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WO2010070716A1 - Procédé et appareil pour la production d'éthanol - Google Patents

Procédé et appareil pour la production d'éthanol Download PDF

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Publication number
WO2010070716A1
WO2010070716A1 PCT/JP2008/072733 JP2008072733W WO2010070716A1 WO 2010070716 A1 WO2010070716 A1 WO 2010070716A1 JP 2008072733 W JP2008072733 W JP 2008072733W WO 2010070716 A1 WO2010070716 A1 WO 2010070716A1
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WIPO (PCT)
Prior art keywords
ethanol
fermentation
liquid
gas
concentration
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.)
Ceased
Application number
PCT/JP2008/072733
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English (en)
Japanese (ja)
Inventor
茂 坂下
勉 川▲崎▼
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mayekawa Manufacturing Co
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Mayekawa Manufacturing Co
Priority date (The priority date 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 date listed.)
Filing date
Publication date
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Priority to PCT/JP2008/072733 priority Critical patent/WO2010070716A1/fr
Publication of WO2010070716A1 publication Critical patent/WO2010070716A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
    • C07B63/00—Purification; Separation; Stabilisation; Use of additives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
    • B01D3/002—Processes specially adapted for distillation or rectification of fermented solutions by continuous methods
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • B01D5/003—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium within column(s)
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/06—Ethanol, i.e. non-beverage
    • C12P7/08—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate
    • C12P7/10—Ethanol, i.e. non-beverage produced as by-product or from waste or cellulosic material substrate substrate containing cellulosic material
    • 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

