JPS6066988A - Method for extraction and apparatus therefor - Google Patents

Abstract

PURPOSE:To extract valuable substances efficiently from a fermentation product, by using a liquefied gas as a solvent for extracting low-molecular weight organic compounds from the fermentation product. CONSTITUTION:A fermentation product solution 1 is pressurized with a pump 2 and mixed with liquefied carbon dioxide gas in a mixer 4 and made to flow in a separation tank 7, and valuable substances are transferred to the liquefied carbon dioxide gas during the process. Both liquids are separated at the interface 8 by the difference in specific gravity in the separation tank 7, and the resultant separated liquefied carbon dioxide gas 9 is decompressed by a valve 10, made to flow in an evaporation tank 11, heated by a heating member 12 and separated into the vaporized carbon dioxide gas and valuable substances 13.

Description

Detailed Description of the Invention [Field of Application of the Invention] The present invention relates to a method and apparatus for extracting valuable low-molecular organic compounds from fermentation products, and a related apparatus or apparatus for producing the compounds. Regarding the method.

[Background of the invention]

Conventionally, when producing valuables by fermentation, the fermented product contains various things such as bacterial cells and polymeric substances in addition to the valuables and the water plate. It was extremely difficult to extract valuables efficiently.

In addition, due to the rising cost of oil and the limited availability of oil resources, in recent years, ethanol production from pie and trout has been attracting attention as an alternative energy source to oil. Ethanol is produced from biomass, as well as from sawdust, rice straw, etc., which were previously treated as waste, so it is extremely promising as an energy solution for our country, which is poor in oil resources. .

Sawdust, rice straw, etc. (To produce lower alcohols from iomas, the cellulose in the material is enzymatically saccharified and then fermented, but the cellulose in the material is wrapped in lignin. It is necessary to remove this lignin.There are methods to remove this lignin, such as decomposition treatment with ozone, but a more effective delignification method is desired.

Next, the main problems in the fermentation process are (a) product inhibition (
(alcohol and carbon dioxide gas), (b) in the heat of reaction. the current,
The yeast used for alcoholic fermentation has a low tolerance to alcohol, so the alcohol concentration of the resulting fermented liquid is 8.
It is about 12%. Therefore, the search for bacteria with high alcohol concentration is underway.

Furthermore, in the case of ethanol, for example, alcoholic fermentation is said to proceed according to the reaction shown below.
2) Ethanol and the same mole of carbon dioxide gas are generated at the same time.

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.

The heat of reaction raises the temperature of the system and reduces yeast performance.

In order to reduce the number of germs in alcohol, it is considered important to search for microorganisms that can ferment even if the fermentation process, which is currently carried out at about 30°C, is raised to 45 to SOC.

In the concentration step, as mentioned above, the alcohol concentration of the fermented liquid is about 8 to 12 yen, so this is reduced to 95%.
In order to use it as fuel, it is necessary to concentrate it to 925% or more. Currently, the distillation method is used, but for example, even in the most advanced alcohol distillation plant, it takes 20.00 liters to distill 1 gap of ethanol from the fermentation stock solution.
Uses 0 Btu of energy. This accounts for 60 to 80q6 of the energy consumed in the entire process, and emphasis is placed on the development of a concentration technology that can replace distillation. However, when the alcohol is ethanol, when the ethanol concentration exceeds 95.6, an azeotropic phenomenon occurs between water and ethanol, and in order to obtain ethanol with a concentration of 95, 64 or higher, benzene azeotropic distillation is carried out. It made the operation complicated.

[Purpose of the invention]

The present invention has been 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 purpose is to provide an extraction wave M for effectively implementing the extraction method used with the extraction solvent Kt
).

A third object is to provide an apparatus for efficiently producing lower alcohols, especially ethanol, by the biomascara fermentation method using the extraction apparatus. The fourth objective is to provide a production method for efficiently producing valuable substances by combining the extraction with fermentation.

[Summary of the invention]

To summarize the present invention, the first invention of the present invention relates to an extraction method, and is characterized in that the method for extracting low molecular weight organic compounds from fermentation products is characterized in that the extraction solvent is a liquefied gas. do.

