WO2015132923A1 - 超臨界流体によるガス化装置 - Google Patents
超臨界流体によるガス化装置 Download PDFInfo
- Publication number
- WO2015132923A1 WO2015132923A1 PCT/JP2014/055696 JP2014055696W WO2015132923A1 WO 2015132923 A1 WO2015132923 A1 WO 2015132923A1 JP 2014055696 W JP2014055696 W JP 2014055696W WO 2015132923 A1 WO2015132923 A1 WO 2015132923A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- fuel gas
- gasification
- raw material
- temperature side
- Prior art date
Links
Images
Classifications
-
- 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
- C10J3/72—Other features
- C10J3/78—High-pressure apparatus
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
- F02C3/14—Gas-turbine plants characterised by the use of combustion products as the working fluid characterised by the arrangement of the combustion chamber in the plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas- turbine plants for special use
- F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas- turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1643—Conversion of synthesis gas to energy
- C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1876—Heat exchange between at least two process streams with one stream being combustion gas
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Definitions
- the present invention relates to a gasification apparatus that heats and pressurizes a gasification raw material to obtain a supercritical fluid and decomposes the gasification raw material to obtain a fuel gas.
- Patent Document 1 discloses that a biomass slurry containing a nonmetallic catalyst is hydrothermally treated under conditions of a temperature of 374 ° C. or higher and a pressure of 22.1 MPa or higher, and the generated gas is used to generate a power generator.
- a biomass gasification power generation system that generates power and heats a slurry body using exhaust heat from a power generation device is described.
- the treated fluid after the gasification treatment is heat-exchanged with the slurry body by a double tube heat exchanger.
- the treated fluid changes from the supercritical state to the subcritical state, and changes from the gas-liquid mixed state to the gas-liquid two-phase flow.
- gas fuel gas or the like
- liquid are separated vertically by a volume ratio of about 2: 8, so the energy of the processed fluid has not been effectively utilized.
- gas since gas has physical pressure energy and also has chemical energy, it can be used as a fuel, but it is used for heat exchange without gas-liquid separation. This caused a decrease in efficiency.
- the treated fluid changes into a gas-liquid two-phase flow between the inner and outer tubes in the middle temperature part of the double-pipe heat exchanger. It was a site where generation was a problem.
- the present invention has been made in view of such circumstances, and an object thereof is to effectively utilize the energy of the processed fluid and to suppress the generation of tar.
- the present invention is a gasification apparatus in which a gasification raw material is heated and pressurized to a supercritical state, and the gasification raw material is decomposed to obtain a fuel gas.
- a heat exchanger that exchanges heat between the gasification raw material and the post-treatment fluid by introducing a supercritical fluid after treatment into the low-temperature side flow channel,
- a gas-liquid separator that takes out the treated fluid that has become a subcritical state by heat exchange from the high-temperature side flow path and performs gas-liquid separation, and returns the separated liquid to the high-temperature side flow path, and the gas-liquid separator And a turbine powered by the fuel gas separated in (1).
- the post-processed fluid in the subcritical state is taken out from the high temperature side flow path and separated into gas and liquid.
- the fuel gas after gas-liquid separation is used as motive power of a turbine, the energy which fuel gas has can be used effectively.
- the liquid after the gas-liquid separation is returned to the high-temperature side flow path, the heat exchange efficiency by the returned liquid can be increased.
- the temperature of the raw slurry can be increased in a short time, the generation of tar can also be suppressed.
- the turbine is rotated by injection of the fuel gas in a high pressure state.
- the turbine since the turbine is rotated by the pressure energy of the fuel gas, the fuel gas after work can be used as the fuel. For this reason, the energy which fuel gas has can be utilized still more effectively.
- the fuel gas after rotating the turbine is used for heating the gasification raw material.
- the energy of the fuel gas can be used more effectively.
- the fuel gas after the turbine is rotated is burned and used for rotating the turbine.
- the fuel gas after rotating the turbine by physical pressure energy is combusted and the turbine is rotated. Therefore, the chemical energy of the fuel gas can also be used to efficiently generate power.
