WO2020008622A1 - Procédé de production hydrogène utilisant la biomasse comme matière première - Google Patents

Procédé de production hydrogène utilisant la biomasse comme matière première Download PDF

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Publication number
WO2020008622A1
WO2020008622A1 PCT/JP2018/025703 JP2018025703W WO2020008622A1 WO 2020008622 A1 WO2020008622 A1 WO 2020008622A1 JP 2018025703 W JP2018025703 W JP 2018025703W WO 2020008622 A1 WO2020008622 A1 WO 2020008622A1
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Prior art keywords
gas
pyrolysis
steam
temperature
heat
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PCT/JP2018/025703
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English (en)
Japanese (ja)
Inventor
白水　渡
俊一 内藤
和幸 原田
正廣 矢野
光揮 日巻
後藤　賢一
安藤　秀行
隆幸 西川
堂脇　直城
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株式会社 翼エンジニアリングサービス
株式会社 ジャパンブルーエナジー
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Priority to PCT/JP2018/025703 priority Critical patent/WO2020008622A1/fr
Priority to JP2020528650A priority patent/JP7140341B2/ja
Publication of WO2020008622A1 publication Critical patent/WO2020008622A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide

Definitions

  • the present invention relates to a method for producing hydrogen using biomass as a raw material.
  • hydrogen When hydrogen is used as a fuel, it does not emit carbon dioxide and is regarded as an environmentally friendly material.
  • hydrogen is supplied to a fuel cell to realize its use as a fuel cell vehicle or fuel cell power plant As the power generation efficiency is expected to improve dramatically, the demand is expected to increase further in the future.
  • Patent Document 1 A method for producing a product gas having a high calorific value from an organic substance and a substance mixture,
  • the circulating heat-carrying medium passes through a heating zone, a reaction zone, a pyrolysis zone and a separation step and subsequently returns to the heating zone, Separating the organic substance or substance mixture into a pyrolysis gas as a solid carbon-containing residue and a volatile phase by contacting the organic substance or substance mixture in a pyrolysis zone with a heated heat carrying medium; After passing through the pyrolysis zone, the solid carbon-containing residue is separated from the heat-carrying medium in a separation step, Mixing the pyrolysis gas with steam as the reaction medium and further heating to exchange a portion of the heat contained in the heated heat carrying medium in the reaction zone to produce a product gas having a high calorific value,
  • the steam is mixed with the pyrolysis gas in the pyr
  • Patent Document 2 The organic waste is heated at 500 to 600 ° C. in a non-oxidizing atmosphere using a heat carrier medium, and the generated pyrolysis gas is mixed with steam at 900 to 1000 ° C. Then, the obtained reformed gas is purified. To recover hydrogen.
  • a method for producing hydrogen using biomass as a raw material includes a pyrolysis step of supplying a heat carrier medium to obtain a pyrolysis gas from a biomass raw material, and increasing the temperature of the pyrolysis gas to be rich in hydrogen.
  • the thermal decomposition reaction temperature is 640 to 740 ° C., and steam and oxygen gas are simultaneously supplied in the reforming step, and the heat carrying medium is not supplied to the reforming step.
  • tar generated by the thermal decomposition reaction is completely decomposed, and hydrogen gas can be stably produced over a long period of time.
  • FIG. 1 is a schematic diagram illustrating an example of an apparatus (equipment) for implementing one embodiment of the present invention.
  • a method for producing hydrogen using biomass as a raw material includes a pyrolysis step of supplying a heat carrier medium to obtain a pyrolysis gas from a biomass raw material, and increasing the temperature of the pyrolysis gas.
  • a reforming step for obtaining a hydrogen-rich reformed gas wherein the heat-carrying medium in the pyrolysis step is heated to 680 to 740 ° C .;
  • the thermal decomposition reaction temperature is set to 640 to 740 ° C. to supply steam and oxygen gas simultaneously in the reforming step, and the heat carrier medium is not supplied to the reforming step.
