WO2004037731A1 - メタンガスの製造方法 - Google Patents
メタンガスの製造方法 Download PDFInfo
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- WO2004037731A1 WO2004037731A1 PCT/JP2003/013397 JP0313397W WO2004037731A1 WO 2004037731 A1 WO2004037731 A1 WO 2004037731A1 JP 0313397 W JP0313397 W JP 0313397W WO 2004037731 A1 WO2004037731 A1 WO 2004037731A1
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- WO
- WIPO (PCT)
- Prior art keywords
- treatment
- methane fermentation
- acid
- production method
- organic waste
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- 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
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- 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
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/36—Means for collection or storage of gas; Gas holders
-
- 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
- C12M45/00—Means for pre-treatment of biological substances
- C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/06—Treatment of sludge; Devices therefor by oxidation
- C02F11/08—Wet air oxidation
- C02F11/086—Wet air oxidation in the supercritical state
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/20—Total organic carbon [TOC]
-
- 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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the present invention relates to a method for producing methane gas from organic waste.
- Activated sludge (organic waste) derived from the treatment of food waste and sewage, etc., is said to be generated in large quantities.
- food waste is approximately 200000 t / year. , About 900,000 t / year, respectively.
- these organic wastes are incinerated and landfilled, and cannot be said to be used effectively.
- incineration requires a dehydration step, which is extremely costly.
- due to the problem of landfill for final waste after incineration it is expected that it will not be possible to secure it in a few years. Therefore, there is a need for ways to recycle and recycle organic waste.
- an object of the present invention is to provide a practical technology capable of effectively utilizing organic waste.
- the present invention provides a method for producing methane gas from organic waste, comprising a step of subjecting the organic waste to low molecular weight treatment with at least one of supercritical water and subcritical water, And subjecting the depolymerized product to methane fermentation.
- the present inventors have conducted various studies in order to achieve the above object. In the process, I came up with the idea of treating organic waste with low molecular weight and subjecting the treated material to methane fermentation. Further investigations based on this idea have shown that the use of supercritical water or subcritical water or both treatments can reduce complex organic compounds such as the processes 1) to 3) described above to simple organic compounds or simple organic compounds.
- FIG. 1 is a schematic view of an example of the method for producing methane gas of the present invention.
- FIG. 2 is a schematic diagram of an example of an apparatus that can be used for methane fermentation of the present invention.
- FIG. 3 is a schematic diagram of the reactor used in the examples.
- FIG. 4 is a diagram illustrating an example of a subcritical water treatment process.
- FIG. 5 is a diagram showing an example of the change over time in the yield of the solid phase at each reaction temperature.
- FIG. 7 is a graph showing an example of a change in the yield of amino acids in an aqueous phase with temperature.
- FIG. 11 is a diagram showing an example of the change over time in the composition of the discharged aqueous solution in continuous methane fermentation.
- a treatment method using subcritical water is preferable to a treatment method using supercritical water.
- Advantages of using subcritical water include, for example, that subcritical water has a higher hydrolysis ability than supercritical water and can produce various useful substances, and whether subcritical water has a lower decomposition power than supercritical water.
- Useful substances can be taken out without decomposing them into inorganic substances, and most of the above-mentioned hydrolysis reactions are exothermic reactions.
- the running cost of subcritical water treatment can be made sufficiently low, and the condition of subcritical water is milder than the condition of supercritical water. It is possible that, even though subcritical water is water, the extraction power of oils and fats is strong, and it is possible to extract almost 100% of them from raw materials.
- supercritical water having a temperature of up to about 700 K can be preferably used in the present invention as long as it is treated in the same manner as the subcritical water treatment without mixing an oxidizing agent or the like. This is because, in the case of the supercritical water treatment, oxidation hardly occurs and thermal decomposition occurs, and the deterioration effect on the apparatus is milder than conventionally known supercritical water oxidation.
