JP5778949B2 - Hydrogen methane fermentation equipment - Google Patents

Description

  The present invention relates to a hydrogen methane fermentation apparatus and a hydrogen methane fermentation method.

  If biomass such as food waste, livestock manure, sewage sludge, and food waste is subjected to anaerobic fermentation, a combustible biogas mainly composed of methane and carbon dioxide is finally generated. The use of biogas is attracting attention from the viewpoint of preventing environmental pollution and regenerating energy.

  Anaerobic fermentation of biomass proceeds in stages with hydrolysis, hydrogen fermentation, and then methane fermentation. For both hydrogen fermentation and methane fermentation, the optimum temperature is around 35 ° C. or around 55 ° C., but other optimum conditions differ between hydrogen fermentation and methane fermentation. For example, the optimum pH for hydrogen fermentation is as low as 4.5 to 6.5, whereas the optimum pH for methane fermentation is as high as 6.5 to 8.5. This is because the microorganism groups involved in hydrogen fermentation and methane fermentation are different. The optimum residence time (HRT) for hydrogen fermentation is as short as about 2 days, whereas the optimum HRT for methane fermentation is as long as 10 to 30 days. For this reason, it is better to control each fermentation condition of hydrogen fermentation and methane fermentation in two-phase fermentation in which hydrogen fermentation and methane fermentation are separately performed in two tanks than in single-phase fermentation in which anaerobic fermentation is performed in a single tank. Fermentation efficiency is good.

  However, the two-phase fermentation using two tanks requires one extra fermenter than the single-phase fermentation using a single tank, and therefore requires extra space. Since the number of pipes increases, the cost on equipment increases.

  Patent Documents 1 to 3 describe a single tank single-phase fermentation apparatus, and Patent Document 4 describes a two tank two-phase fermentation apparatus. All have stirring means for making the fermentation liquid in the tank uniform. As a stirring method, there are mechanical stirring using a rotary blade (Patent Documents 1 and 2), circulating stirring using a pump (Patent Document 3), and gas stirring using a blower. The single-phase fermentation apparatus has a problem that the fermentation efficiency is worse and the HRT is longer than the two-phase fermentation apparatus, so that the stirring power per unit fermentation liquid is large and the fermentation cost increases.

  Incidentally, Non-Patent Document 1 and Patent Documents 5 to 8 describe that in hydrogen fermentation, the efficiency of hydrogen fermentation increases and the recovery rate of hydrogen gas increases by lowering the hydrogen partial pressure in the fermentation broth. Has been. However, all of these methods require a device for reducing the hydrogen partial pressure, such as a decompression device, an aeration device, and a hydrogen gas separation device.

JP 2002-219485 A JP 2006-305491 A JP 2007-111633 A JP 2007-289946 A JP 07-031484 A JP 2005-125149 A JP 2003-135088 A JP 2003-251312 A

Kono et al., “Water and Wastewater”, Industrial Water Research Committee, 2005, Vol. 47, No. 9, pp. 777-783

  An object of this invention is to provide the apparatus and method for performing hydrogen fermentation and methane fermentation efficiently.

  The present invention provides a hydrogen methane fermentation apparatus for performing hydrogen fermentation and methane fermentation in conjunction with each other, and the apparatus is connected to a single tank fermenter and the fermenter to supply biomass into the fermenter. Biomass supply means for connecting to the fermenter, biogas recovery means for recovering the biogas generated in the fermentor outside the fermenter, and generating in the fermenter connected to the fermenter Fermentation residue collecting means for collecting the fermentation residue outside the fermenter is provided, and the fermenter is a porous partition that separates the inside of the fermenter into an upper part and a lower part, and the inside of the upper part and the lower part is stirred. And a transfer means for transferring the fermentation broth in the upper part into the lower part.

  In one embodiment, the fermenter is in the shape of a cylinder and the ratio of the cylinder height to diameter is 2: 1 to 4: 1.

