JP4243295B2 - Low-temperature catalytic gasification apparatus and method for biomass refined fuel - Google Patents

Low-temperature catalytic gasification apparatus and method for biomass refined fuel Download PDF

Info

Publication number
JP4243295B2
JP4243295B2 JP2006535283A JP2006535283A JP4243295B2 JP 4243295 B2 JP4243295 B2 JP 4243295B2 JP 2006535283 A JP2006535283 A JP 2006535283A JP 2006535283 A JP2006535283 A JP 2006535283A JP 4243295 B2 JP4243295 B2 JP 4243295B2
Authority
JP
Japan
Prior art keywords
catalyst
gasification
tar
fuel
gas
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.)
Active
Application number
JP2006535283A
Other languages
Japanese (ja)
Other versions
JP2007506856A (en
Inventor
カン,サン−キュ
シン,ヒュン−ドン
Original Assignee
コリア インスティテュート オブ エナジー リサーチ
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
Priority to KR1020040061657A priority Critical patent/KR100569120B1/en
Application filed by コリア インスティテュート オブ エナジー リサーチ filed Critical コリア インスティテュート オブ エナジー リサーチ
Priority to PCT/KR2005/001808 priority patent/WO2006031011A1/en
Publication of JP2007506856A publication Critical patent/JP2007506856A/en
Application granted granted Critical
Publication of JP4243295B2 publication Critical patent/JP4243295B2/en
Application status is Active legal-status Critical
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/54Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56Apparatus; Plants
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/48Apparatus; Plants
    • C10J3/482Gasifiers with stationary fluidised bed
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/54Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72Other features
    • C10J3/82Gas withdrawal means
    • C10J3/84Gas withdrawal means with means for removing dust or tar from the gas
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • C10K1/024Dust removal by filtration
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • C10K1/026Dust removal by centrifugal forces
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/04Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/046Reducing the tar content
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/08Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/08Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/16Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
    • C10K1/18Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/20Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00Modifying 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
    • C10K3/02Modifying 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
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00Modifying 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
    • C10K3/02Modifying 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
    • C10K3/023Reducing the tar content
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/02Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the alkali- or alkaline earth metals or beryllium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/32Manganese, technetium or rhenium
    • B01J23/34Manganese
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74Iron group metals
    • B01J23/745Iron
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74Iron group metals
    • B01J23/75Cobalt
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/78Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali- or alkaline earth metals
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/04Mixing
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02Processes for making hydrogen or synthesis gas
    • C01B2203/0266Processes for making hydrogen or synthesis gas containing a decomposition step
    • C01B2203/0272Processes for making hydrogen or synthesis gas containing a decomposition step containing a non-catalytic decomposition step
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00Details of gasification apparatus
    • C10J2200/15Details of feeding means
    • C10J2200/158Screws
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/0916Biomass
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/093Coal
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/0946Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0956Air or oxygen enriched air
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0973Water
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983Additives
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983Additives
    • C10J2300/0989Hydrocarbons as additives to gasifying agents to improve caloric properties
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846Partial oxidation, i.e. injection of air or oxygen only
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861Heat exchange between at least two process streams
    • C10J2300/1869Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861Heat exchange between at least two process streams
    • C10J2300/1884Heat exchange between at least two process streams with one stream being synthesis gas
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861Heat exchange between at least two process streams
    • C10J2300/1892Heat exchange between at least two process streams with one stream being water/steam
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of products other than chlorine, adipic acid, caprolactam, or chlorodifluoromethane, e.g. bulk or fine chemicals or pharmaceuticals
    • Y02P20/52Improvements relating to the production of products other than chlorine, adipic acid, caprolactam, or chlorodifluoromethane, e.g. bulk or fine chemicals or pharmaceuticals using catalysts, e.g. selective catalysts

Description

  The present invention relates to a gasification technique for using biomass containing a small amount of inorganic ash and containing a relatively large amount of nitrogen as a clean fuel for district heating in a large city.

  In particular, the present invention relates to an apparatus and a manufacturing method for producing a gas fuel by purifying a substance obtained by refining and mixing biomass organic waste / heavy oil / coal (SOCA: Sludge-Oil-Coal Agglomerates) into gas fuel.

  Here, purified gas fuel means clean gas fuel that can be used in gas power generators or heat-utilizing equipment such as gas engines, gas turbines, steam turbine integrated power generation, fuel cells, boilers, etc. Biomass is a generic term for organic solid materials such as sewage sludge and pulp sludge, industrial waste or household waste, domestic waste such as manure, agricultural waste, livestock manure or cut wood.

  Gasification technology started in the early days for the purpose of producing convenient gas fuel or synthesis gas from a coal mass in the absence of catalyst, and in recent years it has been in the direction of spouted bed gasification and catalytic gasification for most pulverized coal. Evolving.

  Since then, fluidized catalyst gasification using fluidized bed combustion technology has been started for the purpose of heavy oil reforming and gradually applied to coal and biomass gasification. It has been promoted to the plan of the conversion.

  Solid fuel is converted to combustible gases, condensable liquid / tar, solid residues, etc. by gasification with reactive substances such as air, oxygen and steam. In general, gasification maximizes the conversion from solid fuel to gas fuel, but it has limited application in partial gasification processes. In addition, pyrolysis is different from gasification, which means thermal decomposition in an inert atmosphere. However, in the initial stage of gasification, it is in a thermal decomposition state where it is first devolatilized. At this time, the fuel is broken down into char and volatile components. After such devolatilization, a product having a final component distribution of gasification can be obtained by a secondary reaction between the char and the gas component. In fact, product distribution maps are greatly influenced by gasification methods and operating conditions.

In high-temperature gasification, most of the inorganic substances contained in coal or sludge are generated as ash or slag, and inorganic substances such as iron or sodium are volatilized at 900 ° C or higher and the wall surface of the heat exchanger. And so on. Nitrogen (Fuel-N) contained in the fuel changes to NH 3 , HCN, N 2, etc. during the gasification process, but this varies depending on the gasification reactor, fuel properties, operating conditions, and the like.