- the treatment temperature is, for example, preferably in the range of 440 to 553 K, more preferably 470 to 553 K, and still more preferably 493 to 553 K K.
- the processing pressure is, for example, 0.8 to 6.4 MPa, more preferably 1.5 to 6.4 MPa, and still more preferably 2.3 to 6.4 MPa. It is.
- the processing time is, for example, 1 to 20 minutes, more preferably 1 to 10 minutes, and still more preferably 1 to 5 minutes.
- the treatment for depolymerizing the organic waste can be performed, for example, as follows. That is, when the batch method is used, for example, an organic waste and water are charged into a pressure-resistant heat-resistant reactor formed of a material such as stainless steel and sealed. By heating the reactor to a predetermined temperature, the inside of the reactor becomes high temperature and high pressure. As a result, the water in the reactor is brought into a subcritical state or a supercritical state, and the organic waste is reduced in molecular weight.
- the depolymerization treatment is, for example, a continuous method in addition to the batch method as described above. From the viewpoint of practical use, continuous treatment is preferred.
- the production method of the present invention preferably includes, for example, a step of separating an aqueous phase from the depolymerized product, and the aqueous phase is preferably subjected to methane fermentation. By doing so, methane fermentation can be performed in a shorter time and at a higher digestibility.
- This aqueous phase contains, for example, organic acids, phosphoric acids, amino acids, sugars, fatty acids, and the like. Among them, the aqueous phase preferably contains an organic acid.
- Organic acids include, for example, lactic acid, acetic acid, pyroglutamic acid, formic acid and the like, and among them, acetic acid is preferred.
- the method of separating and recovering the aqueous phase from the depolymerized product includes, for example, a centrifugal separation method. In other words, the depolymerized product is separated into three layers of oil-water-solid by centrifugation based on the difference in density, and the layer formed by the aqueous phase may be collected.
- the organic waste to which the production method of the present invention is applied is not particularly limited, and for example, activated sludge derived from sewage treatment, food waste, garbage, livestock manure, and the like is applied.
- the raw material tank 1 is provided with a stirrer, and a high pressure pump 2 is arranged on a pipe connecting the raw material tank 1 and the heater 3.
- the methane gas fermentation unit has an intermediate tank 6, a metering pump 7, a fermenter 8 and a gas holder 9 as main components, which are connected by pipes in this order.
- the intermediate tank 6 is connected with a pipe derived from a subcritical reaction device of the subcritical unit, and a back pressure valve 5 is disposed in the pipe.
- the production of methane gas by this apparatus is performed, for example, as follows. First, organic waste is put into the raw material tank 1. This organic waste may be stirred with a stirrer. This organic waste is introduced into a heater by a high-pressure pump 2 and heated to a predetermined temperature.
- FIG. 1 is a configuration diagram of an example of a continuous methane fermentation apparatus.
- this device has an intermediate tank 6 for storing low molecular weight organic waste, a metering pump 7, a fermenter 8 And gas holder 9 as main components, which are connected by pipes in this order.
- the intermediate tank 6 has a stirrer.
- the fermentation tank 8 is arranged in a constant temperature bath 10 containing a liquid such as water. Both the fermenter 8 and the thermostat 10 are equipped with a stirrer.
- a pipe is led out from the upper part of the constant temperature bath 10, and a tip of the pipe is introduced into a lower part of the constant temperature bath 10, and a circulation pump 15 and a heater 16 are arranged in the middle of the pipe. I have.
- the thermostat 10 is agitated by the stirrer and the liquid inside is circulated by the circulating pump.
- the temperature in the thermostat 10 is monitored by the temperature controller 17 and the information is
- the heater 17 is further controlled, and the liquid in the thermostat 10 is maintained at a constant temperature (for example, 37 to 55 ° C.).
- methane fermentation is performed by the bacteria while being stirred by the stirrer, and the generated gas is sent into the gas holder 9 through the pipe 12 and collected there. Further, in order to monitor the fermentation state, gas is appropriately sampled from the gas sampling valve 14.