- the exhaust gas obtained by combustion of the fuel gas and used for rotating the turbine for heating the gasification raw material.
- the gasification raw material is heated with the high-temperature exhaust gas after being used for rotating the turbine, energy can be used more effectively.
- the energy of the processed fluid is effectively utilized. And the generation of tar can be suppressed.
- (A) is a figure explaining the structure of a gas-liquid separator. It is a figure explaining the state before and behind gas-liquid separation in a double tube type heat exchanger. It is a figure explaining the structure of the modification in a supercritical gasifier.
- the illustrated supercritical gasifier includes a raw material adjustment unit 10, a raw material supply unit 20, a heat exchange unit 30, a gasification processing unit 40, a fuel gas recovery unit 50, and a power generation unit 60.
- the raw material slurry adjusted by the raw material adjusting unit 10 is sent by the raw material supply unit 20 to the low temperature side flow path 31a of the heat exchanger 31 included in the heat exchange unit 30 at a high pressure. And the raw material slurry heated by the heat exchange part 30 is further heated by the gasification process part 40, and is made into a supercritical state. Thereby, the organic substance contained in the raw material slurry is decomposed, and fuel gas such as methane, ethane, and ethylene is generated.
- the post-processed fluid in the supercritical state is introduced into the high temperature side channel 31b of the heat exchanger 31 and heat exchanged with the raw slurry.
- the treated fluid becomes a subcritical state and changes to a gas-liquid two-phase flow. Therefore, the post-processed fluid in the subcritical state is taken out from the heat exchanger 31 in the middle of the high temperature side flow path 31b, and gas-liquid separation is performed by the fuel gas recovery unit 50. And the liquid after gas-liquid separation is returned to the high temperature side flow path 31b of the heat exchanger 31, and is used for heat exchange with a raw material slurry.
- the gas (fuel gas) after gas-liquid separation is recovered by the fuel gas recovery unit 50 and used as power for the power generation unit 60.
- the raw material adjustment unit 10 is a part that adjusts the raw material slurry from the gasification raw material and the like, and includes an adjustment tank 11 and a crusher 12.
- the adjustment tank 11 is a container for preparing a suspension by mixing gasification raw materials, activated carbon, water, and the like, and is provided with a stirring blade (not shown).
- gasification raw material for example, shochu residue, egg-collected chicken manure, and sludge can be used.
- Activated carbon functions as a nonmetallic catalyst, and porous particles having an average particle diameter of 200 ⁇ m or less can be used.
- the crusher 12 is a device for crushing the solid content (mainly gasification raw material) contained in the suspension mixed in the adjustment tank 11 to obtain a uniform size. In this embodiment, crushing is performed so that the average particle size of the solid content is 500 ⁇ m or less. Due to crushing by the crusher 12, the suspension becomes a raw slurry.
- the raw material supply unit 20 is a part that feeds the raw material slurry at a high pressure, and includes a supply pump 21 and a high pressure pump 22.
- the supply pump 21 is a device for supplying the raw slurry sent from the crusher 12 toward the high-pressure pump 22.
- the high-pressure pump 22 is a device for sending the raw slurry at high pressure.
- the high-pressure pump 22 pressurizes the raw material slurry to about 25 MPa.
- the heat exchange unit 30 heats the raw material slurry by causing heat exchange between the raw material slurry supplied from the raw material supply unit 20 and the processed fluid after being decomposed by the gasification processing unit 40. At the same time, it is a part that cools the processed fluid.
- the heat exchanging unit 30 includes a heat exchanger 31, a decompression mechanism 32, and a cooler 33.
- the heat exchanger 31 is a device that exchanges heat between the raw slurry and the processed fluid, and a double tube type is used.
- the inner channel is used as the low temperature side channel 31a through which the raw material slurry flows, and the outer channel is used as the high temperature side channel 31b through which the processed fluid flows.
- the introduction temperature of the treated fluid is about 600 ° C.
- the discharge temperature is about 120 ° C.
- the introduction temperature of the raw slurry is normal temperature and the discharge temperature is about 450 ° C.