  • This hydrogen production method completely decomposes the generated tar and can stably obtain hydrogen gas for a long period of time.
  • the biomass raw material may contain diphosphorus pentoxide (P 2 O 5 ).
  • the thermal decomposition reaction temperature can be easily adjusted to 640 to 740 ° C.
  • the thermal decomposition temperature of the thermal decomposition step in each of the hydrogen production methods is 660 to 700 ° C. As a result, the generation of tar is further suppressed, and hydrogen gas can be stably obtained over a long period of time.
  • the present inventor studied the hydrogen production methods described in Patent Documents 1 and 2 above, and found that the reason why tar did not decompose was that a temperature of 640 ° C. or more described later could not be secured as a temperature in the pyrolyzer. I found something. Therefore, in order to raise the temperature in the pyrolyzer, in the hydrogen production methods described in Patent Documents 1 and 2 described above, it was examined to increase the temperature of the heat-carrying medium to be preheated. In the case, the preheated heat carrier medium is supplied to the pyrolyzer through the reformer, and the heat held by the heat carrier medium is first used as a heat source of the reformer.
  • the preheater In order to raise the pyrolysis temperature for tar decomposition, the preheater requires a further increase in the preheating temperature of the heat carrying medium, that is, a preheating exceeding 1050 ° C. It was not realistic from the point of view, and it was found that it was difficult to raise the temperature of the reformer to 1000 ° C. by the heat carrying medium.
  • the “heating zone”, “reaction zone”, and “pyrolysis zone” in Patent Document 1 are respectively referred to as “preheater”, “reformer”, and “pyrolyzer” in the present invention. You are.
  • the present inventor further studied, (1) In order to suppress the generation of tar to a level that does not hinder the production of hydrogen, it is necessary to set the thermal decomposition reaction temperature to 640 ° C. or higher, and it is difficult to raise the temperature to 1000 ° C. in the reformer. The reason was that the heat transfer coefficient between the heat carrying medium and the reformed gas was small, and based on this finding, (2)
  • the heat source of the thermal decomposer is not limited to the heat carrying medium, and the idea is to supplement the lack of heat from the heat carrying medium with the other heat sources.
  • the pre-heated heat carrier medium is not charged into the reformer but is used only as a thermal decomposer and used as heat for elevating the temperature to the thermal decomposition temperature of the thermal decomposer and evaporating moisture, That the preheating temperature of the carrier medium can be lowered, (4)
  • the temperature can be easily raised to a predetermined thermal decomposition reaction temperature, and At the same time, by simultaneously injecting steam, the sensitivity of the reaction temperature due to insufficient oxygen is eased and the temperature control becomes easy, (5)
  • oxygen gas is supplied in place of the supply of the heat carrying medium, the temperature can be easily raised to the reforming reaction temperature of 1000 ° C.
  • Heat carrying medium (1) Shape and material of the heat carrying medium
  • the shape of the heat carrying medium is preferably a sphere, and the material is preferably ceramic such as alumina or steel. That is, alumina balls, ceramic balls, and steel balls can be used, and the diameter is preferably 10 to 30 mm.
  • (2) Preheating temperature The heat carrying medium is preheated by a preheater, and the preheating temperature range is 680 to 740 ° C. This preheating temperature range is much lower than 1050 ° C. shown in Patent Documents 1 and 2, so that the energy required for preheating can be saved, the thermal efficiency is improved, and an expensive refractory material is used for the preheater. This has the advantage of not having to do so.
  • the heat carrying medium 24 is heated in the preheater 3, serves as a heat carrying medium for thermal decomposition in the pyrolyzer 4, and supplies heat to the reaction for thermal decomposition, and the char separating device 6 separates the char and the heat medium. It is circulated and used in the circulating device 27.