Definitions

  • the present invention relates to a method and an apparatus for producing ethanol in a technology for producing ethanol by saccharifying and fermenting biomass to prevent fermentation inhibition of ethanol-fermenting yeast and improve ethanol yield.
  • Bioethanol is produced by fermenting biomass as a measure for reducing carbon dioxide concentration in the atmosphere and depleting fossil fuels.
  • Bioethanol is vegetable ethyl alcohol produced by saccharification, fermentation and distillation of biomass resources such as sugarcane, cassava, corn, and waste wood, and has attracted attention as a new fuel energy.
  • FIG. 4 shows a conventional general bioethanol production apparatus.
  • Biomass is pulverized in advance, saccharified biologically or chemically to recover a liquid containing sugar, and this sugar-containing liquid is put into the fermentation tank 51.
  • an ethanol fermentation yeast is put into the fermentation tank 51 and fermented for a predetermined time to generate an ethanol solution.
  • ethanol fermentation is an exothermic reaction, a temperature rise in the fermentation tank 51 is observed.
  • the function of the yeast is reduced, so that the fermentation liquid in the fermentation tank 51 can be cooled. Necessary.
  • FIG. 4 shows a conventional general bioethanol production apparatus.
  • Biomass is pulverized in advance, saccharified biologically or chemically to recover a liquid containing sugar, and this sugar-containing liquid is put into the fermentation tank 51.
  • an ethanol fermentation yeast is put into the fermentation tank 51 and fermented for a predetermined time to generate an ethanol solution.
  • a temperature rise in the fermentation tank 51 is observed.
  • the function of the yeast is
  • a cooling line 52 is provided that pulls out the fermentation broth from the bottom of the fermentation tank 51 by the pump 53, cools the fermentation broth via a cooler 54 that indirectly cools the fermentation broth, and then returns it to the fermentation tank 51.
  • the fermentation broth is cooled and maintained at a temperature suitable for fermentation, so that the fermentation is stably performed.
  • Patent Document 1 Japanese Patent Laid-Open No. 2008-182925.
  • Patent Document 1 discloses a reactor that pressurizes and heats an aqueous slurry of biomass, hydrolyzes cellulose and cellulose contained in the biomass to produce sugar, and ethanol that ferments the produced sugar to produce ethanol.
  • a bioethanol production apparatus including a fermentation apparatus is disclosed.
  • An object of the present invention is to provide an ethanol production method and apparatus that can prevent ethanol fermentation inhibition, maintain a high ethanol yield, and efficiently produce ethanol in view of the above-described problems of the conventional techniques.
  • the present invention in an ethanol production method for producing ethanol by distilling a fermentation liquid after fermenting a sugar-containing liquid obtained by hydrolyzing biomass in a fermentation tank,
  • the temperature or ethanol concentration of the fermentation liquid in the fermentation tank is measured, and when the measured temperature or ethanol concentration exceeds a predetermined value, at least a part of the fermentation liquid is extracted from the fermentation tank, and the extracted fermentation liquid is Evaporating gas containing ethanol is separated by vacuum evaporation in a vacuum evaporator, and the residual liquid cooled by the vacuum evaporation and reduced in ethanol concentration is returned to the fermentation tank.
  • the temperature or ethanol concentration of the fermentation liquor in the fermentation tank is monitored, the fermentation liquor is withdrawn before reaching the temperature or ethanol concentration causing fermentation inhibition, the fermentation liquor is cooled by vacuum evaporation,
  • the cooling energy of a fermented liquid can be reduced and cost reduction can be aimed at.
  • the condensate containing condensed ethanol and the non-condensable gas are separated into gas and liquid, and the condensate is distilled to recover ethanol.
  • the evaporated gas generated by the vacuum evaporator ethanol having a higher concentration than the residual liquid exists. Therefore, the ethanol yield can be increased by cooling and condensing the evaporated gas to recover ethanol.
  • the non-condensable gas is brought into contact with water, ethanol in the non-condensable gas is transferred to the water side, and the ethanol-containing water obtained is distilled to recover ethanol.
  • This makes it possible to recover the ethanol remaining in the non-condensed gas after cooling the vaporized gas and separating it from gas and liquid, thereby further improving the ethanol yield.
  • an ethanol production apparatus comprising a fermentation tank for fermenting a sugar-containing liquid obtained by hydrolyzing biomass, and a distiller for distilling the fermentation liquid discharged from the fermentation tank, A circulation cooling line for extracting a part of the fermentation liquor in the fermentation tank and circulating it externally; A valve provided on the outlet side of the fermentation tank; A vacuum evaporator that is provided on the circulating cooling line and that separates the fermentation liquor by evaporating the fermentation liquid into an evaporating gas containing ethanol and a residual liquid cooled by the vacuum evaporating and having a reduced ethanol concentration; A temperature measuring means for measuring the temperature of the fermentation broth in the fermentation tank or a concentration measuring means for measuring the ethanol concentration; A controller that controls to circulate the fermentation broth on the circulating cooling line by opening the valve when the temperature or ethanol concentration measured by the temperature measuring means or the concentration measuring means exceeds a predetermined value. It is characterized by that.
  • a cooler for cooling the evaporative gas A gas-liquid separator that is vapor-liquid separated into a condensate containing ethanol condensed by cooling and a non-condensed gas introduced through the cooler, and The condensate is fed to the distiller. Furthermore, the non-condensable gas separated by the gas-liquid separator is introduced, and the non-condensable gas is brought into contact with water, and an absorption tower for transferring ethanol in the gas to the water side is provided. Ethanol-containing water obtained in the absorption tower is supplied to the distiller.