- the heat exchanger 31 will be described later.
- the decompression mechanism 32 is a device that decompresses the processed fluid discharged from the heat exchanger 31, and the cooler 33 is a device that cools the treated fluid discharged from the decompression mechanism 32.
- the treated fluid a mixture of waste water, activated carbon, and ash
- the gasification processing unit 40 is a part that heats and pressurizes the raw material slurry heated by the heat exchanger 31 to a supercritical state, and decomposes organic substances contained in the raw material slurry.
- the preheater 41 and the gasification reactor 42 are connected to each other. Have.
- the preheater 41 is a device for preheating the raw material slurry discharged from the heat exchanger 31, and in this embodiment, the raw material slurry introduced at about 450 ° C. is heated to about 600 ° C.
- the gasification reactor 42 is an apparatus for decomposing organic substances contained in the raw material slurry while maintaining the raw material slurry in a supercritical state. In this embodiment, the temperature is set to 600 ° C. and the pressure is set to 25 MPa, and the raw material slurry is decomposed for 1 to 2 minutes.
- the fuel gas recovery unit 50 is a part that recovers fuel gas from the processed fluid, and includes a gas-liquid separator 51, a flow rate adjusting mechanism 52, and a gas tank 53.
- the gas-liquid separator 51 is a portion that separates the subcritical processed fluid taken out from the middle of the high-temperature channel 31b of the heat exchanger 31 into gas (fuel gas) and liquid (drainage, activated carbon, ash). It is. Then, the separated liquid is returned to the middle of the high temperature side channel 31 b, and the separated gas is supplied to the flow rate adjusting mechanism 52.
- the gas-liquid separator 51 will be described later.
- the flow rate adjusting mechanism 52 is a mechanism for adjusting the flow rate of the gas separated by the gas-liquid separator 51
- the gas tank 53 is a container for storing fuel gas after working in the power generation unit 60.
- the fuel gas stored in the gas tank 53 is supplied as part of the fuel of the preheater 41 and the gasification reactor 42 included in the gasification processing unit 40.
- the power generation unit 60 is a part that generates power using the fuel gas recovered from the processed fluid as power, and includes a turbine 61 and a generator 62.
- the turbine 61 is a device that rotates using the fuel gas separated by the gas-liquid separator 51 as power.
- the turbine 61 of this embodiment rotates when the flow control device injects fuel gas in a high pressure state.
- the generator 62 is a device that generates power as the turbine 61 rotates.
- the heat exchanger 31 is divided into a high temperature side portion 31H and a low temperature side portion 31L.
- a high-temperature and high-pressure state (600 ° C., 25 MPa in this embodiment) treated fluid is introduced into the high temperature side portion 31H, and heat exchange is performed with the raw material slurry discharged from the low temperature side portion 31L.
- normal temperature raw material slurry pressurized by the high-pressure pump 22 is introduced into the low temperature side portion 31L, and heat exchange is performed with the processed fluid (liquid portion) after gas-liquid separation.
- the post-processed fluid heat-exchanged in the high temperature side portion 31H is lowered to a subcritical state while maintaining a high pressure.
- the temperature drops to about 300 ° C. while maintaining a pressure of 25 MPa.
- the treated fluid becomes a subcritical state and changes to a gas-liquid two-phase flow. Therefore, as described above, the post-processed fluid in the subcritical state is taken out from the high temperature side channel 31b of the heat exchanger 31 and separated into gas and liquid by the gas / liquid separator 51.
- FIG. 2A is a longitudinal sectional view of the gas-liquid separator 51.
- the illustrated gas-liquid separator 51 is an airtight container in which an upper end portion 51a and a lower end portion 51b are hemispherical, and an intermediate portion 51c is cylindrical.
- a fluid introduction part 51d and a liquid discharge part 51e are provided on the side surface of the intermediate part 51c.
- the upper end 51a is provided with a gas discharge part 51f
- the lower end 51b is provided with a drain 51g.
- the fluid introduction part 51 d is a tubular member that communicates the inside and outside of the gas-liquid separator 51.