Coal gasification is generally carried out at high temperatures and requires a lot of energy, which is why the system is bloated because the resulting gas has a low calorific value but the ash is in a molten state Or it is generally complicated. However, the use of a catalyst can improve the gas composition and operating conditions, etc., but the gas composition at the time of non-catalytic high-temperature gasification can be obtained even at a relatively low temperature, which is useful for the conversion of Fuel-N it can. According to some reports, the conversion of Fuel-N to NH 3 and HCN varies depending on the catalyst material and reaction temperature as follows. In the former case, the Fe and Ni catalysts are good at 900 ° C. or higher. In the latter, it was reported that dolomite catalyst and the like were good at 800 ° C. or higher.

Gasified gas usually has a low calorific value, but LNG has a calorific value of about 10,000 kcal / Nm 3 , whereas if coal with a calorific value of 6,850 kcal / kg is gasified, A gas having a low calorific value of 1,100 to 1,450 kcal / Nm 3 is obtained.

  In low temperature non-catalytic gasification of coal, the conversion rate is low, so it is actually operated above the melting temperature of ash. However, in the gasification of biomass with low ash content, high-grade fuel can be obtained by reducing the NO conversion of Fuel-N at a low temperature at which ash slagging does not occur by catalytic gasification.

  On the other hand, this method has been tried for fuels mixed with gasification or coal such as waste or heavy oil with high calorific value. In particular, in the case of waste containing chlorine-based ions, when it is incinerated directly after the step of removing it or gasification, it is designed to stay at a temperature of 1200 ° C. or more for 2 seconds or more. In the case of high-grade polymer waste, there is also a special gasification process that produces high-grade fuel such as hydrogen.

  However, special gasifiers contain a large amount of impurities such as ash in their raw materials, so facilities for removing and purifying them are required, and the temperature must be increased to increase the gasification conversion rate when there is no catalyst. As a result, molten ash is generated, and a quenching system that generates fine slag is required. In addition, since pure oxygen or an air separation device is used to obtain a high calorific value gas, the operating cost or installation cost becomes high. In the gasification of raw materials with a low calorific value, a system that performs indirect heating by an external heat source and thermal decomposition that flows in only steam is installed, and is used for special purposes that do not consider economics.

Therefore, the disadvantage of the non-catalytic partial oxidation process is that expensive pure oxygen or concentrated oxygen must be used to perform a high-temperature gasification reaction, and high-quality product gases (mainly CO and H 2 ) are obtained. Therefore, an expensive heat-resistant material suitable for high-temperature reaction must be used because of the additional fuel consumption. In addition, the useful life of the reactor is shortened. In addition, about 2 to 5% of the glass carbon by high temperature partial combustion using a fixed bed reactor is deposited, the reaction efficiency gradually decreases, and additional costs are required to remove it.

  A circulating low-temperature catalytic gasification reactor can be applied to a relatively clean solid fuel that generates little tar or char. Organic matter hydrocarbons and water vapor are converted to product gas on the oxide catalyst (MO), where the catalyst is also reduced and converted to pure metal (M). The metal (M) having reduced activity as a catalyst is regenerated again into metal oxide (MO) in the combustion reactor. Catalytic reaction also proceeds at a low temperature of about 400 to 600 ° C. and has a feature that the liquid product can be extremely reduced. However, it is limited to be applied to waste containing a large amount of ash or containing a catalyst poison component. It will be a thing.

As such a cyclic reaction reforming catalyst, Ni and Co catalysts are generally used, and V, Cr, Fe, Cu, Mo, Ag, Cd, La, Ce, Perovskite, etc. are also used, but more efficient. As the catalyst, precious metal catalysts such as Rh and Ru are also used, and these are supported on a support in which two or more kinds of oxides such as Mg, Ca, Sr, Ba, Al, Ce, Si, Ti, and Zr are combined. It is common. However, since these catalysts are less active due to catalyst poisons at low temperatures, they tend to be used stably through high temperature reactions or regeneration. At this time, the liberated carbon powder precipitates to block the catalyst surface or react with the support to form other products. For example, there is a drawback that Ni catalyst reacts with alumina at a high temperature to form NiAl 2 O 4 and the like and the activity is lowered. In order to prevent this, high-temperature-resistant hexaaluminate (Hexaaluminate, MeO.6Al 2 O 3 ) may be used.

  In the case of liquid waste containing a large amount of solid impurities such as heavy metals, a gasification reaction may be attempted in a supercritical state by mixing a catalyst into the reactor. As a catalyst to be used, Ru, Pd, R, Pt, Au, Ir, Os, Fe, Ni, Ce, Mn, etc. are impregnated in high temperature resistant titania or zirconia, and in a state of 250 to 600 ° C. and 5 to 130 MPa. You may have driven. The catalyst used at this time is an expensive noble metal and is recovered by a gas-liquid separator and reused.

  Since the solid-solid catalytic reaction is unlikely to actually occur, coal catalyst gasification using an alkali metal impregnated with an alkali catalyst component or containing a large amount of ash was initially developed. The char gasification reaction of coal is found to be generated after fine volatilization occurs on the particle surface, and the solid catalyst is mixed with the coal and reacted. In the case of subbituminous coal, which has a relatively large amount of volatile substances, potassium carbonate was used as a catalyst. However, gasification characteristics differ depending on the solid substances contained in the ash. In general, potassium catalysts have a large difference in activity due to the anions bound to them, iron ions are easily reduced by sulfur, nickel ions have low catalytic activity due to catalyst poisoning, but poisonous substances are not. High catalytic activity is restored at high desorption temperatures.

Utilizing such catalyst characteristics, as a more optimized catalyst configuration, K 2 SO 4 + FeSO 4 or K 2 SO 4 + Ni (NO 3 ) 2 or K 2 SO 4 + CaCO 3 catalyst is used. Operation with a high gasification reaction rate was possible at a relatively low temperature of 850 ° C. However, since the conversion rate is not so high, complicated equipment such as melting residual ash is required.