  In one embodiment, the cylinder has a height of 8-12 m.

  In one embodiment, the ratio of the distance between the lower end surface and the upper end surface of the fermenter and the distance between the lower end surface of the fermenter and the partition wall is 10: 7 to 10: 8.

  In one embodiment, the internal diameter of the hole of the said partition is 50-100 mm.

  In one embodiment, the stirring means is selected from the group consisting of a rotor blade, a blower and a pump.

  The present invention also provides a method for performing hydrogen fermentation and methane fermentation in conjunction with each other, wherein the method continuously or intermittently supplies biomass into the apparatus, and hydrogen fermentation and methane are produced in the apparatus. A method comprising continuously performing fermentation, and continuously or intermittently collecting biogas and fermentation residue from within the apparatus.

  In one embodiment, the inside of the said fermenter is stirred by blowing the biogas collect | recovered at the said process in the said fermenter.

  In one embodiment, the fermenter is stirred by blowing the gas remaining after separating the hydrogen gas from the biogas recovered in the above step into the fermenter.

  ADVANTAGE OF THE INVENTION According to this invention, the apparatus and method for performing hydrogen fermentation and methane fermentation efficiently can be provided. Since the apparatus of the present invention includes a single fermenter, the production cost can be reduced.

It is a schematic diagram which shows one embodiment of the hydrogen methane fermentation apparatus of this invention. It is a schematic diagram which shows one embodiment of the hydrogen methane fermentation apparatus of this invention. It is a schematic diagram which shows one embodiment of the hydrogen methane fermentation apparatus of this invention. It is a schematic diagram which shows one embodiment of the hydrogen methane fermentation apparatus of this invention.

  In this specification, biomass refers to organic resources derived from living organisms. Examples of biomass include organic wastes, resource crops, or wastes thereof. Examples of organic waste include organic wastewater in food waste, manure, sewage sludge, food processing residue, food industry, paper industry, livestock industry, etc. Not. Examples of resource crops include corn, sugar cane, and waste generated in these treatment steps. As biomass, what removed the foreign material which does not contribute to fermentation, such as plastic and glass contained in biomass, may be used.

  In the present specification, the biogas refers to a gas generated by fermentation (anaerobic fermentation) of biomass. Examples of biogas components include hydrogen gas, methane gas, and carbon dioxide gas.

  In this specification, performing hydrogen fermentation and methane fermentation in conjunction with each other usually means performing hydrogen fermentation and methane fermentation separately, but performing fermentation under conditions where there is a certain mass transfer between them. . Therefore, neither hydrogen fermentation nor methane fermentation is performed in stages, nor is hydrogen fermentation and methane fermentation performed under uniform conditions in a complete mixing tank.

  The hydrogen methane fermentation apparatus and the hydrogen methane fermentation method of the present invention will be described with reference to the drawings.

(Hydrogen methane fermentation equipment)
FIG. 1 is a schematic view showing an embodiment of the hydrogen methane fermentation apparatus of the present invention. The apparatus shown in FIG. 1 is connected with the fermenter 1 of a single tank, the biomass supply means 2 for connecting with the fermenter 1 and supplying the biomass 71 in the fermenter 1, the fermenter 1 The biogas recovery means 3 for recovering the biogas 72 generated inside the fermenter 1 and the fermentation residue 73 connected to the fermenter 1 and generated inside the fermenter 1 are out of the fermenter 1. Fermentation residue collecting means 4 for collecting is provided, and the fermenter 1 stirs the interior of the porous partition wall 13 separating the fermenter 1 into an upper part 11 and a lower part 12, and the upper part 11 and the lower part 12, respectively. And a transfer means 15 for transferring the fermentation liquor in the upper part 11 into the lower part 12.