- the metering pump 7 When the low-molecular-weight organic waste in the fermenter 8 is reduced, it is replenished by the metering pump 7 and the excess It is sent to the waste liquid tank 13.
- methane fermentation can be performed continuously.
- a conventionally known methane bacterium or the like can be appropriately used.
- the organic waste used is sewage activated sludge
- digested sludge from a sewage treatment plant is used for methane fermentation.
- the group of microorganisms used for the methane fermentation is preferably methane bacteria rich and may also contain acid-producing bacteria. It is also preferable that the microorganisms used for the methane fermentation are acclimated to acetic acid before use. This is because the efficiency of methane fermentation is improved.
- the reaction rate in the fermenter in the fast high digestibility methane fermentation of the present invention is about 15 to 150 times faster than that of the conventional fermentation, so that the volume of the fermenter is 1/15 to 1 / 150, and the energy required to keep the fermenter at a constant temperature can be reduced to 1/15 to 1/150 compared to the conventional type.
- a buffer, supplementary nutrients, and the like can be appropriately added to the methane fermentation tank.
- the buffer and supplemental nutrients are not particularly limited, and conventionally known ones can be used.
- the carbon digestibility in methane fermentation is, for example, 80% or more, preferably 90% or more, and more preferably 97% or more.
- the carbon digestibility can be calculated using the total organic carbon (TOC) .For example, it can be calculated based on the following formula by analyzing the components of the stock solution used for methane fermentation and the waste solution after methane fermentation. it can.
- the TOC can be measured by, for example, a TOC analyzer.
- the TOC analyzer is an apparatus for determining TOC from the difference between the total carbon content (TC) and the inorganic carbon content (IC).
- Carbon digestibility (stock solution T ⁇ C-waste solution TOC) / stock solution TOCX 100
- the methane gas generated and recovered by performing the methane fermentation is converted to heat by a gas poiler, for example, to power generated by gas power generation. It can be used in various fields, such as conversion and fuel cell hydrogen supply sources.
- a useful product can be produced by subjecting activated sludge to a low molecular weight treatment with at least one of supercritical water and subcritical water.
- the low-molecular-weight treatment of activated sludge can be performed, for example, in the same manner as the low-molecular-weight treatment of organic waste described in the above-described method for producing methane gas.
- a low-molecular-weight treatment step a low-molecular-weight treated product containing phosphoric acid, an organic acid, a fatty acid, an amino acid, a sugar and the like can be obtained. It is preferable to separate and purify useful substances from these.
- Examples of the organic acid include lactic acid, formic acid, acetic acid, pyroglutamic acid, and propionic acid.
- Examples of the fatty acid include palmitoleic acid, palmitic acid, oleic acid, and stearic acid.
- Examples of the amino acids include alanine, aspartic acid, glycine, isoleucine, leucine, and fenylalanine.
- Examples of the sugar include glucose, fructose and the like.
- phosphoric acid is currently limited The present invention can be expected as a technology for extracting new phosphoric acid.
- lactic acid is useful as a raw material for biodegradable plastics.
- the production amount of useful substances contained in the depolymerized product varies depending on the processing conditions in the depolymerization process, for example, the processing temperature, the processing pressure, the processing time, and the like. Therefore, useful products can be selectively produced by adjusting the processing conditions.
- the processing conditions in the depolymerization process for example, the processing temperature, the processing pressure, the processing time, and the like. Therefore, useful products can be selectively produced by adjusting the processing conditions.
- examples of the present invention will be described, but the present invention is not limited thereto.
- activated sludge was used as organic waste, and subcritical water treatment was performed by the patch method. Then, the depolymerized product obtained by the subcritical water treatment was subjected to methane fermentation to recover methane gas, and at the same time, an oil phase, an aqueous phase and a solid phase were separated and recovered, and the components were analyzed.