Among the two-stage gasification methods, in order to obtain a gas product with an intermediate calorific value, air gasification is performed inside the cylindrical reactor and steam gasification is performed outside at about 850 ° C. , Sulfur poisoning in coal was considered using limestone as a catalyst. The reaction at this time occurs as follows.
H 2 S + CaO → CaS + H 2 O

  The solid material generated at this time can separate CaS, CaO, limestone, etc. from the reactor due to the density difference, and separates ash and limestone at the bottom of the reactor. Is complicated, so precise operation is required.

  FIG. 1 shows a conventional biomass non-catalytic high-temperature two-stage gasifier. As shown in the figure, a conventional biomass two-stage pyrolysis facility transfers biomass fuel from a fuel hopper 101 to a circulating fluidized heating furnace 102. Then, it is transferred to the gas reforming furnace 105 through the cyclone 103 and the char separator 104 and subjected to two-stage pyrolysis. After that, the fuel gas passes through the preheating device 106 and the gas quencher 107, once again collects fly ash with the dust collector 108, and purifies the purified gas with the purifier 109.

  In this apparatus, in consideration of high-temperature volatilization of heavy metals, etc., the first stage pyrolysis is carried out at a relatively low temperature of 450 to 850 ° C. in the absence of a catalyst, so the gasification yield is low and tar generation is excessive. Therefore, tar reforming is necessary to increase the gasification yield, but this is performed at 1000 to 1200 ° C. in the absence of catalyst. While flue gas deyellowing is considered in spite of the relatively small amount of sulfur in normal biomass, it is not considered for pollution or pollution caused by relatively large amounts of phosphorus or Fuel-N. , May cause second pollution. In particular, in this step, a gas quencher 107 is provided for suppressing dioxin conversion reaction by chlorine ions present in the raw material.

  FIG. 2 is a diagram showing a conventional high-grade waste two-stage catalyst gasifier. Even if it is a waste with a small amount of impurities and a high calorific value, the raw material is non-catalytically flowed at about 700 to 800 ° C. in a fluidized bed gasification furnace 110 as shown in FIG. One-stage partial oxidation and thermal decomposition using a floor is performed. After the temperature of the generated combustible gas is lowered to about 300 ° C., slaked lime is added to fix Cl and S, and these are collected by the cyclone 103. After the dust is removed, the temperature of the combustible gas is further increased by the gas mixer 111 and the combustion furnace 112, and the two-stage tar catalyst reforming reaction is performed by the gas reformer 113. In the case of a NiO / MoO catalyst, it was known that the reaction was carried out at 800 to 1000 ° C. in the case of a catalyst in which Ni, Cr, Fe, etc. were supported on alumina at 400 to 500 ° C. Reference numeral 114 denotes a boiler, 115 denotes a gas storage tank, and the same reference numerals are given to the devices common to FIG.

The present invention has been made to solve the above-mentioned problems, and by using a more refined fuel, poisoning-resistant catalytic gasification is performed even in the first stage gasification process, and the gasification yield is reduced at a low temperature. The purpose of the two-stage catalytic reforming reaction is to gasify tar and convert Tar-N and HCN in combustible gas to NH 3 .

Another object of the present invention is to lower the temperature of the entire process, reduce the energy consumption of the system for maintaining the reaction, and minimize the CO 2 content in the gas, thereby generating unit heat of the generated gas. By increasing the amount and generating generated ash as fly ash that is not in a molten state, it is necessary to make the reactor compact by eliminating the need for a rapid cooling system for molten ash.

  In order to solve the above-mentioned technical problem, the present invention temporarily stores refined fuel, a fuel hopper including a screw feeder at the bottom for quantitatively supplying the refined fuel, and a refined fuel supply of the fuel hopper. A catalyst circulating fluidized bed gasification furnace including a hot air pipe and a steam pipe provided in the lower part, and an upper part of the catalyst circulating fluidized bed gasification furnace. To the catalyst circulating fluidized bed gasification furnace through a pipe extending from the upper side wall to the upper side wall, and a dust collection cyclone for collecting fly ash, and a pipe from the upper part of the dust collection cyclone to the lower part. A catalyst reformer communicating with the dust cyclone and including a fixed bed filter adsorbent layer in the lower layer and a fluidized catalyst layer in the upper layer, and from the upper center of the catalyst reformer to the center of the catalyst reformer A heat exchanger that communicates with a pipe extending through the pipe, a tar scrubber that is located behind the refined fuel supply direction of the heat exchanger and includes a main body, a tar storage tank, and a circulation pump that circulates the tar, and purification of the tar scrubber A low-temperature catalytic gasification device for biomass refined fuel including a gas storage tank located at the rear of the fuel supply direction is provided.

  The present invention also provides a fuel supply stage in which a mixture obtained by refining biomass organic waste / coal / heavy oil is supplied to the central part of a gasifier using a screw feeder, and hot air in the presence of a catalyst. And steam are used to dry, volatilize, low-temperature catalytic gasification, and partial combustion reaction of the fuel, and to collect the fly ash in the gas generated in the catalytic circulation flow gasification stage A dust collection stage, a catalyst reforming stage in which gas is reformed through a lower fixed adsorption layer and tar-nitrogen, aromatic-nitrogen, phosphorus, and sulfur are reformed through an upper fluidized catalyst layer; The condensate is cooled to below ℃, and the condensate is sent to a tar storage tank, and the tar scrubber which condenses and recovers the unconverted tar or uncondensed liquid and gas strips the condensed liquid. And ring step, providing a low-temperature catalytic gasification process of biomass purified fuel comprising a gas storage method comprising: storing temporarily compressing the gas.

  The fuel used in the present invention is such that the gasification reaction is initiated at a relatively lower temperature than a single fuel material, but by using a catalyst to lower it, the oxygen consumption required to maintain the temperature is reduced. It is cheap and can be produced. In addition, the gasifier operating temperature is low, the heat dissipation loss is small, the slagging treatment system is not required, the equipment can be miniaturized, and the conventional gasification product gas using oxygen is used with less air. It is more economical because it can maintain the same amount of heat.

  The present invention is a clean energy production technology that converts a high-grade refined sludge / coal mixture into a low-priced high-calorie gas fuel.