  The movement of the substance in the apparatus shown in FIG. 1 is as follows. Biomass is supplied into the fermenter 1 by the biomass supply means 2. In the fermenter 1, hydrogen fermentation is mainly performed in the upper part 11 and methane fermentation is mainly performed in the lower part 12 by the microorganisms in the fermenter using biomass as a substrate. A part of the fermentation broth in the upper part 11 is transferred into the lower part 12 by the transfer means 15. Thereby, the upward flow of a fermentation liquid arises in the fermenter 1. FIG. Since the porous partition wall 13 is porous, it does not block the upward flow. In hydrogen fermentation, hydrogen gas and carbon dioxide gas are generated, and in methane fermentation, methane gas and carbon dioxide gas are generated. In the upper part 11, there is a gas phase in which no fermentation liquid exists. A mixed gas composed of hydrogen gas and carbon dioxide generated in the upper part 11 is recovered outside the fermenter 1 by the biogas recovery means 3 through a gas phase located in the upper part of the upper part 11. A mixed gas composed of methane gas and carbon dioxide gas generated in the lower part 12 passes through the pores of the porous partition wall 13 along with the rising flow of the fermentation broth and rises in the fermenter 1, and then the gas phase above the upper part 11. After that, the biogas recovery means 3 recovers the fermenter 1 outside. When the mixed gas generated in the lower part 12 rises in the upper part 11, the fermentation liquid is aerated, the hydrogen partial pressure in the fermentation liquid is lowered, and the fermentation efficiency of hydrogen fermentation is increased. The fermentation residue is recovered outside the fermenter 1 by the fermentation residue recovery means 4.

  The shape of the fermenter 1 is not particularly limited, but is preferably a cylindrical shape. More preferably, it is a vertically long shape, and more preferably the ratio of the height and diameter of the cylinder is 2: 1 to 4: 1. By adopting such a shape, the mass transfer in the vertical direction in the fermenter 1 is restricted, a vertical concentration distribution is generated, and hydrogen fermentation in the upper part 11 and methane fermentation in the lower part 12 are performed in parallel.

  Although the magnitude | size of the fermenter 1 is not specifically limited, In the case of a cylinder shape, a diameter is 3.6 m at the maximum, and the height of a cylinder becomes like this. Preferably it is 8-12 m. By setting it as such a magnitude | size, the fermenter 1 can be laid down and it can mount on the loading platform of a truck.

  The porous partition wall 13 serves to limit, but does not block, the mass transfer between the upper part 11 and the lower part 12. The position of the porous partition wall 13 is not particularly limited, but preferably the ratio of the distance between the lower end surface and the upper end surface of the fermenter 1 and the distance between the lower end surface of the fermenter 1 and the porous partition wall 13 is 10: 7 to 10: 8. This is because the HRT for hydrogen fermentation is about 2 days and the HRT for methane fermentation is 10 to 20 days.

  Although the internal diameter of the hole of the porous partition wall 13 is not specifically limited, Preferably it is 50-100 mm. By setting it as such an internal diameter, the mass transfer between the upper part 11 and the lower part 12 is restrict | limited, but the upward flow of a fermentation liquid is not interrupted | blocked. Further, the solid matter in the biomass can move into the lower portion 12 without being caught in the holes of the porous partition wall 13.

  The stirring means is not particularly limited. As a stirring means, a rotary blade, a pump, and a blower are mentioned, for example. The rotary blade is used for mechanical stirring, the blower is used for gas stirring, and the pump is used for circulating stirring.

  The stirring means shown in FIG. The shape and size of the rotor blade are not particularly limited. The attachment position in the fermenter 1 of the rotary blade 14 is not specifically limited. FIG. 1 shows an embodiment in which the axis of the rotary blade 14 is mounted so as to be located at the center of the cylindrical shape of the fermenter 1. FIG. 4 shows an embodiment in which the shaft of the rotary blade 14 is attached to the cylindrical side surface of the fermenter 1 as a stirring means in the lower part 12.