  • Pyrolysis reaction process in pyrolyzer The pyrolysis reaction in the pyrolyzer will be described in detail.
  • Biomass raw material The raw material used in one embodiment of the present invention is biomass, sewage sludge, thinned wood, driftwood, wood pellets, straw pellets, paper sludge, garbage compost sludge, food waste, sludge, etc. Any type may be used as long as it contains hydrogen and oxygen, but sewage sludge is preferred from the viewpoint of availability. Further, the raw material may be a mixture of plural types of biomass.
  • the size of the biomass may be any size as long as it has undergone coarse pulverization. For example, a solid shape such as a plate having a length of 15 mm or less and a granular shape are preferable. Although the amount of water contained varies depending on the shape, it is preferably pre-dried before being supplied to the pyrolyzer at 30 to 20% by mass.
  • the pyrolysis temperature for obtaining the pyrolysis gas is 640 to 740 ° C.
  • the reason for setting this temperature range is that if the temperature is lower than 640 ° C., it is difficult to completely decompose tar generated by thermal decomposition, and if it exceeds 740 ° C., an excessive heat source is required to completely decompose the tar. That's why.
  • the thermal decomposition temperature is more preferably 660 to 700 ° C.
  • phosphorus pentoxide (P 2 O 5 ) is contained in the organic raw material.
  • P 2 O 5 evaporation is reduced. inhibition can, for volatilization vapor P 2 O 5 which may cause clogging trouble pyrolysis gas does not exist, has the advantage that it is possible to an organic material sewage sludge containing P 2 O 5.
  • the heat source of the thermal decomposition is provided by the heat-carrying medium, but is not sufficient, and the temperature range is set by blowing and supplying oxygen gas.
  • the heat transfer by the supply of steam and oxygen gas is much more efficient than the heat transfer of the heat carrier medium which is a solid phase.
  • the supply of water vapor suppresses the generation of heat spots, alleviates rapid changes in temperature, and controls the thermal decomposition reaction in response to short-term disturbances such as changes in the amount of organic raw material supplied. It has the advantage of being easy.
  • the respective supply ratios of steam and oxygen gas are preferably 1 to 4 in terms of a steam / oxygen gas molar ratio (mol of steam / mol of oxygen gas).
  • the reason for this range is that if it is less than 1, the temperature fluctuation may increase, and if it exceeds 4, the steam becomes oxidizing at 600 ° C. or higher, and the CO 2 concentration increases, which is not preferable for hydrogen recovery.
  • the temperature of steam is not limited, a temperature of 140 ° C. can be mentioned as an example.
  • the oxygen gas is not particularly limited, and is, for example, 40% manufactured by an industrial oxygen gas generator. C. can be used. And, when the molar ratio represented by water vapor / oxygen gas becomes higher, it becomes easier to control the thermal decomposition reaction with respect to disturbance caused by slight fluctuation of the oxygen flow rate.
  • the pyrolysis gas is a gas mainly composed of CH 4 , CO, CO 2 , and H 2 .
  • blowing steam as described above, it is possible to obtain a H 2, because the content of H 2 is small and 10% by volume, in order to increase the content of H 2, modification in the next step I do.
  • Reforming process in reformer The reformer is installed downstream of the pyrolyzer, and without using a heat carrier medium as a heat source, simultaneously supplies steam and oxygen gas, raises the temperature to 1000 ° C or higher, and performs the pyrolysis on the pyrolysis gas to obtain a hydrogen-rich crude gas. Obtain reformed gas. Then, the temperature can be easily raised to 1000 ° C. by simultaneously supplying steam and oxygen gas instead of supplying the heat carrying medium.
  • the steam may be, for example, 100 to 150 ° C.
  • the oxygen gas may be, for example, 40 ° C. produced by an industrial oxygen gas generator.
  • a steam reforming reaction proceeds, and a hydrocarbon gas such as CH 4 gas is converted into a hydrogen gas, and the content ratio of the hydrogen gas increases.
  • CH 4 + H 2 O ⁇ CO + 3H 2 can be mentioned.