- Figure 3 shows an outline of the reactor used for subcritical water treatment.
- This reactor has a structure in which caps 19 are respectively attached to both ends of a pipe 18.
- d indicates the outer diameter of the pipe 18
- d 2 indicates the inner diameter of the pipe 18
- d 3 indicates the diameter of the inscribed circle of the cap 19.
- L 2 represents a length of the reactor.
- the reactor has an outer through d is 9. 5 mm, the inner diameter d 2 is 7.5mm stainless steel: manufactured using the pipe 1 8 (Material SUS 3 1 Ltd. 6).
- the pipe 18 was cut to about 15.5 cm with a pipe cutter, and the length was adjusted to about 15.0 cm using a lathe.
- the cut end of the pipe 18 was cut so as to be smooth, and the cut end was chamfered on the outside and the inside. Thereafter, the cut pipe 18 was washed, and a cap 19 (manufactured by SWAGEL0K, trade name SS-600-C) was attached to each end of the pipe 18.
- Attachment of the cap 19 was performed by first tightening it by hand, and then rotating it one turn and 90 degrees using a monkey wrench.
- total length L 2 is 1 6. 5 cm, the shortest distance L between the cap 1 9 1 2 O cm.
- the inside of the reactor was replaced with Ar in advance. Thereafter, the activated sludge sample (0.8 g of sludge, 4.0 g of ultrapure water) prepared as described above was charged into the reactor. Before sealing the reactor, Ar was again flown for about 30 seconds to deoxygenate, and then the reactor was sealed.
- the contents of the reactor were taken out into a test tube D having an internal volume of 8.0 cm 3 .
- the test tube D was set on a centrifugal separator (manufactured by KUB0TA, trade name: KN-70), and centrifuged at 250 rpm for 10 minutes.
- KUB0TA trade name: KN-70
- the contents in the test tube D formed a multilayer from the difference in mass.
- a liquid oil layer was formed on the uppermost layer, a solid fat layer was formed below the layer, a water layer was formed thereunder, and a solid layer was formed on the lowermost layer.
- the fat and oil phase and a part of the aqueous phase in the test tube D were taken out to the test tube F.
- ultrapure water about 5. 0 cm 3 in addition to the test tube F, for 1 0 minutes at 2 5 0 0 r immediate Centrifuged.
- the aqueous phase present under the oil phase was removed using a Pasteur pipette, and transferred to a volumetric flask G having an internal volume of 250 cm 3 . This operation was repeated two or three times, and a part of the aqueous phase was collected in a volumetric flask G.
- the fat phase was separated and recovered from the test tube D.
- the membrane was dried at room temperature of 25 ° C. for 3 days.
- the fats and oils recovered in this way were treated as a fat and oil phase.
- the contents of the reactor after subcritical water treatment were separated and collected into four phases, an oil phase, a fat phase, an aqueous phase, and a solid phase.
- the mass of the solid phase and the fat phase was measured after air drying.
- hexane was evaporated by air drying, and the mass was measured.
- the organic acid and phosphoric acid in the aqueous phase separated and recovered as described above are separated by high-performance liquid chromatography (HPLC). Analysis and quantification were performed using an analytical system (manufactured by Shimadzu Corporation, product name: LC-10A, separation method: ion exclusion chromatography, detection method: post-column pH buffered electrical conductivity detection method).
- Figure 6 shows the changes in the yield of organic acids and phosphoric acid with temperature when the reaction time of the subcritical water treatment was fixed (10 minutes). The yield was calculated based on the above formula (1). As shown in Fig. 6, there were mainly three types of phosphoric acid, acetic acid, and pyroglutamic acid in the aqueous phase. The yield of mechanical acid was low. The phosphoric acid yield varies depending on the reaction temperature,
- FIG. 7 shows the change in the yield of amino acids in the aqueous phase due to the difference in the reaction temperature when the reaction time of the subcritical water treatment was kept constant (10 minutes). The yield was calculated based on the above formula (1). As shown in FIG. 7, various amino acids were present in the aqueous phase, but glycine and alanine were mainly present. The yield of alanine described above showed a maximum value of 0.009 at 533 K.