  The stirring means in the upper part 11 shown in FIGS. The blower 16 sucks biogas from the gas phase above the upper portion 11 and discharges it into the fermentation broth in the upper portion 11. The fermentation liquor is aerated by discharging the biogas. FIG. 3 shows an embodiment in which a hydrogen gas separation membrane 17 is provided in the middle of the piping of the blower 16. By discharging the hydrogen gas 74 separated from the biogas by the hydrogen gas separation membrane 17 into the fermentation broth in the upper portion 11, the fermentation broth is aerated and the hydrogen partial pressure in the fermentation broth is reduced. Fermentation efficiency of hydrogen fermentation increases.

  The transfer means 15 is not particularly limited as long as the fermentation broth in the upper part 11 can be transferred into the lower part 12. Preferably a pump is used. The attachment position in the fermenter 1 of the transfer means 15 is not specifically limited as long as the fermentation liquid in the upper part 11 can be transferred into the lower part 12. Preferably, it attaches outside the fermenter 1 so that the flow of the culture solution in the fermenter 1 is not affected. The attachment position in the upper part 11 is preferably in the vicinity of the upper side of the porous partition wall 13. The attachment position in the lower part 12 is preferably near the upper side of the lower end surface of the fermenter 1.

  The biomass supply means 2 is not particularly limited as long as biomass can be supplied into the fermenter 1. The attachment position in the fermenter 1 of the biomass supply means 2 is not specifically limited as long as it is the upper part 11 of the fermenter 1.

  The biogas recovery means 3 is not particularly limited as long as biogas generated by fermentation in the fermenter 1 can be recovered outside the fermenter 1. Although the attachment position in the fermenter 1 of the biogas collection | recovery means 3 is not specifically limited, It attaches to the position which can collect | recover biogas from the upper gas phase in the upper part 11 of the fermenter 1. FIG.

  The fermentation residue collection means 4 is not particularly limited as long as the fermentation residue generated by fermentation in the fermentation tank 1 can be collected outside the fermentation tank 1. The attachment position of the fermentation residue collection means 4 in the fermentation tank 1 is not particularly limited as long as it is below the porous partition wall 13.

(Hydrogen methane fermentation method)
In the method of the present invention, biomass is continuously or intermittently supplied into the apparatus, hydrogen fermentation and methane fermentation are continuously performed in the apparatus, and biogas and fermentation residue are continuously supplied from the apparatus. Or the process of collect | recovering intermittently is included.

(Biomass supply)
The biomass is adjusted to an appropriate water content (˜90%) and the temperature is adjusted. The temperature adjustment is preferably in either the intermediate temperature range (30 to 40 ° C.) or the high temperature range (50 to 60 ° C.), but may be any. The biomass thus adjusted is continuously or intermittently supplied into the upper portion 11 of the fermenter 1 by the biomass supply means 2. The supply speed is not particularly limited. When supplying intermittently, supply and supply stop are repeated every few hours.

(Hydrogen fermentation)
Hydrogen fermentation is mainly performed in the upper part 11 of the fermenter 1.

  In the upper part 11 of the fermenter 1, hydrolysis and hydrogen fermentation by microorganisms are performed using carbohydrates, proteins, and lipids contained in the biomass as substrates. Hydrogen gas and carbon dioxide gas are generated mainly by hydrogen fermentation using carbohydrate as a substrate.

  Microorganisms used for hydrogen fermentation include anaerobic non-photosynthetic microorganisms or pure bacteria. It is not particularly limited as long as it is a microbial group having a hydrogen generating ability or a pure bacterium. Preferably, it is a group of microorganisms having hydrogen generation ability, for example, a group of microorganisms present in sludge after methane fermentation of garbage or sewage sludge, or a culture thereof.