Further, a second invention of the present invention relates to an extraction device, which is an invention for extracting low-molecular-weight 15 organic compounds from a fermentation product using a liquefied gas. 1, to separate the liquefied gas liquid containing the low-molecular organic compound from the resulting mixture. I
tank, an evaporation tank that gasifies the liquefied gas from the separated liquefied gas liquid, a heat exchanger that liquefies the obtained gas, a circulation pump that sends the obtained liquefied gas to the mixer, and their connecting equipment. It is characterized by including each type of equipment.

And, the third invention of the present invention is an invention related to a lower alcohol production apparatus #, which is an apparatus for producing lower alcohol from biomass by a fermentation method.
Biomass delignification treatment tank, treated biomass saccharification fermentation tank, mixer for the obtained fermentation product and liquefied gas, separation tank for separating liquefied gas liquid containing lower alcohol from the obtained mixture, separation an evaporator that gasifies the liquefied gas from the liquefied gas liquid; a heat exchanger that liquefies the obtained gas; a circulation pump that sends the obtained liquefied gas to the mixer; a combustor for mixing the fuel gas from the exchanger with oxygen-containing gas and combusting it; a means for introducing water into the combustor to generate water vapor during heat exchange; It is characterized in that it includes means for introducing the lignin into the lignin treatment tank and equipment for connecting them.

Finally, the fourth invention of the present invention is an invention relating to a method for producing a chemical compound, which is a method for producing a low molecular weight organic compound by a fermentation method involving the generation of carbon dioxide, in which carbon dioxide is liquefied carbon dioxide. Perform two fermentations under pressure and temperature moxibustion conditions to produce gas or supercritical carbon dioxide, and extract nuclear low-molecular low organic compounds from the fermentation product in the same fermenter with the liquefied carbon dioxide or induced critical carbon dioxide, f: It is characterized by including a step of shrinking and separating by %.

First, examples of liquefied gases that can be used in the present invention include liquefied gases such as Tetris, methane, ethane, ethylene, ammonia, and chlorofluorocarbons, liquefied carbon dioxide, and stone-critical carbon dioxide or ethane gas, which are harmless and 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 more than the critical m1 pressure and more than the critical pressure, are suitable. Therefore, the following explanation will be made using these carbon dioxide gases as examples.

In addition, the low molecular weight organic compounds which are the object of the present invention include alcohols such as ethanol, butanol, polyhydric alcohols such as 2,3-butylene glycol and glycerin, and ketones having a molecular weight of up to about 150. Acetone, aldehydes such as acetaldehyde. There are also sugars, organic acids, etc., but these are not suitable because they are insoluble in liquefied carbon dioxide gas and supercritical carbon dioxide gas.

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. In addition, enzymes and microorganisms are insoluble in liquefied carbon dioxide gas and can be separated (sedimented).
The extraction solvent is useful. It is also advantageous in that it has a large boiling point difference with the extract.

Next, the extraction device which is the second invention of the present invention will be explained.

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.

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 the high-pressure liquid flowing out from the separation tank is used to rotate a water turbine, and the circulation pump is driven by the power generated by the water turbine.

In addition, as a method of transmitting the power of the turbine to the boost pump, is it possible to use a blower run shaft that is directly connected to the turbine and the pump, or to use the power generated by the turbine? The method of transmitting power is not limited to a specific method, such as converting it into electric power with a generator and then supplying the electric power to an electric motor connected to the pump to rotate the pump.

As mentioned above, the extraction device vll'i of the present invention is particularly preferably used when ethanol is extracted from a fermentation product using liquefied carbon dioxide gas.

Next, a third invention of the present invention, an apparatus for producing a lower alcohol by a fermentation method from pimemus, will be explained.

The process for producing lower alcohols from biomass generally consists of the following steps: (1) thick phase → (2) pretreatment → (3) saccharification → (4) fermentation → (5) concentration → (6) product.

As outlined above, the apparatus for producing lower alcohols, such as ethanol or butanol, particularly ethanol, according to the third aspect of the present invention, comprises the above-mentioned extraction apparatus, which is the second aspect of the present invention, and a delignification treatment tank. It is characterized by the combination of

In the production apparatus of the present invention, the liquefied gas that is 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 a fuel to generate water vapor at around 500° C., and delignification treatment 2 is carried out using the wet oxidation method. The water source of this steam may be prepared in any manner.

