母を投入し糖化処理するステップと、前記酵素で糖化処理した場合は糖化処理後に耐熱好気性酵母を投入し、又は前記遺伝子組み換え型耐熱好気性酵母で糖化処理した場合はそのままアルコール発酵する発酵ステップと、前記発酵液にエアーを吹き込み、前記アルコール発酵を進行させながら連続的にエタノールを回収するステップとを有することを特徴とする。
糖化処理には一般的に糖化酵素を用いるが遺伝子組み換え技術により、糖化能を有する好気性酵母を用いると、そのまま連続してアルコール発酵も行うことができる。
ここで、培養タンクの温調に、培養タンクから発生する培養残渣を焼却して発生する廃熱を利用してもよい。
The ethanol production method according to the present invention using the ethanol production apparatus as described above includes a step of introducing starchy raw materials and / or cellulosic raw materials into a culture tank, and an enzyme or genetic recombination having saccharification ability in the culture tank. A thermostable and aerobic yeast with a saccharification treatment, and if saccharification treatment with the enzyme, a thermostable aerobic yeast is added after saccharification treatment , or if saccharification treatment with the genetically modified thermostable aerobic yeast It has a fermentation step of fermenting, and a step of continuously collecting ethanol while blowing air into the fermentation broth and allowing the alcoholic fermentation to proceed .
In general, saccharification enzymes are used for the saccharification treatment, but if an aerobic yeast having saccharification ability is used by genetic recombination technology, alcohol fermentation can also be carried out continuously as it is.
Here, waste heat generated by incineration of the culture residue generated from the culture tank may be used for temperature control of the culture tank.
本発明にあっては、培養タンクにデンプン質原料、セルロース質原料を投入、乾物重量で１〜６０％、好ましくは２０〜４０％になるように水分調整し、原料の材質に合うような酵素を選択し、焼却炉の廃熱を利用して最適温度に温調する。
例えば、セルロース質原料が主な場合に酵素としてセルラーゼを使用し、２５℃〜７０℃、好ましくは４５℃〜５０℃に温調する。
また、セルロース質原料をセルラーゼで酵素処理する前に９０℃〜１００℃×１〜２時間加熱すると殺菌効果があり、その後の雑菌混入を抑えることができる。
また、デンプン質原料が主な場合には酵素としてアミラーゼを使用する。
α−アミラーゼを使用する場合は、８２℃〜８６℃×約２時間、グルコアミラーゼを使用する場合は６０℃〜６５℃×２４〜４８時間が好ましい。
In the present invention, starch material and cellulosic material are added to the culture tank, the moisture is adjusted to 1 to 60%, preferably 20 to 40% by dry matter weight, and the enzyme matches the material of the material. And adjust the temperature to the optimum temperature using the waste heat from the incinerator.
For example, when cellulosic raw materials are mainly used, cellulase is used as an enzyme, and the temperature is adjusted to 25 ° C to 70 ° C, preferably 45 ° C to 50 ° C.
In addition, if the cellulosic material is heated at 90 ° C. to 100 ° C. for 1 to 2 hours before the enzyme treatment with cellulase, there is a bactericidal effect and subsequent contamination with bacteria can be suppressed.
In addition, amylase is used as an enzyme when starchy raw materials are mainly used.
When α-amylase is used, it is preferably 82 ° C. to 86 ° C. × about 2 hours, and when glucoamylase is used, it is preferably 60 ° C. to 65 ° C. × 24 to 48 hours.
前記のように温調及び撹拌し糖化処理が終了すると、次に培養タンクを３０℃〜５０℃、好ましくは３６℃〜４５℃に温調し、好気性の耐熱性酵母（ｋｌｕｙｖｅｒｏｍｙｃｅｓ ｍａｒｘｉａｎｕｓ）を添加し、培養する。
この場合にｐＨ３．５〜７．０、好ましくは４．５〜５．５に調整されているのがよい。
アルコール発酵が進行すると、エアー吹き込み手段にて培養液中にエアーを吹き込むことでエアーとともにエタノールが排出される。
これを蒸留塔に通過させることで、濃度９０％以上、特に９９％以上のエタノールが得られる。
When the saccharification treatment is completed by temperature control and stirring as described above, the culture tank is then temperature-controlled at 30 ° C. to 50 ° C., preferably 36 ° C. to 45 ° C., and an aerobic thermostable yeast (kluyveromyces marxianus) is added. And incubate.