  • the next shift reaction proceeds, and the content ratio of hydrogen gas increases.
  • the crude reformed gas thus obtained has a H 2 gas content of 50 to 54% by volume (dry basis).
  • the supply of steam is not only performed to advance the steam reforming reaction, but also to ease temperature sensitivity (rapid change).
  • the steam and the oxygen gas supplied to the reformer are preferably simultaneously supplied so that the molar ratio of steam / oxygen gas (mol of steam / mol of oxygen gas) becomes 1 to 4.
  • H 2 gas purification process The gas that has undergone the reforming step (coarse reformed gas) is cooled and dust-removed to remove trace amounts of harmful components such as HCl, CN, and NH 3 .
  • the removal can be performed by appropriately combining conventionally known means.
  • the purification of H 2 gas Thereafter, the purification of H 2 gas.
  • a known means may be appropriately used, and for example, a PSA means and a membrane separation means can be used.
  • the heat carrying medium 24 is heated (preheated) to 680 to 740 ° C. by the preheater 3, and after heating, is fed into the thermal decomposer 4 via the valve 25.
  • the heat source for preheating the heat carrier medium in the preheater 3 is a flue gas 19 of about 800 ° C. obtained by burning part of the char 18 and part of the pyrolysis gas 11 in the combustion furnace 23 as described later.
  • the combustion exhaust gas 20 is discharged from the preheater 3.
  • the pyrolysis step is performed by the pyrolyzer 4, and the biomass raw material 1 is supplied to the pyrolyzer 4 by the biomass raw material transporting device 2 such as a screw conveyor.
  • the temperature of the biomass raw material 1 is increased by the heat from the heat carrier medium 24 and the steam 8 and the oxygen gas 7 which are blown and supplied from the lower part of the pyrolyzer 4 at a temperature of 640 to 720 ° C. It is decomposed to generate pyrolysis gas 11.
  • the reforming step is performed in the reformer 5. Most of the pyrolysis gas 11 obtained by the pyrolysis reaction is sent to the reformer 5. In the reformer 5, steam 10 and oxygen gas 9 are simultaneously blown and supplied from the lower part thereof, and the temperature of the pyrolysis gas 11 is raised to 1000 ° C., and the steam reforming reaction proceeds, and the crude reforming gas 13 Get.
  • the purification process of the H 2 gas is performed in the crude reformed gas cooling / purifying device 21, and the crude reformed gas 13 that has passed through the reformer 5 is introduced into the crude reformed gas cooling / refining device 21, Although not shown, cooling, dust removal, and removal of trace amounts of harmful components are performed, and the purified reformed gas 14 is introduced into the hydrogen separator 22 to obtain pure hydrogen gas 15.
  • the off-gas 16 is discharged from the hydrogen separator 22.
  • the char of the heat carrier medium 24 and the biomass raw material 1 at about 640 ° C. are discharged from the bottom of the pyrolyzer 4, and are introduced into the char separation device 6 via the valve 26.
  • the char separation device 6 the char 17 and the heat carrying medium 24 are separated, and the heat carrying medium 24 is sent to the heat carrying medium circulating device 27, and is returned to the preheater 3 by the device for circulating use.
  • the char 17, except for a part 18 of the char, is used as an alternative fuel in a cement manufacturing facility or a coal-fired power plant.
  • As the char separation device 6, a known device such as a device capable of separating the heat carrying medium 24 and the char 17 by a sieve can be used.
  • the part 12 of the pyrolysis gas and the part 18 of the char are introduced into the combustion furnace 23 and burned, and serve as a heat source for the flue gas 19 at about 800 ° C. It serves as a heat source for preheating the heat carrying medium 24 by the preheater.
  • an external fuel such as LNG or LPG is used to supplement the heat source. It is not necessary to use a special furnace for the combustion furnace 23.
  • steam is produced using waste heat of the combustion exhaust gas 20 of the preheater, and the steam is supplied to the pyrolyzer and supplied to the reformer. It is also possible to use steam 10 that is generated.