- the outer end of the fluid introduction part 51d is connected to a high temperature side flow path 31b provided in the high temperature side part 31H through a pipe 31c (see FIG. 1).
- the liquid discharge part 51 e is also a tubular member that communicates the inside and outside of the gas-liquid separator 51.
- the outer end part of the liquid discharge part 51e is connected to the high temperature side flow path 31b with which the low temperature side part 31L is provided through the piping 31d (refer FIG. 1).
- the gas discharge part 51f is configured by a pipe whose base end communicates with the internal space of the gas-liquid separator 51, and an open / close valve 51h is provided at the tip thereof. This gas discharge part 51f is connected to the flow control mechanism 52 through piping.
- the drain 51g is also configured by a pipe whose base end communicates with the internal space of the gas-liquid separator 51, and a drain valve 51i is provided at the tip.
- the treated fluid in this internal space is separated into a liquid part (activated carbon, water, ash) and a gas part (fuel gas).
- a gas part raises and becomes fuel gas and flows in into the gas discharge part 51f from the upper end part 51a.
- the fuel gas is supplied to the flow rate adjusting mechanism 52.
- the gas-liquid separator 51 does not adjust the pressure. For this reason, the flow rate adjusting mechanism 52 is supplied with fuel gas having a high pressure of about 25 MPa.
- the flow rate adjustment mechanism 52 rotates the turbine 61 without burning the fuel gas by blowing high-pressure fuel gas onto the turbine 61 while adjusting the flow rate. Since the generator 62 generates electricity by the rotation of the turbine 61, the energy of the pressure of the fuel gas can be converted into electric power.
- the fuel gas after work is stored in the gas tank 53.
- the separated liquid part fills the internal space of the gas-liquid separator 51 from below and is discharged from the liquid discharge part 51e.
- activated carbon and ash are contained in a liquid part, since activated carbon and ash have high specific gravity compared with water, they settle and accumulate in the lower end part 51b of internal space. For this reason, activated carbon and ash can be reduced regarding the liquid part discharged
- activated carbon and ash stored in the gas-liquid separator 51 can be recovered by opening the drain valve 51i.
- the end of the liquid discharge part 51e may be connected to the bottom of the lower end part 51b so that activated carbon and ash are not recovered.
- the liquid portion from which the fuel gas, activated carbon, and ash are removed is discharged from the liquid discharge portion 51e.
- the liquid portion from which the fuel gas, activated carbon, and ash are removed is referred to as a post-processed fluid discharged from the gas-liquid separator 51.
- This post-treatment fluid is used for heating the raw slurry in the low temperature side portion 31L of the heat exchanger 31.
- the post-processed fluid in the subcritical state is the high temperature side channel 31b (outer channel) provided in the high temperature side portion 31H of the heat exchanger 31. It is taken out from the gas and separated into gas and liquid. Since the high-pressure fuel gas that has been gas-liquid separated is used as power for the turbine 61, the pressure energy of the fuel gas can be used effectively. Furthermore, the fuel gas after work can be effectively used as fuel for the gasification processing unit 40.
- the post-process fluid after gas-liquid separation is returned to the high temperature side channel 31b (outer channel) included in the low temperature side portion 31L, the heat exchange efficiency between the returned post-process fluid and the raw material slurry is increased. Can be increased. Furthermore, since tar can be removed in the course of gas-liquid separation, clogging of the heat exchanger 31 due to tar can be suppressed.
- the configuration of the power generation unit 60 is different from the above-described embodiment.
- the raw material adjustment part 10 the raw material supply part 20, the heat exchange part 30, and the gasification process part 40, since it is the same as the above-mentioned embodiment, description is abbreviate
- the power generation unit 60 includes a turbine 61, a generator 62, a gas-liquid separator 63, a flow rate adjustment mechanism 64, and a combustor 65.
- the gas-liquid separator 63 and the flow rate adjusting mechanism 64 have the same configuration as the gas-liquid separator 51 and the flow rate adjusting mechanism 52 in the above-described embodiment.
- the fuel gas after rotating the turbine 61 with pressure is combusted by the combustor 65 and reused as power for the turbine 61.
