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WO2005093014A1 - Procédé pour retirer le goudron dans un four à couche fluidisée - Google Patents

Procédé pour retirer le goudron dans un four à couche fluidisée Download PDF

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Publication number
WO2005093014A1
WO2005093014A1 PCT/JP2005/005388 JP2005005388W WO2005093014A1 WO 2005093014 A1 WO2005093014 A1 WO 2005093014A1 JP 2005005388 W JP2005005388 W JP 2005005388W WO 2005093014 A1 WO2005093014 A1 WO 2005093014A1
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WO
WIPO (PCT)
Prior art keywords
particles
alumina
fluidized bed
tar
silica
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2005/005388
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English (en)
Japanese (ja)
Inventor
Naoki Fujiwara
Tsuyoshi Teramae
Takayuki Takarada
Hiroshi Moritomi
Tadaaki Shimizu
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Idemitsu Kosan Co Ltd
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Idemitsu Kosan Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Idemitsu Kosan Co Ltd filed Critical Idemitsu Kosan Co Ltd
Publication of WO2005093014A1 publication Critical patent/WO2005093014A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0072—Preparation of particles, e.g. dispersion of droplets in an oil bath
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/12—Silica and alumina
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
    • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/06—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by pressure distillation
    • C10G9/08—Apparatus therefor
    • C10G9/12—Removing incrustation
    • 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
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10K3/02—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 by catalytic treatment
    • C10K3/023—Reducing the tar content
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • 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
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to a method for removing tar in a fluidized bed furnace in a system for gasifying fossil fuels such as coal and heavy oil, biomass, and the like to generate a fuel gas and a chemical raw material gas.
  • Gasifiers for coal and the like are roughly classified into three types: a spouted bed gasifier, a fluidized bed gasifier, and a fixed bed gasifier.
  • a spouted bed gasifier coarse pulverized coal with an average particle size of 16 mm is used.
  • pulverized coal is fluidized by oxygen or air, which is a gasifying agent, and water vapor, and conversion into CO, CO, and H proceeds in the furnace.
  • Tar treatment methods in fluidized bed gasification include (1) a method in which the gasification temperature is raised to 900 ° C or more, and (2) a tar decomposition catalyst component such as nickel molybdenum is charged or fluidized into a furnace. (3) A adsorptive substance such as alumina, zeolite, limestone, etc. is placed in the furnace, or is charged as a fluid medium, adsorbs tar, and is decomposed in a regeneration furnace such as a combustion furnace. Methods have been studied.
  • the method (1) reduces the cold gas efficiency and increases energy loss
  • the method (2) requires a price of nickel molybdenum used as a decomposition catalyst component impregnated into particles such as alumina. Is expensive, and the particles are easily crushed due to wear due to fluidization of the particles, and the gasification furnace power is also scattered outside the system, or the decomposition effect is reduced due to the carbon content precipitated on the particle surface. Therefore, the method (3), which requires the replenishment of particles and is less economical, regenerates particles by decomposition and combustion of carbon and other substances by using adsorbent particles such as alumina and zeolite without using expensive decomposition catalysts. To some extent, but adsorbable particles • The carbon content resolution is low, and the fine particles are granulated.
  • the present invention has been made in view of the above circumstances, and has as its object to provide an excellent method for removing tar in a fluidized bed furnace. Another object of the present invention is to provide a method for removing tar in a fluidized bed furnace having high cold gas efficiency.
  • the present inventors have conducted intensive studies to achieve the above object, and as a result, in order to improve cold gas efficiency, set the gasification temperature to a low temperature (for example, 600 ° C or more and less than 900 ° C).
  • a low temperature for example, 600 ° C or more and less than 900 ° C.
  • a regeneration furnace such as a combustion furnace.
  • specific adsorbent particles for example,
  • tar generated from the raw material is subjected to fluid catalytic cracking.
  • Catalyst, fluid catalytic cracking equilibrium catalyst adsorbs and decomposes using silica-alumina-based particles or alumina-based particles produced by oil immersion granulation, and z or fluid catalytic cracking catalyst, fluid catalytic cracking equilibrium catalyst,
  • a method for removing tar in a fluidized bed furnace which comprises attaching and burning silica-alumina-based particles or alumina-based particles produced by an oil immersion granulation method.
  • the raw material power is also generated.
  • Adsorbed particles to adsorb and decompose the tar, and adhere to Z or adsorbent particles for combustion A method for removing tar in a fluidized bed furnace is provided.