  Hydrogen fermentation is generally performed at 30 to 60 ° C, preferably around 35 ° C or around 55 ° C. Hydrogen fermentation is generally carried out at pH 4.5 to 6.5, preferably at pH 5 to 6. The biomass supplied into the upper part 11 of the fermenter 1 by the biomass supply means 2 has a pH of 4.5 or less, but the fermentation liquid in the lower part 12 having a high pH moves into the upper part 11 by the upward flow, In order to mix with a fermentation broth, the pH of the fermentation broth in the upper part 11 is maintained at pH 5-6 suitable for hydrogen fermentation. You may adjust pH by adding a pH adjuster as needed.

  In the upper part 11 of the fermenter 1, the fermented liquid is appropriately stirred by a stirring means. The main purpose of stirring in the upper part 11 is to remove scum generated on the surface of the fermentation substrate, and the homogenization of the fermentation broth is incidental. As shown in FIG. 1, the fermentation liquid flow 62 spreads radially on the surface of the porous partition wall 13, and when it hits the wall surface, it becomes an upward flow that propagates through the wall surface. However, the upward flow gradually attenuates due to the friction of the wall surface, merges with the flow toward the center, and changes to the downward flow at the center.

  Although the mass transfer between the upper part 11 and the lower part 12 is restricted by the porous partition wall 13, stirring is performed to such an extent that the fermentation liquid in the upper part 11 does not enter the lower part 12 through the holes of the porous partition wall 13. As a stirring means, a rotary blade, a pump, and a blower are mentioned, for example. The stirring means shown in FIG. The stirring means in the upper part 11 shown in FIGS. Stirring may be performed intermittently.

  As shown in FIG. 3, a hydrogen gas separation membrane 17 is provided in the middle of the piping of the blower 16, and the hydrogen gas is separated from the biogas by the hydrogen gas separation membrane 17 and the remaining gas is discharged into the fermentation broth in the upper portion 11. By doing so, the fermentation broth is aerated, the hydrogen partial pressure in the fermentation broth is reduced, and the fermentation efficiency of hydrogen fermentation is increased.

  By gently stirring, a gentle concentration distribution of the substance in the vertical direction in the upper part 11 of the fermenter 1 can be made. In the upper part 11, the substance concentration is low and the microorganism concentration is also low. However, since the microorganisms that perform hydrogen fermentation have a high growth rate, the microorganism concentration does not become a rate-determining condition for hydrogen fermentation.

  Next, the fermentation residue of hydrogen fermentation is transferred into the lower part 12 by the transfer means 15 as a part of the fermentation liquid in the upper part 11. The transfer speed is not particularly limited. When transferring intermittently, repeat transfer and transfer stop every few hours.

  By the transfer of the fermentation broth in the upper portion 11, the fermentation broth in the lower portion 12 is extruded into the upper portion 11, an upward flow is generated, and the fermentation broth is circulated appropriately in the fermenter 1. The fermentation broth in the lower part 12 moves into the upper part 11 and mixes with the fermentation liquid in the upper part 11. Since the fermentation broth in the lower part 12 has a high pH, the pH of the fermentation broth in the upper part 11 is maintained at pH 5-6 suitable for hydrogen fermentation. Moreover, since the biogas is generated in the fermentation liquid in the lower part 12 by methane fermentation performed in the lower part 12 and passes through the porous partition wall 13 and becomes an upward flow, the hydrogen partial pressure of the fermentation liquid in the upper part 11 is increased. The fermentation efficiency of hydrogen fermentation increases.

(Methane fermentation)
Methane fermentation is mainly performed in the lower part 12 of the fermenter 1.

  By-product organic acid (acetic acid, formic acid, lactic acid, butyric acid, propionic acid, etc.) contained in the fermentation liquid of the upper part 11 transferred into the lower part 12 by the transfer means 15 or not used for hydrogen fermentation Methane fermentation by microorganisms is performed using carbohydrates, proteins, lipids, etc. as substrates. Methane gas and carbon dioxide gas are generated by methane fermentation.

  Examples of microorganisms used for methane fermentation include activated sludge and digested sludge accumulated and cultured under anaerobic conditions.