  Gasification of the refined sludge / coal / oil mixture is initiated at a lower temperature than single component gasification, since even a material with a high gasification reaction start temperature can start together at a lower temperature and take less time. , Rapid gasification can be achieved. The device can be downsized due to its low ash content and ease of control such as fly ash at low temperatures, so energy can be saved and operational efficiency can be improved. Because there is very little heavy metal and salt, a post-combustion treatment system is unnecessary.

  For gasification, a fluidized bed system that can be operated at a relatively low temperature is selected, and an inexpensive natural limestone powder or granular material that can be gasified at a low temperature is used. The operating efficiency is 1100 ° C. or higher.

The reforming reaction temperature in the conventional tar reformer is higher than the gasification reaction temperature, and it is usually operated at 1200 ° C or higher. However, in this equipment, the heat source added to the reformer is not required at 650 ° C or lower. Before the reforming catalytic reaction, hydrogen sulfide and phosphorus pentoxide gas, etc., which are catalyst poison components, are removed by reaction fixation with quicklime, and then the reforming of tar and conversion of Fuel-N to NH 3 by the catalyst. Increase.

  In the conventional process, tar is an unnecessary substance, which is recycled or disposed of. In this process, unreacted tar or tar generated by catalytic reforming, and liquid generation generated during cold storage of gas are generated. It has the characteristics of collecting things and using them for other purposes. That is, liquid components such as tar generated in the conventional coal gasification process are not the desired product, so additional equipment or a utilization plan such as adding this to the gasification process or using it as liquid fuel is necessary. It is. However, in this process, since this is used as an agglomerated material for agglomerate formation, there is no problem.

  Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

  FIG. 3 is a block diagram of a catalytic gasifier that can recover an energy source in the form of gas from the biomass refined fuel of the present invention.

  Biomass refined fuel is a combustible material that is obtained by selectively separating only organic solids in biomass and coal together with oil using an oil agglomeration method or flotation method. Is a high-quality solid fuel with a calorific value of 7,000 kcal / kg or more.

  The apparatus of the present invention includes a fuel hopper 10 for storing fuel, a screw feeder 11 for supplying the stored fuel to the next apparatus, and a catalyst circulation fluidized bed gasifier 20 provided behind the fuel hopper 10.

  The fuel inlet supplied from the screw feeder 11 is attached to the center of the catalyst circulating fluidized bed gasifier 20.

  A hot air pipe 21 and a steam pipe 22 are attached to the conical lower portion of the catalyst circulation fluidized bed gasification furnace 20. At this time, the hot air pipe 21 is attached at the same level as the conical lower part, and the steam pipe 22 is attached so that the end protrudes from the lower part to a height of 15 to 30 cm.

  A small cyclone 23 can be further attached to the upper part of the catalyst circulating fluidized bed gasifier 20.

  A dust collection cyclone 30 is attached to the rear of the catalyst circulation fluidized bed gasification furnace 20, and a pipe from the upper part of the catalyst circulation fluidized bed gasification furnace 20 communicates with the upper side wall of the dust collection cyclone 30 so that fly ash in the gas can be obtained. Are collected at the bottom of the dust collection cyclone 30. A catalyst reformer 40 is attached behind the dust collection cyclone 30, and a pipe 31 from the upper part of the dust collection cyclone 30 communicates with the lower part of the catalyst reformer 40.

  The catalyst reformer 40 is provided with a fixed bed filter adsorbent layer 41 on the lower side of the inside thereof, and a fluidized catalyst layer 42 is formed above the fixed bed filter adsorbent layer.

  The fixed bed filter adsorbent layer 41 is in the form of a cartridge, and is a mixture of an asbestos material filter, a granular alkaline earth metal oxide system, and an alkali metal salt granular powder.

  A steam pipe 33 communicates with an intermediate part of the pipe 31 drawn from the upper part of the cyclone 30 via a valve 32, and is connected to a steam sprayer 43 located below the fixed bed filter adsorbent layer 41 of the catalyst reformer 40. You can communicate.

  Heated steam is mixed through the steam pipe 33 so that the condensate is not generated in the gas pipe guided from the cyclone 30 to the catalyst reformer 40, and the residual tar is gasified and reformed again by the catalyst reformer 40. In order to make it happen, it spouts with gas.

  A normal heat exchanger 50 is attached to the rear of the catalyst reformer 40, and a tar scrubber 60 is attached to the rear of the catalyst reformer 40. A tar scrubber main body 61 and a tar storage tank 62 below it are provided. And tar is circulated by the circulation pump 63. Further, the tar storage tank 62 communicates with each lower pipe via a tar valve 64 in order to collect tar generated in the catalyst reformer 40 and the heat exchanger 50.

  A gas storage tank 70 is provided behind the tar scrubber 60, and a fuel gas storage pump 71 is disposed therebetween.

  Hereinafter, a method for producing clean gas using the apparatus of the present invention will be described.

  The refined mixed fuel fed from the fuel hopper 10 through the screw feeder 11 is dried, volatilized and cooled by air or oxygen and water vapor supplied from the catalyst circulation fluidization gasification furnace 20 through the hot air pipe 21 and the steam pipe 22. Catalytic gasification, pyrolysis gasification and partial combustion reaction. At the lower end of the gasification cone, unreacted fuel comes into contact with air or oxygen and undergoes a complete combustion reaction.

  The ratio of air or oxygen charged into the catalyst circulating fluidized bed gasification furnace 20 is about 0.3 to 0.7 with respect to the theoretical amount of complete combustion of the refined mixed fuel, and water vapor is 0.5 by volume with respect to air. -10 times. The fluidizing catalyst agent in the gasification process in the catalyst circulation fluidized bed gasification furnace 20 is granular or powder that can be fluidized, natural limestone, lime magnesite, quick lime, alkaline earth metal such as calcium, magnesium, barium and the like. It includes oxides, alkali metals such as potassium, oxides thereof, and alumina or a mixture thereof. Using such a catalyst, high-speed operation is performed at a maximum temperature of 900 ° C. or less, for example, the gas residence time is set to 2 to 4 seconds.