  • an excellent method for removing tar in a fluidized bed furnace can be provided. Further, it is possible to provide a method for removing tar in a fluidized-bed furnace having high cold gas efficiency.
  • FIG. 1 is a schematic diagram of a publishing type fluidized bed gasification furnace.
  • fluidized bed is synonymous with “fluidized bed”.
  • the raw material used in the method of the present invention is not particularly limited, and for example, fossil raw materials such as petroleum, coal, and coats, waste, biomass, and the like can be used.
  • biomass particularly woody biomass, is preferred.
  • the fluidized bed furnace is not particularly limited.
  • a fluidized bed furnace that processes a publishing type fluidized bed, an external / internal circulation type fluidized bed, a pressurized type / normal pressure type fluidized bed, or the like is used.
  • it is a fluidized bed furnace using a publishing type fluidized bed as a process.
  • conditions for gasifying, thermally decomposing, or partially oxidizing the raw material can be appropriately adjusted according to the type of the raw material and the like.
  • the raw material is gasified at a low temperature.
  • it is gasified at a low temperature of less than 900 ° C, more preferably 850 ° C or less. Further, it is usually gasified at a temperature of 500 ° C or higher, preferably 550 ° C or higher.
  • tar produced by the above-mentioned raw material power is adsorbed and decomposed using adsorptive particles to remove tar.
  • examples of the adsorptive particles include fluid catalytic cracking catalyst (FCC catalyst) particles, fluid catalytic cracking equilibrium catalyst (FCC equilibrium catalyst) particles, silica-alumina particles, and alumina produced by an oil immersion granulation method.
  • Based particles porous alumina, activated alumina, ⁇ -alumina, activated bokeh Site
  • silica-based particles such as silica gel, raw concrete sludge and its sludge cake, particles of lime cake, concrete, concrete structures and waste of concrete structures, and clay mineral particles such as activated clay, zeolite, and sepiolite.
  • the adsorptive particles include used adsorptive particles or a catalyst containing the adsorptive particles.
  • the used catalyst means a catalyst used in a process that is the original purpose of the catalyst such as a desulfurization reaction of petroleum fraction and discarded due to a decrease in desulfurization reaction activity and the like.
  • These used catalysts can be used as they are, or they can be used by burning and regenerating adhering carbonaceous materials, and by washing and removing precipitated metal components with an acid or the like.
  • adsorptive particles FCC catalyst particles, FCC equilibrium catalyst particles, silica-alumina-based particles, and alumina-based particles produced by an oil immersion granulation method are preferable.
  • porous alumina or activated alumina produced by an oil immersion granulation method is preferable.
  • the oil immersion granulation method is a method of immersing mainly hydroxylated aluminum converted into a hydrogel in a heated roll bath and granulating into spherical particles by surface tension.
  • the fluid catalytic cracking catalyst is a catalyst for catalytically cracking heavy oil (such as vacuum gas oil or atmospheric residual oil) to produce gasoline with a high octane number.
  • Metal oxides such as silica 'alumina, titanium, and alumina' titanium; clay minerals such as kaolin and bentonite; various zeolites; 'Examples include porous particle FCC catalysts prepared by a method such as spray drying using alumina, rare earth-substituted Y zeolite, kaolin, or the like.
  • Fluid catalytic cracking equilibrium catalyst is a catalyst that is periodically withdrawn when the catalytic activity of the FCC unit becomes constant. Etc.), the metals such as iron, vanadium and nickel accumulated on the above FCC catalyst.
  • vanadium and Z or nickel on the particle surface are 500-15000 mass ppm
  • FCC equilibrium catalysts that have accumulated FCC and have a vanadium and / or Z or nickel accumulation of 800-5000 ppm by mass!
  • a new catalyst is added at appropriate times in order to keep the activity of the FCC catalyst constant. It is completely mixed with a certain catalyst, and the activity of the catalyst will be averaged. However, since the amount of catalyst in the equipment would be excessive if it was not used, a certain amount was always extracted.
  • tar can be adsorbed and decomposed by pre-filling these adsorbed particles in a fluidized-bed furnace or charging them into a fluidized-bed furnace.
  • tar can also be adsorbed and decomposed by using these adsorbed particles as a fluid medium and a circulating medium (circulating solid) of a fluidized bed furnace.
  • these adsorptive particles when using a fluidized bed furnace that processes a publishing type fluidized bed and an internal circulation type fluidized bed, these adsorptive particles can be used as a fluidized medium.
  • these adsorptive particles can be used as a circulating medium.
  • tar can be adsorbed and decomposed in a fluidized bed furnace (for example, a freeboard portion or the like).
  • the conditions for scattering the adsorptive particles can be appropriately adjusted according to the type of the fluidized bed and the adsorptive particles.
  • tar produced by the above-mentioned raw material force is attached to the above-mentioned adsorptive particles and burned, whereby tar can be removed.