  Methane fermentation is generally performed at 25 to 65 ° C, preferably 30 to 40 ° C, and in the case of thermophilic bacteria, 50 to 60 ° C. Methane fermentation is generally carried out on the alkaline side at pH 5-10, preferably 7-9. You may adjust pH by adding a pH adjuster as needed.

  In the lower part 12 of the fermenter 1, the fermented liquid is appropriately stirred by stirring means. The main purpose of stirring in the lower part 12 is to prevent precipitation, and the homogenization of the fermentation broth is incidental. As shown in FIG. 1, the fermented liquid flow 62 spreads radially at the lower end surface of the fermenter 1. However, the upward flow gradually attenuates due to the friction of the wall surface, merges with the flow toward the center, and changes to the downward flow at the center.

  Although the mass transfer between the upper part 11 and the lower part 12 is restricted by the porous partition wall 13, stirring is performed to such an extent that the fermentation liquid in the lower part 12 does not enter the upper part 12 through the holes of the porous partition wall 13. As a stirring means, a rotary blade, a pump, and a blower are mentioned, for example. The stirring means shown in FIG. FIG. 4 shows an embodiment in which the shaft of the rotary blade 14 is attached to the cylindrical side surface of the fermenter 1 as a stirring means in the lower part 12. Stirring may be performed intermittently.

  By gently stirring, the concentration distribution of the substance can be made in the vertical direction in the lower part 12 of the fermenter 1. In the lower part 12, since the concentration of the substance is high and the microorganisms are present at a high concentration, methane fermentation is performed efficiently.

(Recovery of biogas and fermentation residue)
The mixed gas composed of hydrogen gas and carbon dioxide generated by hydrogen fermentation shifts to the upper gas phase in the upper portion 11. In addition, the mixed gas composed of methane gas and carbon dioxide generated by methane fermentation passes through the holes of the porous partition wall 13 and moves to the gas phase above the upper portion 11 through the upper portion 11. These biogas are continuously recovered out of the fermenter 1 by the biogas recovery means 3 from the gas phase in the upper part 11. Biogas may be stored as it is, or may be stored after removing carbon dioxide.

  The fermentation residue containing substances that have not been used for hydrogen fermentation and methane fermentation is continuously or intermittently recovered outside the fermenter 1 by the fermentation residue recovery means 4.

  In the method of the present invention, the residence time is preferably 5 to 25 days, more preferably 10 to 20 days.

  EXAMPLES The present invention will be described below with reference to examples, but the present invention is not limited to the following examples.

Example 1
As shown in FIG. 1, a soy shochu is added to a hydrogen methane fermentation apparatus having a fermenter 1 having a cylindrical shape with a height of 12 m and a diameter of 3.5 m and having a porous partition wall 13 at a height of 8.4 m from the lower end surface of the cylinder. Hydrogen fermentation and methane fermentation were performed in an interlocked manner by continuously supplying 5 tons / day of koji (solids concentration 6.0%, organic matter concentration 5.4%). The organic substance concentration was calculated from the result of an ignition loss test in which the shochu shochu was dried and then heated at 600 ° C. for 2 hours. The height of the liquid level of the fermentation liquid in the fermenter was 10.5 m from the lower end surface of the cylinder. Stirring was performed intermittently so that operation and stop were repeated every hour. Hydrogen fermentation was performed at 35 ° C. with the pH adjusted to pH 5.2. Methane fermentation was performed at 35 ° C. without controlling the pH. The amount of gas generated was measured using a positive displacement gas flow meter, and the gas component was measured by gas chromatography. The results are shown in Table 1.

(Example 2)
Hydrogen fermentation and methane fermentation are linked in the same manner as in Example 1 except that barley shochu (solids concentration 10.5%, organic matter concentration 10.0%) is used instead of shochu shochu. went. The results are shown in Table 1.

(Comparative Example 1)
Fermentation was carried out in the same manner as in Example 1 except that a complete mixing tank type fermentation apparatus was used instead of the hydrogen methane fermentation apparatus. The results are shown in Table 1.