- the chemical energy which fuel gas has can also be utilized, the turbine 61 can be rotated, and electric power generation can be performed efficiently.
- the gasification raw material after the heat exchange in the heat exchange unit 30 is configured to be heated by the combustion of the fuel gas, but before the heat exchange in the heat exchange unit 30
- the gasification raw material may be heated by combustion of fuel gas.
- the exhaust gas is emitted.
- the exhaust gas may be used as a heating source for the gasification raw material. Since the exhaust gas also has thermal energy, the energy of the fuel gas can be used more effectively.
Abstract
Description
Claims (6)
- ガス化原料を加熱及び加圧して超臨界状態とし、前記ガス化原料を分解処理して燃料ガスを得るガス化装置であって、
前記ガス化原料を低温側流路に導入し、超臨界状態の処理後流体を高温側流路に導入することで、前記ガス化原料と前記処理後流体との間で熱交換を行わせる熱交換器と、
熱交換によって亜臨界状態となった前記処理後流体を前記高温側流路から取り出して気液分離し、分離された液体を前記高温側流路に戻す気液分離器と、
前記気液分離器で分離された燃料ガスを動力とするタービンと、
を有することを特徴とするガス化装置。 - 前記タービンは、高圧状態の前記燃料ガスの噴射によって回転することを特徴とする請求項1に記載のガス化装置。
- 前記タービンは、高圧状態の前記燃料ガスを燃焼させ、その噴射によって回転することを特徴とする請求項1に記載のガス化装置。
- 前記タービンを回転させた後の前記燃料ガスを、前記ガス化原料の加熱に使用することを特徴とする請求項2に記載のガス化装置。
- 前記タービンを回転させた後の前記燃料ガスを燃焼させ、前記タービンの回転に使用することを特徴とする請求項2に記載のガス化装置。
- 前記燃料ガスの燃焼によって得られ、前記タービンの回転に使用した後の排気ガスを、前記ガス化原料の加熱に使用することを特徴とする請求項3,5に記載のガス化装置。
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2015514697A JP5865554B1 (ja) | 2014-03-05 | 2014-03-05 | 超臨界流体によるガス化装置 |
MYPI2016703210A MY181029A (en) | 2014-03-05 | 2014-03-05 | Gasification apparatus with supercritical fluid |
SG11201607317XA SG11201607317XA (en) | 2014-03-05 | 2014-03-05 | Apparatus for gasification with supercritical fluid |
PCT/JP2014/055696 WO2015132923A1 (ja) | 2014-03-05 | 2014-03-05 | 超臨界流体によるガス化装置 |
US15/123,445 US20170066982A1 (en) | 2014-03-05 | 2014-03-05 | Gasification apparatus with supercritical fluid |
EP14884715.5A EP3115441A4 (en) | 2014-03-05 | 2014-03-05 | Apparatus for gasification with supercritical fluid |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2014/055696 WO2015132923A1 (ja) | 2014-03-05 | 2014-03-05 | 超臨界流体によるガス化装置 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2015132923A1 true WO2015132923A1 (ja) | 2015-09-11 |
Family
ID=54054759
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2014/055696 WO2015132923A1 (ja) | 2014-03-05 | 2014-03-05 | 超臨界流体によるガス化装置 |
Country Status (5)
Country | Link |
---|---|
US (1) | US20170066982A1 (ja) |
EP (1) | EP3115441A4 (ja) |
JP (1) | JP5865554B1 (ja) |
SG (1) | SG11201607317XA (ja) |
WO (1) | WO2015132923A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017051365A1 (en) | 2015-09-24 | 2017-03-30 | Reliance Industries Limited | System and process for production of biofuel |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2679330C1 (ru) * | 2017-12-01 | 2019-02-07 | Федеральное государственное бюджетное научное учреждение Федеральный научный агроинженерный центр ВИМ (ФГБНУ ФНАЦ ВИМ) | Энергетический комплекс на основе газификации отходов биомассы |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11262742A (ja) * | 1998-03-19 | 1999-09-28 | Ube Ind Ltd | 廃棄物の処理方法および処理装置 |