  • the combustion of the attached tar can be performed in the combustion zone in the fluidized bed furnace.
  • the tar can be continuously removed by adsorbing and decomposing the tar using the adsorptive particles and further burning the adhered tar remaining without being decomposed by the adsorptive particles. it can.
  • the adsorbable particles since the adsorbable particles are regenerated in the combustion region by the combustion of the attached tar, the adsorbable particles can be used continuously.
  • the method of the present invention is efficient because the heat of combustion can be used as a gasification heat source.
  • gasified gas generated by the combustion of raw materials and fuel generated by the combustion of tar Since the combustion gas is separated, the gasification gas becomes a high-calorie gas.
  • a lab-type publishing type fluidized-bed gasification furnace 1 shown in FIG. 1 was used.
  • This apparatus 1 is composed of a gasifier 2, a dispersion plate 4, and a wind box 6.
  • This apparatus 1 is cylindrical and made of stainless steel with an inner diameter of 100 mm and a height of 1.5 m (the disperser 4 is also up to the furnace outlet 8).
  • an electric furnace 10 for controlling the gasification temperature is installed outside the device 1. Nitrogen gas is used as the gasification gas at a flow rate of 6 liters Z, from the gas inlet 12 through the gas preheater 14 equipped with a gas preheating function, the wind box 6, and the disperser 4, Feeded to 2.
  • the apparatus 1 was previously filled with particles (particles A to E) having a height of 150 mm as a fluid medium 16 on a dispersion plate 4.
  • the fluid medium 16 flows and scatters inside the gasification furnace 2 by the gas gas supplied through the dispersion plate 4.
  • a raw material feeder 18 provided outside the apparatus 1 is heated.
  • the raw material and the particles were supplied quantitatively from the feeder and the particle feeder 20, respectively.
  • the gasified product gas and tar are discharged to the outside through the furnace outlet 8 at the upper part of the gasification furnace, and a part of the gas and tar is introduced into the organic solvent (ethanol) for tar recovery in the tar recovery unit 22. , Completely recovered.
  • the amount of the collected tar sample was measured by a combination of GC-FID and desolvation residue method.
  • the raw material is wood biomass (cedar: carbon content 48.7%, hydrogen content 5.8%, oxygen content 40.2%, ash content 0.4%, moisture 4.9%), particle size 200—300 / zm And supplied at a flow rate of 5 gZ.
  • the total amount of the fluid medium particles was adjusted to a particle size of lmm or less and supplied at a flow rate of 60 gZ.
  • Particle A Alumina particles produced by the oil immersion granulation method
  • the injection rate of the aqueous solution of aluminum sulfate was set to about 102 mlZmin, and the injection rate of the aqueous solution of sodium aluminate was set to 23.3 mlZmin.
  • the mixture was simultaneously mixed with a metering pump under high shear.
  • the target basic aluminum sulfate hydrosol molar ratio (SO ZA1 O) is 0.9
  • a circulating system of the mixture was formed under high shear so as to obtain 2, and 546 g of an aqueous solution of sodium aluminate was added thereto and mixed at an injection rate of 2. OmlZmin.
  • the prepared basic aluminum sulfate hydrosol is further aged for 20 days at room temperature with stirring and aging to promote polymerization and increase the viscosity of the basic aluminum sulfate hydrosol to prepare a concentrated ammonia monosalt in advance.
  • PH buffer solution of ammonium chloride (NH Cl: 70g and concentrated
  • aqueous ammonia Approximately 500 ml of aqueous ammonia was ion-exchanged and hydrogenated, and the basic aluminum hydrosol was extruded with a syringe into a buffer solution (pH 9.84), adjusted to a total volume of 1 liter, and hydrogelated at room temperature.
  • a columnar transparent alumina hydrogel was prepared. After washing with water and drying, it was calcined at 600 ° C. for 3 hours to obtain transparent activated alumina particles.
  • the crystalline state of the particle A (600 ° C. for 3 hours) is amorphous, the BET specific surface area is 274 m 2 Zg, and the pore area is 0.37 ml / g.
  • Particle B silica 'alumina particles (Neobead SA manufactured by Mizusawa I-Dagaku Kogyo Co., Ltd.)
  • Particle C FCC equilibrium catalyst
  • Particle D Limestone (made by Taiheiyo Cement, crushed product of 1 mm or less)
  • Particle E Alumina particles manufactured by powder granulation method (GB, manufactured by Mizusawa Chemical Industry Co., Ltd.)
  • the powder granulation method involves drying and pulverizing a hydrogel, followed by extrusion or fluidization. It refers to a method of molding and flowing.
  • Example 1-9 Comparative Example 1-6
  • the particle ratio was determined when the particles A, B, D and E were used. Table 2 shows the results.
  • the powdering rate was as follows. The force of the following formula was also calculated, where d is the weight and e is the weight of the particles initially charged.
  • the method of the present invention is suitable for use in a field of energy and a field of research using a system for producing gas for fuel and gas for chemical raw materials.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Industrial Gases (AREA)
  • Catalysts (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