  • the controller is configured such that the temperature measured by the temperature measuring means is 32 ° C. or higher, or the ethanol concentration measured by the concentration measuring means is set to 6% or higher as a condition for opening the valve. It is characterized by.
  • the temperature of the fermentation broth is 32 ° C. or higher or the ethanol concentration is 6% or higher, fermentation inhibition tends to occur. Therefore, when the temperature or the ethanol concentration is exceeded, the fermentation broth is discharged onto the circulation cooling line, and the ethanol concentration is lowered and cooled by the vacuum evaporator, whereby the fermentation can be continued stably.
  • a heater is provided in front of the vacuum evaporator, and the fermentation broth is heated to a temperature set based on a gas-liquid equilibrium curve of ethanol.
  • the temperature set based on the vapor-liquid equilibrium curve of ethanol is the temperature at which ethanol most moves to the gas phase side when vacuum-evaporated with a vacuum evaporator.
  • the temperature or ethanol concentration of the fermentation liquid in the fermentation tank is monitored, the fermentation liquid is drawn out before reaching the temperature or ethanol concentration causing fermentation inhibition, and the fermentation liquid is cooled by vacuum evaporation.
  • the fermentation liquid is drawn out before reaching the temperature or ethanol concentration causing fermentation inhibition, and the fermentation liquid is cooled by vacuum evaporation.
  • the cooling energy of a fermented liquid can be reduced and cost reduction can be aimed at.
  • the ethanol yield can be increased by cooling and condensing the evaporated gas generated in the vacuum evaporator to recover ethanol. Furthermore, the ethanol yield can be further improved by absorbing and recovering ethanol remaining in the non-condensable gas after cooling and evaporating the vaporized gas.
  • 1 is an overall configuration diagram of an ethanol production apparatus according to an embodiment of the present invention. It is a graph which shows the relationship between the ethanol concentration in fermentation liquid, and fermentation time. 1 is an overall configuration diagram of an ethanol production apparatus to which an embodiment of the present invention is applied. It is a block diagram of the conventional ethanol manufacturing apparatus.
  • the ethanol production apparatus is equipped with a pretreatment device (not shown) in the preceding stage.
  • the pretreatment device pulverizes biomass as appropriate, hydrolyzes it at a predetermined temperature and a predetermined pressure with water, and contains sugar.
  • a liquid is produced.
  • This sugar-containing liquid is a raw material for the ethanol production apparatus.
  • the biomass is an organic substance resulting from photosynthesis, which is biomass such as woody material, vegetation, agricultural products, and moss, and in the present embodiment, is a plant resource that contains a large amount of sugar or starch. Is preferred.
  • the ethanol production apparatus includes a fermentation tank 1 in which a sugar-containing liquid 21 is charged and fermentation yeast is added thereto to perform ethanol fermentation.
  • the fermentation tank 1 is connected to a circulating cooling line 2 that draws out at least a part of the fermentation liquid in the tank, cools it, and returns it to the fermentation tank 1.
  • a valve 3 On the circulating cooling line 2, a valve 3 is provided on the outlet side of the fermentation tank 1, and a vacuum evaporator 4 is provided on the downstream side thereof.
  • the vacuum evaporator 4 is sucked by a vacuum pump (not shown) and the inside is maintained at a vacuum low pressure.
  • the vacuum evaporator 4 is preferably maintained at about 0.005 to 0.02 atm, more preferably about 0.01 atm.
  • the fermentation tank 1 is provided with a temperature sensor 15 for measuring the temperature of the fermentation broth in the tank and a concentration sensor 16 for measuring the ethanol concentration. Further, based on the measured values measured by the temperature sensor 15 and the concentration sensor 16, a controller 17 that performs opening / closing control of the valve 3 of the circulation cooling line 2 and a valve 19 provided on a discharge line 18 described later is provided. I have.
  • a discharge line 18 is connected to the lower part of the fermentation tank 1 for discharging the fermented liquor that has been fermented.
  • a valve 19 is provided at the tank outlet, and a distiller 20 is provided downstream thereof.
  • the distiller 20 is a device that distills the fermentation broth to remove impurities, and an ethanol concentrator (not shown) may be provided in the previous stage or subsequent stage of the distiller 20.
  • the evaporated gas generated in the vacuum evaporator 4 is discharged to a gas line 5 different from the circulation cooling line 2.
  • a cooler 6, a gas-liquid separator 7, a pump 8, and an ethanol absorption tower 9 are provided in this order from the upstream side.
  • the cooler 6 is a device that cools the evaporative gas by indirect cooling.
  • an ammonia cooler using ammonia as a refrigerant is used.
  • the gas-liquid separator 7 is a device that separates the condensate 22 that has been cooled by the cooler 6 and partially condensed and the non-condensable gas 23.
  • the ethanol absorption tower 9 is a device for introducing the non-condensable gas 23 and bringing the non-condensable gas 23 into contact with water to transfer ethanol in the gas to the water side and recover it.
  • water is sprayed from a plurality of nozzles installed at the upper side, brought into countercurrent contact with the non-condensable gas 23 introduced from the lower side to transfer ethanol to the water side, and CO 2 , O 2, etc. It is set as the apparatus which isolate
  • the ethanol-containing water 24 may be circulated on the circulation line 10 by the pump 11 and discharged when the ethanol concentration exceeds a predetermined concentration.
  • the condensate 22 condensed in the gas-liquid separator 7 contains a large amount of ethanol, it is led to the distiller 20 together with the fermentation liquid discharged from the fermentation tank 1 and recovered as ethanol. Similarly, the ethanol-containing water 24 discharged from the ethanol absorption tower 9 is also led to the distiller 20 to recover ethanol.
  • the sugar-containing liquid 21 obtained by hydrolyzing biomass is put into the fermentation tank 1 and fermented yeast is added and fermented for a predetermined time.