JP2001115174A (ja) * | 1999-10-15 | 2001-04-24 | Toshiba Corp | 燃料処理システム |
JP2008249207A (ja) * | 2007-03-29 | 2008-10-16 | Hiroshima Univ | バイオマスガス化発電システム |
JP2009149773A (ja) * | 2007-12-20 | 2009-07-09 | Hiroshima Univ | バイオマスガス化方法、及びバイオマスガス化システム |
JP2010174189A (ja) * | 2009-01-30 | 2010-08-12 | Hiroshima Univ | 燃料ガス製造方法 |
Family Cites Families (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1993002969A1 (en) * | 1991-08-09 | 1993-02-18 | Board Of Regents, The University Of Texas System | High temperature wet oxidation using sintered separators |
US5578647A (en) * | 1994-12-20 | 1996-11-26 | Board Of Regents, The University Of Texas System | Method of producing off-gas having a selected ratio of carbon monoxide to hydrogen |
US5571424A (en) * | 1995-02-27 | 1996-11-05 | Foster Wheeler Development Corporation | Internal platelet heat source and method of use in a supercritical water oxidation reactor |
JP4683748B2 (ja) * | 2001-03-07 | 2011-05-18 | ヤンマー株式会社 | 超臨界水又は亜臨界水による被反応物質の反応装置 |
US6519926B2 (en) * | 2001-05-01 | 2003-02-18 | General Atomics | Hydrothermal conversion and separation |
US20040221507A1 (en) * | 2003-05-07 | 2004-11-11 | Wu Benjamin C. | Method and apparatus for providing hydrogen |
US8579996B2 (en) * | 2007-07-27 | 2013-11-12 | Ignite Energy Resources Pty Ltd | Process and apparatus for converting organic matter into a product |
US8132410B2 (en) * | 2007-12-17 | 2012-03-13 | Battelle Energy Alliance, Llc | Methods and systems for the production of hydrogen |
US20090206007A1 (en) * | 2008-02-20 | 2009-08-20 | Air Products And Chemicals, Inc. | Process and apparatus for upgrading coal using supercritical water |
US20130192971A1 (en) * | 2009-01-21 | 2013-08-01 | Michael C. Cheiky | Biomass reactor |
AU2010250769A1 (en) * | 2009-05-20 | 2011-12-08 | Ramot At Tel-Aviv University Ltd. | Catalytic gasification of organic matter in supercritical water |
US20120039430A1 (en) * | 2010-08-16 | 2012-02-16 | Abel Cal R | Nuclear powered facility that generates consumable fuels |
US8367881B2 (en) * | 2011-05-09 | 2013-02-05 | Cool Planet Biofuels, Inc. | Method for biomass fractioning by enhancing biomass thermal conductivity |
US8173044B1 (en) * | 2011-05-09 | 2012-05-08 | Cool Planet Biofuels, Inc. | Process for biomass conversion to synthesis gas |
US8568493B2 (en) * | 2011-07-25 | 2013-10-29 | Cool Planet Energy Systems, Inc. | Method for producing negative carbon fuel |
NL1039007C2 (en) * | 2011-08-26 | 2013-02-27 | Klaas Gerrit Smit | A process and a reaction apparatus for the gasification of wet biomass. |
US9024096B2 (en) * | 2012-12-11 | 2015-05-05 | Lummus Technology Inc. | Conversion of triacylglycerides-containing oils |
US9376639B2 (en) * | 2013-03-15 | 2016-06-28 | Terrapower, Llc | Method and system for performing gasification of carbonaceous feedstock |
CN105143412B (zh) * | 2013-03-20 | 2017-03-08 | 英派尔科技开发有限公司 | 通过播种牺牲金属的超临界水气化的腐蚀减轻 |
US20150191653A1 (en) * | 2014-01-09 | 2015-07-09 | Cool Planet Energy Systems, Inc. | Apparatus, system, and method for biomass fractioning |