  Desirably, partial oxidation and low-temperature catalytic pyrolysis are performed simultaneously at 850 ° C or lower, and most gasification processes use oxygen at high temperatures during partial oxidation for supplying system heat sources. However, even if high-grade fuel and air that functions as a fuel oxidant are reacted at a relatively low temperature, gas can be produced with the same heat quantity as when oxygen is used in the conventional process. At this time, air is injected at the lowermost end of the gasifier, and the lowermost portion of the gasifier can be completely burned with unreacted combustible material in an oxygen-excess state.

  By installing a small cyclone 23 on the upper part of the catalyst circulation fluidized bed gasification furnace 20, the scattered catalyst or unreacted raw material and fuel agglomerates such as heavy tar are efficiently collected to the catalyst circulation gasification furnace 20. It can also be recycled to complete the gasification reaction.

  In the dust collection cyclone 30, a small amount of fly ash is efficiently collected and removed.

  The catalyst reformer 40 is composed of two layers. The low-layer fixed bed filter adsorbent layer 41 is a cartridge type, and the upper layer is a fluidized catalyst layer 42.

In the fixed bed filter adsorbent layer 41, the fine fly ash is first removed with an asbestos thread filter, and sulfur and phosphorus poisoning is removed by chemical adsorption with potassium oxide and sodium carbonate adsorbent. Recycle or replace after a certain period of use. As an example, hydrogen sulfide (H 2 S) generated in the gasification process reacts with CaO to be converted to CaS and is adsorbed by reaction. Vapor compounds such as PH 4 -halogen react with Na 2 CO 3 to form NaPO 3 salts, which are selectively chemically adsorbed. The phosphorus component is converted to P α H β S γ Halogen δ (α = 1-7, β = 0-5, γ = 0-7, δ = 0-7) and chemically adsorbed. Similarly, the P x S y compounds generated in the gasification process react with the respective selective chemisorbents or react with the calcium salts and chemisorb.

The fluid catalyst of the fluid catalyst layer 42 serves to decompose tar by gasification and convert aromatic nitrogen, HCN, etc. into an alkane or alkene compound and NH 3 . As the reforming catalyst to be used, it is possible to use a single metal and a metal oxide such as Ni, Fe, Co, Mo, Mn, Zr, Ti, Ce, Ru, Rh, Pt or a mixed form thereof. The working temperature is preferably 650 ° C or lower.

  The gas that has undergone the reforming reaction is heat-exchanged by the heat exchanger 50 to cool the gas to 200 ° C. or lower, and the condensate is sent to the tar storage tank 62. The heat exchange cooling medium is converted into hot air and water vapor using air or oxygen and water used in the gasification process. In this case, the heat exchanger 50 can improve energy utilization efficiency by using a metal heat exchanger made of a high temperature material.

  Tar or uncondensed liquid that has not been converted by the catalyst reformer 40 is condensed by the tar scrubber 60 and collected in the tar storage tank 62. At this time, in order to increase the recovery efficiency of dust and tar, the condensed liquid of 150 ° C. or less is sent again to the upper part of the tar scrubber 60 by the tar circulation pump 63 to perform gas stripping.

  Thereafter, the generated clean gas fuel is compressed and temporarily stored in the gas storage tank 70.

  Hereinafter, examples will be described in detail.

Example 1: Effect of improving gas generation efficiency by catalytic gasification In order to gasify SOCA (Sludge-Oil-Coal Agglomerates) under a Fe 2 O 3 / CaO mixed catalyst, the mixed catalyst and SOCA are converted into non-catalytic gas. Under similar operating conditions, a gas product was obtained by mixing uniformly at 3.4: 1. The state of the product is as shown in FIG. When using a mixed catalyst, the gasification reaction starts at 230 ° C, starting at an extremely low temperature compared to 560 ° C when no catalyst is used, and there is less CO conversion and more hydrocarbons than when no catalyst is used. , Mostly methane was confirmed. In non-catalytic gasification, hydrocarbons were generated at 850 ° C or higher and CO was generated at 1050 ° C or higher. However, when a mixed catalyst was used, CO and hydrocarbons were vigorously generated at around 500 ° C. CO is maximum generated again at about 850 ° C., and the gasification reaction is completed within a short time. The amount of unreacted char generated after the gasification reaction using the mixed catalyst was very low at about 0.35%, but the residual char after maintaining at 1050 ° C. for 2 hours under the condition of no catalyst. Compared to the generated amount of about 11.31%, an excellent result was shown.

Example 2: Effect of reducing tar generation and Fuel-N pollutant generation by two-stage catalytic gasification Using CaO catalyst which is an oxide of alkaline earth metal in the first stage gasification, As a result of using the NiO catalyst, as shown in FIG. 5, compared with the case where only the first stage catalyst CaO is used, the generation of CO is similar, but the generation of hydrocarbons is slightly increased and the reaction is completed in a short time. did. However, as shown in Table 1, after using calcium oxide as the first stage catalyst and using NiO and MnO 2 as the second stage catalyst, the generation of tar and NH are compared with the case where only the primary catalyst is used. Although generation 3 and HCN were significantly less, which is mostly tar is reacted reforming and Fuel-N is determined to be because he is immediately converted into N 2. On the other hand, the MnO 2 catalyst has an inferior tar reforming reaction compared to the NiO catalyst, and only the Fuel-N is converted to HCN and not ammonia. Therefore, the NiO catalyst is not converted to ammonia. It shows that it is more excellent in reforming.

It is the schematic of the non-catalyst high temperature two-stage gasification apparatus of biomass. It is a schematic process diagram of a two-stage catalyst gasifier for high-grade waste. It is a figure of the two-stage catalyst gasification apparatus of the biomass refinement | purification fuel of this invention. It is a comparison figure of the non-catalyst and catalyst gasification characteristic of sewage sludge refined fuel. It is a comparison figure of the two-stage catalyst gasification characteristic of sewage sludge refined fuel.