In this case, the pH may be adjusted to 3.5 to 7.0, preferably 4.5 to 5.5.
When alcohol fermentation progresses, ethanol is discharged together with air by blowing air into the culture solution by air blowing means.
By passing this through a distillation column, ethanol having a concentration of 90% or more, particularly 99% or more can be obtained.
本発明に係るエタノールの製造装置にあっては、培養タンクに食品廃棄物等を投入し、水分調整した後に糖化処理するステップと発酵処理するステップ及びその後に連続的にエタノールの蒸留が行えるので、装置がコンパクトで設備投資が従来法よりも少なくてよい。
また、処理フローが簡単なので原材料の変更やバラツキにも対応しやすく、安定したエタノールの製造が可能である。
さらに、焼却炉と組み合せることで培養残渣物をエタノール製造装置の熱源として利用できるだけでなく、蒸留廃液を焼却炉の排ガスの減温処理に利用できるので相互に有効利用できる。
In the ethanol production apparatus according to the present invention, food waste and the like are introduced into the culture tank, and after adjusting the moisture, the step of saccharification treatment and the step of fermentation treatment and subsequent ethanol distillation can be performed. The equipment is compact and the capital investment may be less than that of the conventional method.
In addition, since the processing flow is simple, it is easy to cope with changes and variations in raw materials, and stable ethanol production is possible.
Further, in combination with an incinerator, not only can the culture residue be used as a heat source for the ethanol production apparatus, but also the distilled waste liquid can be used for the temperature reduction treatment of the exhaust gas from the incinerator, so that they can be used effectively.
本発明に係るエタノール装置の構成例を図１に基づいて説明する。
図１において実線で囲んだ部分が直接的にエタノールの製造に関与する装置であり、点線で囲んだ部分が焼却装置を組み合せた部分である。
本実施例では、原材料毎に温調範囲が相違しても対応できるように培養タンク１０Ａ、１０Ｂの二基を備えた例になっているが、培養タンクが少なくとも一基以上備えていれば、その数に制限はない。
培養タンク１０Ａ、１０Ｂは原材料の投入口１１と発生したエタノール含有ガスを取り出すための排出口１２を有し、この排出口１２は蒸留塔２０に配管連結されている。
培養及びエタノールの発生が終了した培養残渣物は残渣取出口１４から排出され、焼却炉３０の残渣物投入口１４ａに投入され焼却される。
残渣物は必要に応じて着火バーナー３０ａ及び２次燃焼バーナー３０ｂにより制御された焼却炉３０で燃焼し、高温の排ガスは予冷器３１及び減温器３２にて減温され、バクフィルター３３等にて浄化後に誘引ファン３４を介して煙突３５から大気中に放出される。
予冷器３１にて約１０００℃以下に温度が下がった排ガスは熱交換器３２ａを介して熱媒体の加温に使用され、この熱媒体はジャケット構造の培養タンクの熱媒体ＩＮ１３ａから流入し、熱媒体ＯＵＴ１３ｂを介して熱交換器３２ａに循環される。
また、培養タンク１０Ａ，１０Ｂには図示を省略したエアーの吹き込み手段を有し、蒸留前エタノールが排出口１２からエアーとともに排出し、蒸留塔２０にて高濃度のエタノールに蒸留される。
蒸留塔２０から発生する蒸留廃液１７は予冷器３１及び減温器３２中に噴露気化され、排ガスの減温処理に用いられる。
これによりエタノールの製造と廃棄物の焼却処理とを組み合せることが可能になり、有機系の廃棄物処理を行いながらエタノールの製造を行うことも可能になる。
A configuration example of an ethanol apparatus according to the present invention will be described with reference to FIG.
In FIG. 1, the part surrounded by a solid line is an apparatus directly involved in ethanol production, and the part surrounded by a dotted line is a part combining an incinerator.
In this example, it is an example provided with two culture tanks 10A, 10B so that even if the temperature control range is different for each raw material, but if at least one culture tank is provided, There is no limit to the number.
The culture tanks 10 </ b> A and 10 </ b> B have a raw material input port 11 and a discharge port 12 for taking out the generated ethanol-containing gas, and the discharge port 12 is connected to a distillation column 20 by piping.
The culture residue after completion of the culture and generation of ethanol is discharged from the residue outlet 14, and is charged into the residue inlet 14 a of the incinerator 30 and incinerated.