For example, the evaporator may include a heating section built into the evaporation tank, a means for causing water to flow through the heating section, and passing the water into the combustor to generate 11 kg iA. It is preferred for this device.

Examples of liquefied fuel gas include LNG and LPG.

Finally, a method for producing a low molecular weight 6'' organic compound, which is the fourth aspect of the present invention, will be explained.

The main point of the fourth aspect of the present invention is that, as outlined above, fermentation and the extraction of a low molecular weight organic compound, which is a target valuable product, from the fermentation product with liquefied carbon dioxide gas or supercritical carbon dioxide gas are performed in the same manner. The point that it is done in parallel within the facility is +ci. Therefore, the target low molecular weight organic compound must be soluble in the liquefied carbon dioxide gas or supercritical carbon dioxide gas.

So, the above-mentioned over-fermented T? Regarding the problem of product inhibition in (a), a simple solution to I)) is to remove the generated f (inhibitor, such as alcohol, from the system, and prevent the inhibitor ij3 from increasing). This enables continuous operation and maximizes the functions of microorganisms.According to the present invention, the inhibitors are dissolved in liquefied carbon dioxide or supercritical carbon dioxide. In particular, it is taken out of the system.Next, in addition to the heat of reaction in (b), carbon dioxide gas is produced during the fermentation process and can be liquefied at room temperature and under high pressure. Since fermentation can be carried out at around room temperature, the effect on microbial function is extremely small.Furthermore, regarding pressure, generally speaking, the effect of pressure on the fermentation function of microorganisms is due to the reaction system being exposed to gas. It is thought that the amount is small unless it involves giving and receiving. Carbon dioxide is produced in the fermentation process of the present invention, so if the concentration becomes high, the fermentation reaction will not proceed. Therefore, the solubility of liquefied carbon dioxide in water is It becomes a problem.

Therefore, the present inventors measured the mutual solubility of water and liquefied carbon dioxide.

Measurements were carried out at 21° C. and 57 atg using an SOS pipe (inner diameter 10.8, length 400 watts). As a result, the solubility of water in liquefied carbon dioxide (9 of water/2 of liquefied carbon dioxide) was 0.0013. On the other hand, the solubility of liquefied carbon dioxide in water (2 of liquefied carbon dioxide/-y of water) was 0.00077. This value of 0.00077 means that the degree of solubility of carbon dioxide at atmospheric pressure and 25°C is 0.0.
01446, which is extremely small. Furthermore, in the fluidized bed type Alfur fermentation plant, the carbon dioxide gas produced in the bioreactor is recycled and used for agitation within the 411 chamber, so the effect of high pressure is estimated to be small.

Furthermore, since the above value of 0.0013'ii is extremely small, the desired product can be obtained at a high concentration.

In the fourth aspect of the present invention, extraction may be performed using only the produced carbon dioxide, but fermentation may be performed by adding liquefied carbon dioxide gas or supercritical carbon dioxide gas. Furthermore, the method may include a step of gradually vaporizing and separating the liquefied carbon dioxide gas or supercritical carbon dioxide from the liquid containing the separated low-molecular compound. This separation step is easy due to the large difference in boiling points.

[Embodiments of the invention]

Hereinafter, the present invention will be explained in detail with reference to Examples, but the present invention is not limited to these Examples.

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.

Example 1 In an example of the extraction apparatus of the present invention shown in FIG. 1, 2 is a pump, 4 is a mixer, 7 separation tanks, 8 fermentation product liquids, and a liquefied carbon dioxide liquid containing the target product. interface with, 10
11 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.

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 gas are transferred to the separation tank 7, valuable substances in the solution are transferred to the liquefied carbon dioxide gas in the mixer and tube 6. By allowing a certain amount of residence time in the separation tank 7, the solution and liquefied carbon dioxide gas are separated into a solution that does not contain valuable substances and a liquefied carbon dioxide gas that contains them, due to the difference in specific gravity between the solution and the liquefied carbon dioxide gas. 8 in the separation tank indicates the interface between both liquids. In a solution such as water where the ratio of liquefied carbon dioxide is greater than 1F, the solution is in the lower part, while the liquefied carbon dioxide is in the upper part. The separated liquefied carbon dioxide gas passes through pipe 9 and enters valve 1.
The pressure is reduced by 0, and 151 fi people enter the evaporation tank 11.