Claims (11)

  1. A fuel hopper (10) having a screw feeder (11) in a lower part for temporarily containing the refined fuel and quantitatively supplying the refined fuel;
    Catalyst circulation which is arranged in the vicinity of the fuel hopper (10) and has a charging port communicating with the screw feeder (11) in the central part and a hot air pipe (21) and a steam pipe (22) in the lower part. A fluidized bed gasifier (20);
    A dust collecting cyclone (30) communicating with the upper part of the catalyst circulating fluidized bed gasifier (20) via a pipe and collecting fly ash from the upper wall;
    A catalyst reformer (40) communicating with the upper part of the dust collection cyclone (30) through a pipe, having a fixed bed filter adsorbent layer (41) in a lower layer and a fluidized catalyst layer (42) in an upper layer;
    A heat exchanger (50) in communication with the catalytic reformer (40) via a pipe and an upper portion of the catalytic reformer (40);
    A tar scrubber (60) disposed in the vicinity of the heat exchanger (50) and including a main body (61) communicating with the heat exchanger (50), a tar storage tank (62), and a circulation pump (63) for circulating tar. )When,
    A gas storage tank (70) disposed in the vicinity of the tar scrubber (60);
    A low-temperature catalytic gasification apparatus for biomass refined fuel, comprising:
  2.   The low-temperature catalytic gasification apparatus for biomass refined fuel according to claim 1, wherein the catalyst circulation fluidized bed gasification furnace (20) further includes a small cyclone (23) in an upper part thereof.
  3.   The low temperature catalytic gasification of biomass refined fuel according to claim 1, wherein the catalyst reformer (40) further comprises a steam sprayer (43) below the fixed bed filter adsorbent layer (41). apparatus.
  4.   The biomass-refined fuel according to claim 1, wherein the fixed bed filter adsorbent layer (41) has a cartridge form and includes an asbestos material filter, granular alkaline earth metal oxide, and alkali metal salt. Low temperature catalytic gasifier.
  5.   The tar storage tank (62) communicates with the lower pipes of the catalyst reformer (40) and the heat exchanger (50) via a tar valve (64) in order to collect the generated tar. The low-temperature catalytic gasification apparatus for biomass refined fuel according to claim 1, wherein
  6. A fuel supply stage for supplying a mixture obtained by refining biomass organic waste / coal / heavy oil to the center of the gasifier using a screw feeder;
    A catalyst circulation fluidization gasification stage in which the fuel is dried, volatilized, low temperature catalyst gasification, and partial combustion reaction using hot air and steam in the presence of a catalyst;
    A dust collection stage for collecting fly ash in the gas generated in the catalyst circulation flow gasification stage;
    A catalytic reforming stage in which gas is reformed through a lower fixed adsorbent layer and tar-nitrogen, aromatic-nitrogen, phosphorus, and sulfur are reformed through an upper fluidized catalyst layer;
    A heat exchange stage in which the gas is cooled to below 200 ° C. and the condensate is sent to a tar storage tank;
    A tar scrubbing stage that condenses and recovers unconverted tar or uncondensed liquid and gas strips the condensed liquid;
    A gas storage stage for compressing and temporarily storing the gas;
    A low-temperature catalytic gasification method for biomass refined fuel, comprising:
  7.   The catalyst used in the catalyst circulation fluidization gasification step is composed of fluidized granular or powdered natural limestone, lime magnesite, quicklime, alkaline earth metal such as calcium, magnesium, barium and oxides thereof. The method for low-temperature catalytic gasification of biomass refined fuel according to claim 6, wherein the method is selected from the group consisting of alkali metals such as potassium and oxides thereof, alumina, and mixtures thereof.
  8.   The catalyst circulation fluidization gasification step further comprises the step of recirculating the scattered catalyst or fuel agglomerate through a small cyclone (23) to the catalyst circulation fluidized bed gasification furnace (20). Low temperature catalytic gasification method for biomass refined fuel.
  9.   The catalyst reforming step includes a step of spraying water vapor below the fixed bed adsorption layer (41) to reduce the reforming temperature to 650 ° C. or less in order to accelerate the reforming reaction and prevent clogging of the piping. The method for low-temperature catalytic gasification of a purified biomass fuel according to claim 6, further comprising:
  10. In the catalyst reforming step, hydrogen sulfide is CaS and phosphorus is P α H β S γ Halogen δ (α = 1-7, β so that it is chemically adsorbed on the fixed bed adsorbent layer (41). = 0-5, γ = 0-7, δ = 0-7).
  11. The fluid catalyst of the fluid catalyst layer (42) used in the catalyst reforming step decomposes tar by gasification and converts aromatic-nitrogen or HCN into an alkane compound, an alkene compound and NH 3. It is characterized by being a single metal such as Ni, Fe, Co, Mo, Mn, Zr, Ti, Ce, Ru, Rh or Pt and an oxide thereof, or a mixture thereof. A method for low-temperature catalytic gasification of a purified biomass fuel according to claim 6.
JP2006535283A 2004-08-05 2005-06-14 Low-temperature catalytic gasification apparatus and method for biomass refined fuel Active JP4243295B2 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
KR1020040061657A KR100569120B1 (en) 2004-08-05 2004-08-05 Apparatus of catalytic gasification for refined biomass fuel at low temperature and the method thereof
PCT/KR2005/001808 WO2006031011A1 (en) 2004-08-05 2005-06-14 Apparatus of catalytic gasification for refined biomass fuel at low temperature and the method thereof

Publications (2)

Publication Number Publication Date
JP2007506856A JP2007506856A (en) 2007-03-22
JP4243295B2 true JP4243295B2 (en) 2009-03-25

Family

ID=36060239

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2006535283A Active JP4243295B2 (en) 2004-08-05 2005-06-14 Low-temperature catalytic gasification apparatus and method for biomass refined fuel

Country Status (5)

Country Link
US (1) US20070094929A1 (en)
EP (1) EP1773968A4 (en)
JP (1) JP4243295B2 (en)
KR (1) KR100569120B1 (en)
WO (1) WO2006031011A1 (en)