  • the valve 3 on the circulation cooling line 2 and the valve 19 on the discharge line 18 are set to be closed.
  • the temperature of the fermentation broth in the fermentation tank 1 is measured by the temperature sensor 15 and the temperature of the fermentation broth is monitored.
  • the controller 17 opens the valve 3 and discharges the fermented liquid to the circulation cooling line 2.
  • the temperature in the fermentation tank 1 when the valve 3 is opened is preferably 32 ° C. or higher.
  • bulb 3 was made into the temperature above, it is good also considering the ethanol concentration of the fermentation liquid in the fermentation tank 1 as an opening condition.
  • the ethanol concentration of the fermentation broth is measured and monitored by the concentration sensor 16, and the valve 3 is opened by the controller 17 when the concentration exceeds a predetermined ethanol concentration.
  • the ethanol concentration in the fermentation tank 1 when the valve 3 is opened is preferably 6% or more.
  • the fermentation liquor discharged to the circulation cooling line 2 is introduced into the vacuum evaporator 4.
  • the fermentation liquor brought to a low pressure state in the vacuum evaporator 4 is boiled and evaporated to obtain an evaporating gas and a residual liquid.
  • the evaporative gas contains ethanol having a concentration along the vapor-liquid equilibrium curve of ethanol, but the evaporated gas contains ethanol having a higher concentration than the residual liquid.
  • the evaporated gas contains CO 2 , O 2 and the like.
  • the residual liquid is cooled by vacuum evaporation and returned to the fermentation tank 1 through the circulation cooling line 2 in a state where the ethanol concentration is lowered.
  • the evaporated gas is discharged to the gas line 5 and introduced into the cooler 6 provided on the gas line 5.
  • the evaporative gas is cooled in the cooler 6 and is introduced into the gas-liquid separator 7 in a partially condensed state.
  • the gas-liquid separator 7 is separated into a condensate 22 containing condensed ethanol and a non-condensable gas 23 mainly composed of CO 2 and O 2 .
  • the non-condensable gas 23 is guided to the absorption tower 9 by the pump 8.
  • ethanol remaining in the gas moves to the water side and is recovered as ethanol-containing water 24.
  • the condensate 22 separated by the gas-liquid separator 7 and the ethanol-containing water 24 recovered by the absorption tower 9 are guided to the distiller 20 and recovered as high-concentration ethanol.
  • the circulation cooling line 2 closes the valve 3 by the controller 17 to stop the circulation of the fermentation broth.
  • the circulation stop condition may be ethanol concentration in addition to temperature.
  • fermentation is performed continuously.
  • the temperature in the fermentation tank 1 is monitored by the temperature sensor 15 in the same manner as described above, and when the temperature becomes equal to or higher than the predetermined temperature, the valve 3 on the circulation cooling line 2 is opened again to cool the fermentation broth.
  • the change in ethanol concentration in the fermentation tank 1 is monitored by the concentration sensor 16, and when no change is observed in the ethanol concentration, it is determined that fermentation has ended, and the controller 17 determines the discharge line 18.
  • the upper valve 19 is opened, the fermented liquid in the fermentation tank 1 is fed to the still 20 and high-concentration ethanol is recovered.
  • the temperature or ethanol concentration of the fermentation liquor in the fermentation tank 1 is monitored, the fermentation liquor is withdrawn before reaching the temperature or ethanol concentration causing fermentation inhibition, and the liquid is cooled and cooled by vacuum evaporation.
  • the ethanol concentration therein it is possible to prevent fermentation inhibition from occurring in the fermentation tank 1, to perform ethanol fermentation stably, and to improve the ethanol yield.
  • the cooling energy of a fermented liquid can be reduced and cost reduction can be aimed at.
  • FIG. 2 shows a graph comparing ethanol concentrations in the ethanol production apparatus of the present embodiment shown in FIG. 1 and the conventional ethanol production apparatus shown in FIG.
  • the horizontal axis in FIG. 2 is the fermentation time, and the vertical axis is the ethanol concentration.
  • the ethanol concentration in the fermentation liquid increases with time and increases to a concentration that causes fermentation inhibition.
  • the ethanol concentration does not exceed 6%. It has become. Therefore, the concentration does not become so high as to cause fermentation inhibition, and the fermentation can be performed stably, and the ethanol yield can be improved.
  • FIG. 3 shows an embodiment in which the ethanol production apparatus shown in FIG. 1 is applied.
  • This ethanol production apparatus has a configuration in which a heater 14 is provided in front of the vacuum evaporator 4 on the circulation cooling line 2.
  • the heater 14 is a device that heats the fermented liquid discharged from the fermentation tank 1 to the circulation cooling line 2 to a temperature set based on a gas-liquid equilibrium curve of ethanol.
  • the temperature set based on the vapor-liquid equilibrium curve of ethanol is the temperature at which ethanol moves most to the gas phase side when the vacuum evaporator 4 is used for vacuum evaporation.
  • the fermented liquid heated by the heater 14 is introduced into the vacuum evaporator 4, and evaporating gas containing ethanol is generated by vacuum evaporation.
  • the evaporative gas contains a higher concentration of ethanol than when the heater 14 is not installed.
  • the evaporative gas is cooled by the cooler 6 and then gas-liquid separated by the gas-liquid separator 7 to recover the ethanol. Is done.
  • the residual liquid from which the evaporated gas has been separated by the vacuum evaporator 4 is returned to the fermentation tank 1 via the circulation cooling line 2. According to this embodiment, more ethanol can be transferred to the evaporation gas side, and the ethanol concentration in the residual liquid returned to the fermentation tank 1 can be reliably reduced.
  • the present invention prevents ethanol fermentation inhibition, maintains a high ethanol yield, and can produce ethanol efficiently, it is suitably used for the production of bioethanol used for fuels and chemical raw materials.