There is a heating member 12 in the evaporation tank, and due to pressure reduction by the valve 10 and heating by the heating part H, the liquefied carbon dioxide gas is vaporized, and the valuables 13 dissolved in the liquefied carbon dioxide gas are liquefied in the lower part of the evaporation tank. and are separated. This valuable material 13 exits the yarn through a pipe 14 and a valve 15.

Valuables are used as products. On the other hand, the carbon dioxide gas vaporized in the evaporation tank flows through the pipe 16fr: into the heat exchanger 17, where it is completely cooled down and becomes liquefied carbon dioxide gas, which is then passed through the pipe 18,
It flows into the mixer 4 from the pipe 5 via the pump 19, the pipe 20, and the valve 21.

In addition, the high-pressure liquid from which valuable substances have been removed in the separation tank is transferred to the pipe 22.
The water passes through the water, enters the water turbine 23, rotates the turbine, and then exits the system through the pipe 24. The power from the turbine 23 becomes the power for rotating the pump 19. Furthermore, 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, it exchanges heat with the liquefied carbon dioxide flowing out from the pipe 9. When the temperature drops, it flows out through the pipe 26. Heat exchanger 17 has pipe line 2
Cooling water flows in from 7, where it indirectly exchanges heat with carbon dioxide gas, liquefies the carbon dioxide gas, and flows out through pipe 28. The cooling water from pipe 27 is piped! When it flows out from 828, the temperature rises corresponding to the liquefaction heat amount of the carbon dioxide gas, and it flows out.

In addition, if the specific gravity of the solution is smaller than the specific gravity of liquefied carbon dioxide, the upper part of the boundary surface 8 in the separation tank is the bath liquid, and the lower part is the liquefied carbon dioxide gas phase. It is provided in the gas phase, and the t7 passage 22 needs to be provided above the interface 8.

Example 2 FIG. 2 illustrates an apparatus for producing ethanol from biomass. In Figure 2, the symbol 2.4.5.7.8.10
~14.16~19.23~26 are the same as in Figure 1, 31 is biomass material, 32 is a crusher, 33&i delignification treatment tank, 34 is a saccharification fermentation tank, 57 is a combustion vessel, 3
9 Heat exchanger tubes, others mean pipes.

311d - A cellulosic biomass material such as Saiki M, Web et al., 32 is a crushing process performed on materials that require crushing, such as rice straw, and 33 is a wet oxidation process that performs 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, turning sugar into ethanol. The concentration of ethanol here is 1 due to the characteristics of fermentation engineering.
The punch size is 0%. The ethanol solution having a concentration of about 10% is pressurized by the pump 2 and enters the mixer 4. Here, it comes into contact with the liquefied carbon dioxide gas that has been pressurized by the circulation pump 19, and the ethanol component moves into the liquefied carbon dioxide gas, and the ethanol component is transferred to the separation tank 7.
The liquid is separated into liquefied carbon dioxide gas and a liquid that does not contain ethanol. Line 8#-i in separation tank 7: indicates the boundary line between liquefied carbon dioxide gas and a liquid not containing ethanol, and the upper part is the liquefied carbon dioxide phase. The liquefied carbon dioxide gas that enters the evaporation tank 11 from the tank 7 through the valve 1o is vaporized by being depressurized by the valve 10 and heated by the heating member 12 built into the evaporation tank 11, and the liquefied carbon dioxide gas becomes gas. The ethanol 13 dissolved in the liquefied carbon dioxide gas is separated from the vaporized carbon dioxide gas while remaining as a liquid. This separated ethanol exits the system through a pipe 14t and becomes a product. This ethanol has a purity of approximately 99% and is immediately used as a product. The vaporized carbon dioxide gas passes through the pipe 16 and enters the heat exchanger 17, where it is converted into LNG supplied from the pipe 35.
(liquefied natural gas) is cooled and liquefied,
, pump 19 and enters mixer 4 through line 5. The natural gas vaporized in the heat exchanger 17 (is transferred from the pipe 36 to the combustor 37
In this step, the water is mixed with air from the pipe 38 and combusted, and the water flowing through the heat transfer pipe 39 built into the combustor is heated.
Water vapor. This water vapor is supplied to the wet oxidation process 33 via the pipe 4o. On the other hand, heat transfer tube 39Fj heat in the combustion chamber?
The stolen combustion gas is discharged out of the system through the pipe 41. Tap water, which serves as a heating source, is supplied from a pipe 25 to a heating unit 12 built in the evaporation tank 11, flows out from a pipe 26, and enters a heat exchanger 57.