Families Citing this family (65)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL1030864C2 (en) * 2006-01-06 2007-07-09 Stichting Energie Method and device for treating biomass.
FI118647B (en) 2006-04-10 2008-01-31 Valtion Teknillinen Procedure for reforming gas containing tar-like pollutants
DE102006017353A1 (en) * 2006-04-11 2007-10-18 Spot Spirit Of Technology Ag Method and apparatus for process-integrated hot gas cleaning of dust and gaseous ingredients of a synthesis gas
JP2007283209A (en) * 2006-04-17 2007-11-01 Takuma Co Ltd Gasification catalyst, its manufacturing method and gasification system
FR2904405B1 (en) * 2006-07-31 2008-10-31 Inst Francais Du Petrole Process for preparing a biomass-containing load for subsequent gasification
JP5032101B2 (en) * 2006-11-29 2012-09-26 国立大学法人 筑波大学 Tar gasification catalyst for reforming and gasifying pyrolytic tar of carbonaceous raw material, tar gasification method, method for using tar gasification gas, and method for regenerating tar gasification catalyst
KR100784851B1 (en) * 2007-01-12 2007-12-14 한국에너지기술연구원 Biomass gasifier producing low tar
WO2008102414A1 (en) * 2007-02-22 2008-08-28 Ihi Corporation Fuel gasification equipment
WO2008135226A2 (en) * 2007-05-02 2008-11-13 Pall Corporation Gasification apparatus and method for generating syngas from gasifiable feedstock material
US7942943B2 (en) * 2007-06-15 2011-05-17 Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College Biomass gasifier system with low energy and maintenance requirements
US20090031698A1 (en) * 2007-07-31 2009-02-05 O'brien & Gere Engineers Inc. Liquid and Solid Biofueled Combined Heat and Renewable Power Plants
EP2034003A1 (en) * 2007-09-07 2009-03-11 ReSeTec Patents Geneva S.A. i.o. Process and apparatus for producing synthesis gas from waste
US8084656B2 (en) 2007-10-09 2011-12-27 Rentech, Inc. Systems and methods for oxidation of synthesis gas tar
KR100986241B1 (en) * 2007-10-23 2010-10-07 서울시립대학교 산학협력단 Catalytic for steam reforming of tar produced from biomass gasification process and method of steam reforming of tar using the same
CA2713656C (en) 2007-12-28 2014-07-08 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
KR100912249B1 (en) 2008-03-25 2009-08-14 한국에너지기술연구원 Catalytic reactor for reforming tar and removing soot
JP4966239B2 (en) * 2008-03-28 2012-07-04 メタウォーター株式会社 Organic waste treatment method, gasification furnace, reforming furnace, organic waste treatment equipment
WO2009124017A2 (en) 2008-04-01 2009-10-08 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
DE102008021084A1 (en) * 2008-04-28 2009-10-29 Süd-Chemie AG Use of a noble metal based catalyst for reducing tar content in gases from gasification processes
DE102008021081A1 (en) * 2008-04-28 2009-10-29 Süd-Chemie AG A process for the catalytic reduction of tar content in gases from gasification processes using a noble metal based catalyst
FI126542B (en) * 2008-06-13 2017-02-15 Valmet Technologies Oy Method and plant for handling lime slurry and bed material
US8460410B2 (en) * 2008-08-15 2013-06-11 Phillips 66 Company Two stage entrained gasification system and process
US8499471B2 (en) * 2008-08-20 2013-08-06 The Board Of Regents Of The Nevada System Of Higher Education, On Behalf Of The University Of Nevada, Reno System and method for energy production from sludge
JP5521187B2 (en) * 2008-09-25 2014-06-11 株式会社神鋼環境ソリューション Combustible gas generator for gasifying waste and method for producing combustible gas
US8669404B2 (en) 2008-10-15 2014-03-11 Renewable Fuel Technologies, Inc. Method for conversion of biomass to biofuel
JP5572855B2 (en) * 2009-03-24 2014-08-20 昭和シェル石油株式会社 Biomass gasification reforming catalyst and method for producing synthesis gas using the same
US8668753B2 (en) * 2009-04-24 2014-03-11 G.D.O. Inc Two stage process for converting biomass to syngas
US8404910B2 (en) * 2010-02-17 2013-03-26 Uop Llc Low oxygen biomass-derived pyrolysis oils and methods for producing the same
WO2011112526A2 (en) * 2010-03-08 2011-09-15 Shulenberger Arthur M Device and method for conversion of biomass to biofuel
US9296962B2 (en) 2010-09-01 2016-03-29 Starlight Energy Holdings LLC System and process for gasifying biomass products
CA2815243A1 (en) 2010-11-01 2012-05-10 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US20120137700A1 (en) * 2010-12-07 2012-06-07 Dennis John Werner System for Producing Power Using Low Pressure Gasification of a Stock Fuel
JP5857340B2 (en) * 2011-03-15 2016-02-10 九州電力株式会社 Combined system using coal for char / raw gas production and power generation
CN103597056A (en) 2011-04-21 2014-02-19 国际壳牌研究有限公司 Process for converting a solid biomass material
EP2699643A1 (en) 2011-04-21 2014-02-26 Shell Internationale Research Maatschappij B.V. Improvements to separation of product streams
WO2012143568A2 (en) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Liquid fuel composition
CA2833201A1 (en) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Process for converting a solid biomass material
US9062597B2 (en) 2011-05-10 2015-06-23 Innerpoint Energy Corporation Centrifugal particle separator and method of operating the same
CN102226111A (en) * 2011-05-27 2011-10-26 吴道洪 Method for gasifying cyclone bed powder coal
CN103582693A (en) 2011-06-03 2014-02-12 格雷特波因特能源公司 Hydromethanation of a carbonaceous feedstock
WO2012169711A1 (en) * 2011-06-09 2012-12-13 한국에너지기술연구원 Low-grade-coal coal gas production system
KR101065184B1 (en) 2011-06-09 2011-09-19 한국에너지기술연구원 A production system of coal gas from low-rank coal
US9920929B2 (en) 2011-06-13 2018-03-20 Ecolab Usa Inc. Method for reducing slag in biomass combustion
US9127219B2 (en) 2011-07-19 2015-09-08 General Electric Company Additive systems for biomass gasification
JP5971836B2 (en) * 2011-07-21 2016-08-17 株式会社タクマ Method for producing gasification catalyst and gasification treatment system
WO2013052553A1 (en) 2011-10-06 2013-04-11 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
WO2013108920A1 (en) 2012-01-20 2013-07-25 新日鐵住金株式会社 Continuous fixed-bed catalyst reaction device and catalyst reaction method using same
TWI447598B (en) * 2012-06-13 2014-08-01 China Steel Corp Method for drying biomass and computer product thereof
JP5974363B2 (en) * 2012-06-15 2016-08-23 株式会社Ihi Gasification gas generator and tar reformer
KR101646890B1 (en) 2012-10-01 2016-08-12 그레이트포인트 에너지, 인크. Agglomerated particulate low-rank coal feedstock and uses thereof
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
KR101576781B1 (en) 2012-10-01 2015-12-10 그레이트포인트 에너지, 인크. Agglomerated particulate low-rank coal feedstock and uses thereof
WO2014055365A1 (en) 2012-10-01 2014-04-10 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
KR101890950B1 (en) * 2012-12-07 2018-08-22 에스케이이노베이션 주식회사 Method for Gasification Using Spent Catalyst Discharged from Refinery Process
US20150368393A1 (en) * 2013-02-14 2015-12-24 Veolia Water Solutions & Technologies Support Process for the extraction of polyhydroxyalkanoates from biomass
JP2014205806A (en) * 2013-04-15 2014-10-30 株式会社Ihi Gasified gas generation system
WO2014182295A1 (en) * 2013-05-08 2014-11-13 Innerpoint Energy Corporation A centrifugal particle separator and method of operating the same
CN103343021B (en) * 2013-07-17 2015-06-24 王建伟 Device and method for waste heat recovery and purification of biomass gasified gas
KR101623476B1 (en) * 2013-10-16 2016-06-07 한국기계연구원 NOx REMOVAL DEVICE FOR SEMICONDUCTOR MANUFACTURING PROCESS
KR101537058B1 (en) * 2014-04-04 2015-07-16 주식회사 온이엔지 Apparatus for gasification of refuse derived fuel and method for gasification of refuse derived fuel using the same
US9545590B2 (en) 2015-01-16 2017-01-17 Innerpoint Energy Corporation Rotating centrifugal particle separator and gasifier having the same
KR101863359B1 (en) * 2015-07-01 2018-06-01 한국에너지기술연구원 An apparatus of continuous catalytic reaction of bio-oil
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3115394A (en) * 1961-05-29 1963-12-24 Consolidation Coal Co Process for the production of hydrogen
US3929431A (en) * 1972-09-08 1975-12-30 Exxon Research Engineering Co Catalytic reforming process
US5213587A (en) * 1987-10-02 1993-05-25 Studsvik Ab Refining of raw gas
DK583587D0 (en) * 1987-11-06 1987-11-06 Dansk Termo Ind Method and apparatus for the production of gas from a comminuted biological material
US4865625A (en) * 1988-05-02 1989-09-12 Battelle Memorial Institute Method of producing pyrolysis gases from carbon-containing materials
JPH11502891A (en) * 1995-03-31 1999-03-09 ユニバーシティ オブ ハワイ Gasification in a supercritical state of the wet biomass using a catalyst
NZ514823A (en) * 2000-02-29 2003-06-30 Mitsubishi Heavy Ind Ltd Biomass gasification furnace and methanol synthesis system making use of gas produced through biomass gasification
EP1142981A3 (en) * 2000-03-23 2003-04-02 Fraunhofer-Gesellschaft Zur Förderung Der Angewandten Forschung E.V. Apparatus for power generation by gasification of biomass with subsequent catalytic removal of tar compounds from the heating gas
US6797253B2 (en) * 2001-11-26 2004-09-28 General Electric Co. Conversion of static sour natural gas to fuels and chemicals
JP3975271B2 (en) * 2001-12-18 2007-09-12 国立大学法人東北大学 Biomass gasification method and catalyst used therefor
JP2003342588A (en) * 2002-05-27 2003-12-03 Setec:Kk Biomass gasification equipment
JP2004149556A (en) * 2002-10-28 2004-05-27 Isao Mochida Method for gasifying biomass and gasifying apparatus therefor