(Comparative Example 2)
Fermentation was carried out in the same manner as in Example 2 except that a complete mixing tank type fermentation apparatus was used instead of the hydrogen methane fermentation apparatus. The results are shown in Table 1.

  As is clear from Table 1, when either shochu shochu or barley shochu is used, the hydrogen methane fermentation apparatus uses hydrogen gas, methane gas, or these generated by fermentation as compared with a complete mixing tank type fermentation apparatus. It can be seen that the amount of any of the contained biogas is large. It can be seen that the amount of hydrogen gas is particularly large. Thus, it was found that hydrogen fermentation and methane fermentation can be performed efficiently by using the hydrogen methane fermentation apparatus of the present invention.

  ADVANTAGE OF THE INVENTION According to this invention, the apparatus and method for performing hydrogen fermentation and methane fermentation efficiently can be provided. Since the apparatus of the present invention includes a single fermenter, the production cost can be reduced. Moreover, since high fermentation efficiency is brought about, size can be made small and since it can be transported by land to an installation place after an assembly, manufacturing cost can further be suppressed. Since the method of the present invention can efficiently recover biogas from biomass, it can contribute to prevention of environmental pollution and energy reproduction.

DESCRIPTION OF SYMBOLS 1 Fermenter 11 Upper part in fermentation layer 12 Lower part in fermentation layer 13 Porous partition 14 Rotary blade 15 Transfer means 16 Blower 17 Hydrogen gas separation membrane 2 Biomass supply means 3 Biogas recovery means 4 Fermentation residue recovery means 5 Hydrogen gas 61 Fermentation liquid level 62 Flow of fermentation broth 71 Biomass 72 Biogas 73 Fermentation residue 74 Hydrogen gas

Claims (9)

A hydrogen methane fermentation apparatus for performing hydrogen fermentation and methane fermentation in conjunction with each other,
The apparatus is a single fermenter, biomass supply means for connecting to the fermenter and supplying biomass into the fermenter, and biogas generated in the fermenter connected to the fermenter. A biogas recovery means for recovering outside, and a fermentation residue recovery means for recovering the fermentation residue generated in the fermenter connected to the fermenter to the outside of the fermenter,
The fermenter isolates the inside of the fermenter into an upper part for hydrogen fermentation and a lower part for methane fermentation , and a porous partition wall capable of moving solids in biomass to the lower part, for stirring the inside of the upper part and the lower part, respectively. And a transfer means for transferring the fermentation broth in the upper part into the lower part.   The apparatus according to claim 1, wherein the fermenter has a cylindrical shape, and a ratio of the height and diameter of the cylinder is 2: 1 to 4: 1. The apparatus according to claim 2 , wherein the cylinder has a height of 8 to 12 m.   The ratio of the distance between the lower end surface and the upper end surface of the fermenter and the distance between the lower end surface of the fermenter and the partition wall is 10: 7 to 10: 8. The device according to item.   The device according to any one of claims 1 to 4, wherein an inner diameter of the hole of the partition wall is 50 to 100 mm.   The apparatus according to claim 1, wherein the stirring means is selected from the group consisting of a rotor blade, a pump, and a blower. A method for performing hydrogen fermentation and methane fermentation in conjunction with each other, wherein biomass is continuously or intermittently supplied into the apparatus according to any one of claims 1 to 6, and hydrogen is supplied at an upper portion in the apparatus. A method comprising continuously performing fermentation and methane fermentation at a lower part in the apparatus, and continuously or intermittently recovering biogas and fermentation residue from the apparatus.   The method of Claim 7 which stirs the inside of this fermenter by blowing the biogas collect | recovered at the said process in the fermenter in the said apparatus.   The method of Claim 7 or 8 which stirs the inside of this fermenter by blowing the gas which isolate | separated hydrogen gas from the biogas collect | recovered at the said process into the fermenter in the said apparatus.

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