Due to the nature of carbon dioxide gas, the gas temperature in the evaporator is approximately 10°C, and the pressure is approximately 42 atm and 8°C.

In addition, high pressure (approximately 45 to
After the liquid (s Oatm ) generates power in the water turbine 23, it flows out of the system through the pipe 24. water turbine 2
The power generated in step 3 is used as a power source for the pump 19.

Example 3 FIG. 3 illustrates the steps of an ethanol fermentation and extraction process which is an example of the fourth invention 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, a liquefied carbon dioxide gasification tank 55, a condenser 56, and the like. carbohydrate system,
A fermentation stock solution obtained from starch-based and cellulose-based raw materials is continuously supplied to a fermentation tank 54 by a pump 52. Although the fermentation tank is exemplified as being filled with immobilized microorganisms 54', the present invention is not limited thereto. Fermentation tank 54tj: For example, the temperature is adjusted to 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. At this time, carbon dioxide gas is liquefied. Since ethanol and carbon dioxide gas occur at the same point, ethanol can be efficiently dissolved into liquefied carbon dioxide gas. The density of liquefied carbon dioxide gas is about 0.8, and the density of the fermentation liquid is 0.98 considering that it is a 10% ethanol aqueous solution, so the generated liquefied carbon dioxide gas rises while dissolving ethanol. On the other hand, the fermentation liquid descends. If the fermentation is temporary and insufficient, some or all of the fermentation liquid should be removed from the pump 5.
Circulate by 3. 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 is collected at the bottom of the liquefied carbon dioxide gasification tank 55 and then taken out. On the other hand, the carbon dioxide gas is transferred to the condenser 56 to become 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 ferment and decompose the ethanol that could not be completely dissolved by the produced liquefied carbon dioxide gas, and to prevent the temperature from rising due to reaction heat and maintain the temperature inside the fermentation tank at a predetermined value.

In addition, since the immobilized microorganism is one in which 1 VC microorganism is immobilized in a gelatinous material, the above-mentioned filling rate into the fermentation tank 54 can be completely increased.

So far, the method of filling the fermentation tank with immobilized microorganisms has been described, but it goes without saying that fermentation may be carried out in the fermentation tank using a normal fluidized bed method.

Example 4 Ethanol fermentation was carried out using supercritical carbon dioxide instead of liquefied carbon dioxide in Example 3.

Figure 4 shows the process diagram. In Figure 4, 51-5
4' has the same meaning as in FIG. 3, 5711-]: supercritical carbon dioxide gasification tank, 58 means a compressor, and 59 means a temperature regulator.

In this example, 54 fermentation tanks were used, and the temperature was adjusted to about 73 atm at room temperature. 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-thiethanol 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 gas is transferred to a compressor 58, and then converted into supercritical carbon dioxide gas at an appropriate temperature by a temperature regulator 59. Other steps are the same as in Example 3.

〔Effect of the invention〕

As described above in detail, according to the present invention, low molecular weight compounds can be efficiently extracted from fermentation products. And that? In particular, if applied to the production of ethanol by fermentation, the energy conventionally required for distillation can be significantly reduced. For example, if you calculate the energy required for fermentation and concentration (extraction) from the heat and power required for fermentation and concentration (extraction), it is 9,500 yen using the normal distillation method.
, about 5,500 mJ using the latest distillation method, but 1,500 mJ when using liquefied carbon dioxide gas during fermentation using the method of the present invention.
m, T weighing results in significant energy savings. In addition, the remarkable effects of mutual dissolution with the fermentation liquor (in the evening) are small, and separation of ethanol and liquefied gas is easy.