The residue is combusted in the incinerator 30 controlled by the ignition burner 30a and the secondary combustion burner 30b as necessary, and the high-temperature exhaust gas is reduced in temperature by the precooler 31 and the temperature reducer 32, and is supplied to the back filter 33 and the like. After purification, it is discharged from the chimney 35 through the induction fan 34 into the atmosphere.
The exhaust gas whose temperature has decreased to about 1000 ° C. or less in the precooler 31 is used for heating the heat medium via the heat exchanger 32a, and this heat medium flows from the heat medium IN13a of the culture tank having the jacket structure, It is circulated to the heat exchanger 32a via the medium OUT13b.
In addition, the culture tanks 10 </ b> A and 10 </ b> B have air blowing means (not shown), and the pre-distillation ethanol is discharged together with the air from the discharge port 12, and is distilled into high-concentration ethanol in the distillation tower 20.
The distillation waste liquid 17 generated from the distillation column 20 is vaporized into the precooler 31 and the temperature reducer 32 and used for the temperature reduction treatment of the exhaust gas.
This makes it possible to combine ethanol production and waste incineration, and it is also possible to produce ethanol while performing organic waste treatment.
次に、米のとぎ汁を用いてエタノールの製造実験を実施したので以下説明する。
培養タンクに、米のとぎ汁４５ｋｇ（固形分約８６ｇ）と窒素源として硫化アンモニウム１００ｇを投入し、前処理として７０℃×３時間保温した。
次に、培養タンクを５０℃に温調し、アミラーゼ（グルコアミラーゼ４，０００，０００ｕｎｉｔｓ、α−アミラーゼ７，５００，０００ｕｎｉｔｓ）を加え、撹拌しながら約２時間保持した。
次に培養タンクを４５℃に温調し、酵母（ｋｌｕｙｖｅｒｏｍｙｃｅｓ ｍａｒｘｉａｎｕｓ）を加え３９時間培養した。
グルコースがほぼ消費されたことを確認し、エアーを吹き込み始め、そのまま７９時間維持した。
このエアーの吹き込みにより培養液から出てくるガスを冷却管に通してエタノール溶液を回収した。
その時のグルコースの変化と１００％換算エタノールの発生量を図２のグラフに示す。
これによりデンプンが多く含まれる米のとぎ汁固形分約８６ｇから約２．２ｍｌのエタノールを得たことになる。
ここで、７０℃×３時間の前処理をしたことにより雑菌の混入を抑え、ｐＨは６．７から４．７に変化していた。
なお、エタノールの発酵を約４５℃で実施したことも雑菌の混入を抑える効果があったと推定される。
Next, since the ethanol production experiment was conducted using rice soup, it will be described below.
To the culture tank, 45 kg of rice broth (solid content: about 86 g) and 100 g of ammonium sulfide as a nitrogen source were added, and kept at 70 ° C. for 3 hours as a pretreatment.
Next, the temperature of the culture tank was adjusted to 50 ° C., amylase (glucoamylase 4,000,000 units, α-amylase 7,500,000 units) was added, and the mixture was held for about 2 hours with stirring.
Next, the temperature of the culture tank was adjusted to 45 ° C., and yeast (kluyveromyces marxianus) was added and cultured for 39 hours.
After confirming that glucose was almost consumed, air was blown in and maintained for 79 hours.
The gas coming out of the culture broth by blowing air was passed through a cooling tube to recover the ethanol solution.
The graph of FIG. 2 shows the change in glucose and the amount of 100% equivalent ethanol generated at that time.
As a result, about 2.2 g of ethanol was obtained from about 86 g of the solid content of rice broth containing a large amount of starch.
Here, pretreatment at 70 ° C. × 3 hours suppressed contamination of various bacteria, and the pH changed from 6.7 to 4.7.
In addition, it was presumed that the fermentation of ethanol at about 45 ° C. also had the effect of suppressing contamination with various bacteria.