Procédé pour retirer le goudron dans un four à couche fluidisée qui comprend la soumission dans un système où un matériau brut est gazéifié, pyrolysé ou partiellement oxydé pour former un gaz objectif, d'un goudron formé á partir du matériau brut á l'absorption et á la décomposition par l'usage d'un catalyseur fluidisé de criquage, un catalyseur fluidisé d'équilibre de criquage, des particules à base de silice-albumine ou des particules à base d'alumine préparées par le procédé de granulation d'immersion d'huile, et/ou à la fixation à un catalyseur fluidisé de criquage, un catalyseur d'équilibre de criquage fluidisé, des particules à base de silice-albumine ou des particules à base d'alumine préparées par le procédé de granulation par immersion d'huile et au chalumeau
PCT/JP2005/005388 2004-03-26 2005-03-24 Procédé pour retirer le goudron dans un four à couche fluidisée Ceased WO2005093014A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2004092275A JP4505247B2 (ja) 2004-03-26 2004-03-26 流動層炉におけるタールの除去方法
JP2004-092275 2004-03-26

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Publication Number Publication Date
WO2005093014A1 true WO2005093014A1 (fr) 2005-10-06

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JP (1) JP4505247B2 (fr)
CN (1) CN1934230A (fr)
WO (1) WO2005093014A1 (fr)

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JP2005272782A (ja) * 2004-03-26 2005-10-06 Idemitsu Kosan Co Ltd 流動層炉におけるタールの除去方法
WO2007064014A1 (fr) * 2005-11-30 2007-06-07 Nippon Oil Corporation Carburant et son procede de production
JP2007153924A (ja) * 2005-11-30 2007-06-21 Nippon Oil Corp 流動接触分解を用いたバイオマスの処理方法
JP2007153939A (ja) * 2005-11-30 2007-06-21 Nippon Oil Corp 液化燃料ガス組成物
JP2007153925A (ja) * 2005-11-30 2007-06-21 Nippon Oil Corp 流動接触分解を用いたバイオマスの処理方法
JP2007177193A (ja) * 2005-11-30 2007-07-12 Nippon Oil Corp 流動接触分解を用いたバイオマスの処理方法
JP7017747B1 (ja) 2021-09-08 2022-02-09 シンエネルギー開発株式会社 バイオマス発電方法、バイオマス発電の情報管理方法、バイオマス発電システム、及びバイオマス発電の外販商品の販売方法

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JP5679160B2 (ja) * 2010-07-12 2015-03-04 バイオコーク技研株式会社 炭素担持体、炭素担持体製造方法、炭素担持体製造装置、ガス生成方法、ガス生成装置、発電方法及び発電装置
WO2012037164A1 (fr) * 2010-09-13 2012-03-22 Conocophillips Company Élimination de goudron tolérant au soufre à basse température avec conditionnement concomitant de gaz de synthèse
CN108525511B (zh) * 2018-02-07 2019-04-26 山东荣信集团有限公司 一种可凝性有机物净化处理系统
JP7118341B2 (ja) * 2020-08-07 2022-08-16 株式会社堤水素研究所 水素製造装置
PH12023552844A1 (en) * 2021-04-14 2024-05-20 Revo Int Inc Organic feedstock decomposition method, and method for manufacturing liquid fuel, solid fuel, or activated carbon using same
KR102653928B1 (ko) * 2022-01-05 2024-04-02 한국에너지기술연구원 타르 개질기 일체형 가스화기
KR102541598B1 (ko) * 2022-03-03 2023-06-13 한국화학연구원 중질유분 분해용 촉매 및 이를 이용한 중질유분의 경질화 방법

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JP7017747B1 (ja) 2021-09-08 2022-02-09 シンエネルギー開発株式会社 バイオマス発電方法、バイオマス発電の情報管理方法、バイオマス発電システム、及びバイオマス発電の外販商品の販売方法
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