[Brief explanation of the drawing]

FIG. 1 is a system diagram of an example of the extraction apparatus of the present invention, FIG. 2 is a system diagram of an apparatus according to the present invention for producing and directing lower alcohols from biomass, and FIGS. 6 and 4 are the system diagrams of the present invention. It is a process diagram of an example of the ethanol manufacturing method by. 4: Mixer, 7: Separation tank, 11: Evaporation tank, 17: Heat exchanger, 23: Water turbine, 33: Delignification tank, 34
: Saccharification fermentation tank, 67: Combustor, 54: Fermentation tank, 54
': Filled layer (immobilized microorganisms), 55: Liquefied carbon dioxide gasification tank, 56: Condenser, 57: Supercritical carbon dioxide gasification tank, 58: Compressor, 59: Temperature regulator% Applicant Hitachi, Ltd. Agent Hiroki Nakamoto / Figure 3 Figure η

Claims (1)

[Scope of Claims] 1. A method for extracting low molecular weight organic compounds from fermentation products, characterized in that the extraction solvent is a liquefied gas. λ The extraction method according to claim 1, wherein the liquefied gas is liquefied carbon dioxide gas or supercritical carbon dioxide gas. 5. The extraction method according to claim 1 or 2, wherein the low molecular weight organic compound is a low molecular weight alcohol. 4. An apparatus for extracting a low molecular weight organic compound from a fermentation product using a liquefied gas, which includes a mixer for the fermentation product and the liquefied gas, and a liquefied gas liquid containing the low molecular weight organic compound from the resulting mixture. a separation tank that separates the 475 liquefied gas, an evaporation tank that gasifies the liquefied gas from the separated liquefied gas liquid, a heat exchanger that liquefies the obtained gas, a circulation pump that sends the obtained 475 liquefied gas to the mixer, and An extraction device characterized by including each of the facilities of those connected devices. 5. The extraction device according to claim 4, which includes equipment for rotating a water turbine using the high-pressure liquid flowing out from the separation tank, and driving the circulation pump using the power generated by the water turbine. & An apparatus for producing lower alcohol from biomass by a fermentation method, which includes a biomass delignification treatment tank, a saccharification fermentation tank for the treated biomass, a mixer for the obtained fermentation product and liquefied gas, and a a separation tank that separates a liquefied gas liquid containing lower alcohol from a mixture of alcohols, an evaporation tank that gasifies the liquefied gas from the separated liquefied gas liquid, a heat exchanger that liquefies the obtained gas, and a heat exchanger that liquefies the obtained liquefied gas. A circulation pump for feeding the liquefied fuel gas into the mixer, a means for introducing the liquefied fuel gas into the heat exchanger, a combustor that mixes the fuel gas from the exchanger with oxygen-containing gas and combusts it, and introduces water into the combustor. An apparatus for producing lower alcohols, comprising means for generating steam by heat exchange, means for introducing the obtained steam into the delignification treatment tank, and equipment for connecting these. 7. The lower alcohol production apparatus according to claim 6, which includes equipment that uses the high pressure liquid flowing out of the separation tank to drive a water turbine all the time, and drives the circulation pump with the power thereof. a. Claim 6, which includes equipment such as a heating section built into the evaporator, and means for causing water to flow through the heating section and introducing the water into the combustor to generate steam. Or the lower alcohol production apparatus according to item 7. 9. In a method for producing low molecular weight organic compounds by a fermentation method accompanied by the generation of carbon dioxide, fermentation is carried out under pressure and temperature conditions where carbon dioxide becomes liquefied carbon dioxide or supercritical carbon dioxide, and fermentation is carried out in the same fermenter. A method for producing a low molecular weight organic compound, which comprises a step of extracting, concentrating and separating the low molecular weight organic compound from the fermentation product using the liquefied carbon dioxide gas or supercritical carbon dioxide gas. 10. The method for producing a low molecular weight organic compound according to claim 9, wherein the fermentation is carried out by adding liquefied carbon dioxide gas or supercritical carbon dioxide gas. 11. Claim 9 or 10, which includes the step of gasifying and separating the liquefied carbon dioxide or supercritical carbon dioxide from the separated liquid containing the low molecular weight organic compound.
A method for producing a low molecular weight organic compound as described in Section 1.