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Abstract

La présente invention concerne un procédé de production d'éthanol qui permet d'empêcher la fermentation de l'éthanol tout en conservant un rendement élevé, et un appareil pour mettre en œuvre ce procédé. Le procédé consiste à fermenter un liquide contenant des sucres obtenus par saccharification biologique ou chimique d'une biomasse dans une cuve de fermentation (1), puis à distiller le liquide fermenté pour obtenir de l'éthanol. La température ou la concentration d'éthanol du liquide fermenté dans la cuve de fermentation (1) est mesurée avec une sonde de température (15) ou un capteur de concentration (16). Quand la température ou la concentration d'éthanol ainsi mesurée atteint une valeur prédéterminée, au moins une partie du liquide fermenté est retirée de la cuve (1). Le liquide fermenté retiré est introduit dans un évaporateur à vide (4) par une ligne de circulation refroidie (2). Le liquide fermenté est évaporé sous vide pour séparer ainsi le gaz évaporé contenant de l'éthanol. Enfin, le liquide résiduel qui a été refroidi et qui présente une concentration d'éthanol abaissée est retourné dans la cuve de fermentation (1).
PCT/JP2008/072733 2008-12-15 2008-12-15 Procédé et appareil pour la production d'éthanol Ceased WO2010070716A1 (fr)

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PCT/JP2008/072733 WO2010070716A1 (fr) 2008-12-15 2008-12-15 Procédé et appareil pour la production d'éthanol

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013183704A (ja) * 2012-03-09 2013-09-19 Oji Holdings Corp リグノセルロース系原料からのエタノール製造方法。
CN109852535A (zh) * 2019-04-01 2019-06-07 安徽逸能生物科技有限公司 一种生物发酵液提取系统
CN110455681A (zh) * 2019-09-06 2019-11-15 云南大唐汉方制药股份有限公司 一种龙血竭浓缩过程乙醇回收和浓度在线检测方法
CN115074208A (zh) * 2022-05-26 2022-09-20 厦门大学 一种搅拌型气升发酵罐及系统
IT202200010538A1 (it) * 2022-05-20 2023-11-20 Francesco Vitale Gruppo di evaporazione sottovuoto

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6211088A (ja) * 1985-07-08 1987-01-20 Hitachi Zosen Corp アルコ−ル濃縮法

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6211088A (ja) * 1985-07-08 1987-01-20 Hitachi Zosen Corp アルコ−ル濃縮法

Non-Patent Citations (2)

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Title
SABURO SHICHIJI: "Biseibutsu Kogaku no Oyo", 1 December 1972, KYORITSU SHUPPAN CO., LTD., pages: 110 - 112 *
SHADAN HOJIN KAGAKU KOGAKU KYOKAI: "Kagaku Sochi Binran", 30 March 1989, MARUZEN CO., LTD., pages: 431 - 432 *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2013183704A (ja) * 2012-03-09 2013-09-19 Oji Holdings Corp リグノセルロース系原料からのエタノール製造方法。
CN109852535A (zh) * 2019-04-01 2019-06-07 安徽逸能生物科技有限公司 一种生物发酵液提取系统
CN110455681A (zh) * 2019-09-06 2019-11-15 云南大唐汉方制药股份有限公司 一种龙血竭浓缩过程乙醇回收和浓度在线检测方法
IT202200010538A1 (it) * 2022-05-20 2023-11-20 Francesco Vitale Gruppo di evaporazione sottovuoto
CN115074208A (zh) * 2022-05-26 2022-09-20 厦门大学 一种搅拌型气升发酵罐及系统

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