- Methane fermentation was performed using the aqueous solution of low molecular organic matter obtained by the subcritical water treatment as described above.
- the sewage digester sludge used as the microorganism group used for methane fermentation was adjusted to VSS (loss on ignition of suspended solids (SS)) of 100 mg / l and sealed with a stirrer. Put in a 000 ml container, keep the temperature constant in a thermostat at 35 ° C, and continuously inject an aqueous solution of acetic acid adjusted to 5,000 Omg / 1 at a load of 400 ml per day. Adaptation of activated sludge containing methane bacteria to acetic acid
- Figure 10 shows the change in the concentration of methane gas generated during acetic acid acclimation. As shown in Fig. 10, in about 15 days, a group of microorganisms used for methane fermentation was generated. The activated sludge that had been subjected to acclimation was VS S 4,000 m g / l, and the mixture was put in a sealed 2,000 ml fermentation vessel capable of stirring the inside with a mixer, and used for methane fermentation in a 35 ° C constant temperature bath.
- composition Weight ratio (% by mass) Concentration (mg / I)
- the stock solution having the composition of Table 1 (2,000 Omg / 1) shown in Table 1 was continuously injected into the fermentation vessel at a rate of 200 m1 for 1 hour. Methane fermentation was performed. Methane fermentation was performed using the apparatus shown in the schematic diagram of FIG. The concentrations of acetic acid, short-chain fatty acids, and formic acid in the discharged treatment liquid, and the amount of generated gas and methane per minute were measured every 30 minutes. The generation of gas was confirmed, and the time was set to zero.
- Fig. 11 shows a graph of the change over time in the concentration of the discharged liquid
- Fig. 12 shows a graph of the change over time in the amount of gas generated. As shown in Figs.
- the ratio of TOC to the short-chain fatty acid stock solution concentration was 62% (720 + 1160 X 100), and the ratio of TOC to the waste solution concentration was 49% (67 + 13). 8 ⁇ 100), which indicates that the fatty acids are degraded by the acid-producing bacteria contained in the microorganism group used for the methane fermentation to reduce the molecular weight.
- the method for producing methane gas of the present invention provides a practical technique that can effectively utilize organic waste. Since the method for producing methane gas of the present invention has a short digestion rate and a high digestibility, organic wastes, which require enormous costs for incineration, can be turned into re-energy resources. Also, the equipment used for manufacturing can be made compact, for example, it can be distributed and installed in cities as a regional decentralized zero-emission methane fermentation and power generation system.