  • the organic raw material commonly used in each example and each comparative example is sewage sludge, which is as follows.
  • Example 1> The preheating temperature of the heat carrying medium was set at 700 ° C.
  • the temperature of the pyrolyzer pyrolysis reaction temperature
  • steam at 140 ° C. and oxygen gas at 40 ° C. were blown.
  • the oxygen gas flow rate and the steam flow rate to the pyrolyzer were 1.71 Nm 3 / h and 2.75 kg / h, respectively
  • the flow rates of oxygen gas and steam to the reformer were 2.3 Nm 3 / h and 3.7 kg / h, respectively.
  • composition of the pyrolysis gas The composition of the pyrolysis gas, the amount of tar, and the composition of the gas leaving the reformer were measured. Table 4 shows the results. In the display of the composition of the pyrolysis gas, all hydrocarbon gases were represented by CH 4 . Hereinafter, the same notation is used.
  • Example 1 the temperature of the pyrolyzer was 690 ° C. and the temperature range was 650 to 740 ° C., and the steam / oxygen gas molar ratio was 2.0 and the molar ratio range was 1.0 to 4.0. Therefore, the content ratio of CH 4 gas contained in the pyrolysis gas was low, and the generation of tar could be completely suppressed. Further, the temperature of the reformer could be set to 1000 ° C. On the other hand, in Comparative Example 1, the pyrolysis temperature was 600 ° C. and was not in the above temperature range, so that the content ratio of the CH 4 gas contained in the pyrolysis gas was high, tar was generated, and The temperature was 937 ° C.
  • Example 2 in order to confirm that the evaporation of P 2 O 5 contained in the sewage sludge is suppressed, in Example 2 and Comparative Example 2, P 2 deposited on the crude reformed gas cooling / purifying device 22 in FIG. the amount of O 5 was measured.
  • Example 2 With the preheating temperature of the heat carrying medium set at 700 ° C. and the temperature of the pyrolyzer at 690 ° C., steam at 140 ° C. and oxygen gas at 40 ° C. were blown. At this time, the oxygen gas flow rate and the steam flow rate to the pyrolyzer were 1.71 Nm 3 / h and 2.75 kg / h, respectively, and the steam / oxygen gas molar ratio was 2.0. The amount of P 2 O 5 deposited on the crude reforming gas cooling / refining device 22 of FIG. 1 was measured. Table 5 shows the results.
  • the estimated P 2 O 5 vapor concentration was estimated based on the amount of clogs that blocked the crude reformed gas cooling / refining device 22 and the analysis results.
  • Example 2 the temperature of the pyrolyzer was 690 ° C. and the temperature range was 650 to 740 ° C., and the steam / oxygen gas molar ratio was 2.0 and the molar ratio range was 1.0 to 4.0. Therefore, the amount of P 2 O 5 deposited in the crude reforming gas cooling / refining apparatus is as small as 0.02 kg, and it can be said that the evaporation of P 2 O 5 contained in the sewage sludge is almost completely suppressed. .
  • the thermal decomposition temperature was 780 ° C., which was higher than the above temperature range, and the evaporation of P 2 O 5 was not suppressed.
  • Example 3 In order to confirm the influence of the steam / oxygen gas molar ratio on the yield of H 2 and the stability of temperature fluctuation, a comparison is made between Example 3 and Example 2.
  • Example 2 was performed as described above, but the amount of the pyrolysis gas was 16.64 Nm 3 / h, and the amount of the oxygen gas blown was ⁇ 0.30 Nm 3 / h. The variation in the temperature of the decomposer was ⁇ 60 ° C. Table 6 shows the composition of the resulting crude reformed gas.
  • Example 3 With the preheating temperature of the heat carrying medium set to 700 ° C. and the temperature of the pyrolyzer set to 690 ° C., 140 ° C. steam and 40 ° C. oxygen gas were blown. At this time, the flow rates of oxygen gas and steam to the pyrolyzer were 1.71 Nm 3 / h and 5.49 kg / h, respectively, and the molar ratio of steam / oxygen gas was 4.0. Table 6 shows the composition of the obtained pyrolysis gas.
  • Example 2 Comparing Example 2 with Example 3, the higher the molar ratio of water vapor / oxygen gas, the more the fluctuation of the pyrolysis reaction temperature can be suppressed with respect to the fluctuation of the oxygen gas flow rate. It can be said that the sensitivity of the resulting temperature change is improved.