-
2014
- 2014-03-05 JP JP2015514697A patent/JP5865554B1/ja active Active
- 2014-03-05 WO PCT/JP2014/055696 patent/WO2015132923A1/ja active Application Filing
- 2014-03-05 EP EP14884715.5A patent/EP3115441A4/en not_active Withdrawn
- 2014-03-05 US US15/123,445 patent/US20170066982A1/en not_active Abandoned
- 2014-03-05 SG SG11201607317XA patent/SG11201607317XA/en unknown
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11262742A (ja) * | 1998-03-19 | 1999-09-28 | Ube Ind Ltd | 廃棄物の処理方法および処理装置 |
JP2001115174A (ja) * | 1999-10-15 | 2001-04-24 | Toshiba Corp | 燃料処理システム |
JP2008249207A (ja) * | 2007-03-29 | 2008-10-16 | Hiroshima Univ | バイオマスガス化発電システム |
JP2009149773A (ja) * | 2007-12-20 | 2009-07-09 | Hiroshima Univ | バイオマスガス化方法、及びバイオマスガス化システム |
JP2010174189A (ja) * | 2009-01-30 | 2010-08-12 | Hiroshima Univ | 燃料ガス製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP3115441A4 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2017051365A1 (en) | 2015-09-24 | 2017-03-30 | Reliance Industries Limited | System and process for production of biofuel |
EP3352928A4 (en) * | 2015-09-24 | 2019-06-12 | Reliance Industries Limited | SYSTEM AND METHOD FOR PRODUCING BIOFUEL |
Also Published As
Publication number | Publication date |
---|---|
JP5865554B1 (ja) | 2016-02-17 |
EP3115441A4 (en) | 2017-02-15 |
JPWO2015132923A1 (ja) | 2017-03-30 |
SG11201607317XA (en) | 2016-10-28 |
EP3115441A1 (en) | 2017-01-11 |
US20170066982A1 (en) | 2017-03-09 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DK2507346T3 (en) | DEVICE AND PROCEDURE FOR THERMOCHEMICAL HARMONIZATION AND GASATION OF MOISTURIZED BIOMASS | |
JP6573261B2 (ja) | 超臨界水ガス化システム | |
JP2006274013A (ja) | バイオマスガス化システム | |
JP6250293B2 (ja) | 超臨界水によるバイオマスガス化システム及びその運転方法 | |
JP6070906B1 (ja) | 超臨界水ガス化システムおよびガス化方法 | |
JP6488364B2 (ja) | 超臨界水ガス化システム | |
JP5865553B1 (ja) | 超臨界流体によるガス化装置 | |
WO2015132923A1 (ja) | 超臨界流体によるガス化装置 | |
JP6057362B1 (ja) | 超臨界水ガス化システム | |
JP6066411B2 (ja) | 活性炭によるバイオマスの超臨界水ガス化システムの運転方法 | |
JP6338080B2 (ja) | 超臨界水によるバイオマスガス化システム | |
JP5007999B2 (ja) | 気液分離器 | |
JP6127215B2 (ja) | ガス化システム | |
JP6364645B2 (ja) | バイオマス処理システム | |
JP6020951B1 (ja) | ガス化システム、及びガス化システムにおけるガス化方法 | |
JP5859713B1 (ja) | バイオマスガス化システムおよびバイオマスガス化方法 | |
WO2020217398A1 (ja) | 超臨界水ガス化システム | |
WO2016063399A1 (ja) | 超臨界流体によるガス化装置、及びガス化方法 | |
JP2019196452A (ja) | 改質炉およびそれを用いたガス化システム | |
JP6671677B1 (ja) | 超臨界水ガス化システム | |
JP2013006938A (ja) | バイオマススラリーをガス化する超臨界水ガス化システム |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
ENP | Entry into the national phase |
Ref document number: 2015514697 Country of ref document: JP Kind code of ref document: A |
|
REEP | Request for entry into the european phase |
Ref document number: 2014884715 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 15123445 Country of ref document: US Ref document number: 2014884715 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: IDP00201606623 Country of ref document: ID |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 14884715 Country of ref document: EP Kind code of ref document: A1 |