Abstract
Description
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Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE60336495T DE60336495D1 (de) | 2002-10-22 | 2003-10-20 | Herstellungsverfahren für methangas |
AT03758743T ATE502903T1 (de) | 2002-10-22 | 2003-10-20 | Herstellungsverfahren für methangas |
DK03758743.3T DK1561730T3 (da) | 2002-10-22 | 2003-10-20 | Fremgangsmåde til fremstilling af methangas |
JP2004546426A JP4590613B2 (ja) | 2002-10-22 | 2003-10-20 | メタンガスの製造方法 |
AU2003275567A AU2003275567A1 (en) | 2002-10-22 | 2003-10-20 | Method for producing methane gas |
US10/532,038 US7736510B2 (en) | 2002-10-22 | 2003-10-20 | Method for producing methane gas |
EP03758743A EP1561730B1 (en) | 2002-10-22 | 2003-10-20 | Method for producing methane gas |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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JP2002306993 | 2002-10-22 | ||
JP2002-306993 | 2002-10-22 |
Publications (1)
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WO2004037731A1 true WO2004037731A1 (ja) | 2004-05-06 |
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PCT/JP2003/013397 WO2004037731A1 (ja) | 2002-10-22 | 2003-10-20 | メタンガスの製造方法 |
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US (1) | US7736510B2 (ja) |
EP (1) | EP1561730B1 (ja) |
JP (1) | JP4590613B2 (ja) |
CN (1) | CN1711219A (ja) |
AT (1) | ATE502903T1 (ja) |
AU (1) | AU2003275567A1 (ja) |
DE (1) | DE60336495D1 (ja) |
DK (1) | DK1561730T3 (ja) |
WO (1) | WO2004037731A1 (ja) |
Cited By (6)
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JP2007023214A (ja) * | 2005-07-20 | 2007-02-01 | Hiroshima Univ | バイオマスガス化方法及びシステム |
JP2007111673A (ja) * | 2005-10-24 | 2007-05-10 | Osaka Prefecture Univ | 生ゴミ又は食品残渣のメタン発酵処理方法 |
WO2013008907A1 (ja) * | 2011-07-14 | 2013-01-17 | 東洋ゴム工業株式会社 | 亜臨界水処理を用いた生ごみの高効率メタン発酵 |
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- 2003-10-20 AT AT03758743T patent/ATE502903T1/de not_active IP Right Cessation
- 2003-10-20 US US10/532,038 patent/US7736510B2/en not_active Expired - Fee Related
- 2003-10-20 WO PCT/JP2003/013397 patent/WO2004037731A1/ja active Application Filing
- 2003-10-20 DE DE60336495T patent/DE60336495D1/de not_active Expired - Lifetime
- 2003-10-20 JP JP2004546426A patent/JP4590613B2/ja not_active Expired - Lifetime
- 2003-10-20 AU AU2003275567A patent/AU2003275567A1/en not_active Abandoned
- 2003-10-20 CN CNA2003801018977A patent/CN1711219A/zh active Pending
- 2003-10-20 EP EP03758743A patent/EP1561730B1/en not_active Expired - Lifetime
- 2003-10-20 DK DK03758743.3T patent/DK1561730T3/da active
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
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JP2007023214A (ja) * | 2005-07-20 | 2007-02-01 | Hiroshima Univ | バイオマスガス化方法及びシステム |
JP2007111673A (ja) * | 2005-10-24 | 2007-05-10 | Osaka Prefecture Univ | 生ゴミ又は食品残渣のメタン発酵処理方法 |
WO2013008907A1 (ja) * | 2011-07-14 | 2013-01-17 | 東洋ゴム工業株式会社 | 亜臨界水処理を用いた生ごみの高効率メタン発酵 |
CN102921711A (zh) * | 2012-07-17 | 2013-02-13 | 上海锦泰新能源环保科技有限公司 | 一种有机固体废弃物再生资源化处理方法及设备系统 |
JP2016028800A (ja) * | 2014-07-25 | 2016-03-03 | 国立大学法人豊橋技術科学大学 | 有機物含有廃棄物の処理方法と処理システム |
CN107254493A (zh) * | 2017-07-31 | 2017-10-17 | 海宁文硕科技咨询有限公司 | 一种沼气的制备工艺 |
Also Published As
Publication number | Publication date |
---|---|
ATE502903T1 (de) | 2011-04-15 |
DE60336495D1 (de) | 2011-05-05 |
US20060183951A1 (en) | 2006-08-17 |
JPWO2004037731A1 (ja) | 2006-02-23 |
US7736510B2 (en) | 2010-06-15 |
EP1561730A4 (en) | 2007-07-18 |
EP1561730A1 (en) | 2005-08-10 |
JP4590613B2 (ja) | 2010-12-01 |
CN1711219A (zh) | 2005-12-21 |
EP1561730B1 (en) | 2011-03-23 |
DK1561730T3 (da) | 2011-06-14 |
AU2003275567A1 (en) | 2004-05-13 |
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