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Abstract

L'invention concerne un procédé de production d'hydrogène en utilisant une biomasse en tant que matière première, le procédé comprenant une étape de pyrolyse servant à fournir un caloporteur afin d'obtenir un gaz de pyrolyse à partir d'une matière première de biomasse, et une étape de reformage pour élever la température du gaz de pyrolyse afin d'obtenir un gaz reformé riche en hydrogène, le procédé étant tel que : le caloporteur dans l'étape de pyrolyse est chauffé entre 680 et 740 °C ; dans l'étape de pyrolyse, la vapeur d'eau et le gaz oxygène sont également acheminés simultanément pour régler la température de réaction de pyrolyse entre 640 et 740 °C ; et dans l'étape de reformage, la vapeur d'eau et le gaz oxygène sont acheminés simultanément, sans le caloporteur.
PCT/JP2018/025703 2018-07-06 2018-07-06 Procédé de production hydrogène utilisant la biomasse comme matière première WO2020008622A1 (fr)

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PCT/JP2018/025703 WO2020008622A1 (fr) 2018-07-06 2018-07-06 Procédé de production hydrogène utilisant la biomasse comme matière première
JP2020528650A JP7140341B2 (ja) 2018-07-06 2018-07-06 バイオマスを原料とする水素製造方法

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021221165A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2021221164A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2021221163A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse

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JP2002080865A (ja) * 2000-09-08 2002-03-22 Toshiba Corp 廃棄物処理システム
JP2003510403A (ja) * 1999-09-24 2003-03-18 ドクトーア ミューレン ゲゼルシャフト ミット ベシュレンクテル ハフツング ウント コンパニー コマンディトゲゼルシヤフト 有機物質および物質混合物をガス化する方法
JP2011144330A (ja) * 2010-01-18 2011-07-28 Raito Kogyo Co Ltd 木質バイオマスのガス化システム及びその方法
JP2012201769A (ja) * 2011-03-24 2012-10-22 Raito Kogyo Co Ltd 有機物質のガス化システムにおける高速昇温方法
WO2017203587A1 (fr) * 2016-05-23 2017-11-30 株式会社ジャパンブルーエナジー Appareil de gazéification de biomasse

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JP2003510403A (ja) * 1999-09-24 2003-03-18 ドクトーア ミューレン ゲゼルシャフト ミット ベシュレンクテル ハフツング ウント コンパニー コマンディトゲゼルシヤフト 有機物質および物質混合物をガス化する方法
JP2002080865A (ja) * 2000-09-08 2002-03-22 Toshiba Corp 廃棄物処理システム
JP2011144330A (ja) * 2010-01-18 2011-07-28 Raito Kogyo Co Ltd 木質バイオマスのガス化システム及びその方法
JP2012201769A (ja) * 2011-03-24 2012-10-22 Raito Kogyo Co Ltd 有機物質のガス化システムにおける高速昇温方法
WO2017203587A1 (fr) * 2016-05-23 2017-11-30 株式会社ジャパンブルーエナジー Appareil de gazéification de biomasse

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021221165A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2021221164A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse
WO2021221163A1 (fr) * 2020-04-30 2021-11-04 株式会社ジャパンブルーエナジー Dispositif de gazéification de biomasse

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