次に、培養液の発酵効率を確認すべく以下のとおり実験を行った。
グルコース２，０００ｇに耐熱好気性酵母（ｋｌｕｙｖｅｒｏｍｙｃｅｓ ｍａｒｘｉａｎｕｓ）エキス１００ｇ及び酵母の栄養源としてペプトン１００ｇを加え、さらに水１７，８００ｇを加え、全量で２０，０００ｇに調整した。
この液をｐＨ５．０に調整し、４０℃に維持した。
培養中、コンプレッサーを用いて１２ｌ／ｍｉｎのエアーを吹き込み、発生したガスはコンデンサーにて冷却し、水（２ｌ）にトラップした。
このときの蒸留液と培養残渣の組成を図３に示す。
この結果、２，０００ｇのグルコースから蒸留液中にエタノール６８５ｇ、培養残渣中にエタノール１９９ｇ含まれたことから合計８８４ｇのエタノールが発生したことになり、理論値（エタノール１，０２３ｇ）に対するエタノールの発生量は８６％であった。
Next, an experiment was conducted as follows to confirm the fermentation efficiency of the culture solution.
To 2,000 g of glucose, 100 g of thermophilic aerobic yeast (kluyveromyces marxianus) extract and 100 g of peptone as a nutrient source of yeast were added, and 17,800 g of water was further added to adjust the total amount to 20,000 g.
The solution was adjusted to pH 5.0 and maintained at 40 ° C.
During culture, air of 12 l / min was blown using a compressor, and the generated gas was cooled by a condenser and trapped in water (2 l).
The composition of the distillate and the culture residue at this time is shown in FIG.
As a result, 685 g of ethanol was contained in the distillate from 2,000 g of glucose, and 199 g of ethanol was contained in the culture residue, so that a total of 884 g of ethanol was generated, and generation of ethanol relative to the theoretical value (ethanol 1,023 g). The amount was 86%.
１０Ａ 培養タンク
１１ 投入口
１２ 排出口
１３ａ 熱媒体ＩＮ
１３ｂ 熱媒体ＯＵＴ
１４ 残渣物取出口
１４ａ 残渣物投入口
１５ 蒸留前エタノール
１６ 蒸留エタノール
１７ 蒸留廃液
２０ 蒸留塔
３０ 焼却炉
10A culture tank 11 inlet 12 outlet 13a Heat medium IN
13b Heat carrier OUT
14 Residue outlet 14a Residue inlet 15 Ethanol 16 before distillation 16 Distilled ethanol 17 Distilled waste 20 Distillation tower 30 Incinerator
Claims (5)
糖化処理と耐熱好気性酵母による発酵を連続的に行うための培養タンクと、
前記培養タンク中の発酵した培養液に当該発酵を進行させながらエアーを吹き込むためのエアー吹き込み手段と、
前記エアーの吹き込みにより排出されるガス中からエタノールを回収するための蒸留手段とを備えたことを特徴とするエタノール製造装置。 Starchy raw material or / and cellulosic raw material charging means;
A culture tank for continuously performing saccharification treatment and fermentation with thermophilic aerobic yeast ,
Air blowing means for blowing air while advancing the fermentation to the fermented culture solution in the culture tank;
An ethanol production apparatus comprising distillation means for recovering ethanol from gas discharged by blowing air.
前記蒸留手段から発生する蒸留廃液を前記焼却炉から発生する排ガスの減温処理に使用することで、焼却装置と連結したことを特徴とする請求項１記載のエタノール製造装置。 An incinerator for incinerating culture residues generated from the culture tank;
2. The ethanol production apparatus according to claim 1, wherein the distillation waste liquid generated from the distillation means is used for temperature reduction treatment of exhaust gas generated from the incinerator, and is connected to an incinerator.
培養タンクに糖化能を有する、酵素又は遺伝子組み換え型耐熱好気性酵母を投入し糖化処理するステップと、
前記酵素で糖化処理した場合は糖化処理後に耐熱好気性酵母を投入し、又は前記遺伝子組み換え型耐熱好気性酵母で糖化処理した場合はそのままアルコール発酵する発酵ステップと、
前記発酵液にエアーを吹き込み、前記アルコール発酵を進行させながら連続的にエタノールを回収するステップとを有することを特徴とするエタノールの製造方法。 Adding a starchy material or / and a cellulosic material to the culture tank;
A step of having a glycated ability to culture tank was charged with enzyme or gene recombinant heat aerobic yeast saccharification,
A fermentation step if you saccharification treatment with the enzyme heat aerobic yeast was charged after saccharification, or if you saccharification treatment with the genetic recombinant heat aerobic yeast to directly alcohol fermentation,
And a step of continuously recovering ethanol while advancing the alcoholic fermentation by blowing air into the fermentation broth.
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