Also Published As

Publication number Publication date
KR20060012934A (en) 2006-02-09
JP2007506856A (en) 2007-03-22
KR100569120B1 (en) 2006-04-10
US20070094929A1 (en) 2007-05-03
EP1773968A4 (en) 2012-03-28
EP1773968A1 (en) 2007-04-18
WO2006031011A1 (en) 2006-03-23

Similar Documents

Publication Publication Date Title
EP0803562B1 (en) Method and apparatus for treating wastes by gasification
EP1193444B1 (en) Method for simultaneously reducing co2 and so2 emissions in a combustion plant
CN101312905B (en) Process and system for gasification with in-situ tar removal
US7767191B2 (en) Combustion looping using composite oxygen carriers
RU2290428C2 (en) Method of coal conversion for obtaining quality hydrogen for fuel mixtures and carbon dioxide ready for utilization and device for realization of this method
CA2458404C (en) Facility and process for the multi-stage gasification of a load comprising organic matter
ES2343167T3 (en) Gasificator of multiple facets and related procedures.
CN1276787C (en) Apparatus and method for cleaning acidic gas
US7452392B2 (en) Process for pyrolytic heat recovery enhanced with gasification of organic material
CN102585910B (en) Hot solids gasifier with CO2 removal and hydrogen production
JP2011526325A (en) Two-line catalytic gasification system
JP4259777B2 (en) Biomass gasification method
EP0676464A2 (en) Method of and apparatus for fluidized-bed gasification and melt combustion
DE60024288T2 (en) A steam reformer and a fuel cell containing integrated system
JP2004534903A (en) How to create clean energy from coal
RU2272782C2 (en) Production of hydrogen out of carbon-containing material
CN101555420B (en) Method, system and equipment for catalytic coal gasification
CA2636325C (en) Systems and methods of converting fuel
Göransson et al. Review of syngas production via biomass DFBGs
US5243922A (en) Advanced staged combustion system for power generation from coal
US8038746B2 (en) Reduced-emission gasification and oxidation of hydrocarbon materials for liquid fuel production
US5290327A (en) Device and allothermic process for producing a burnable gas from refuse or from refuse together with coal
CN101213273B (en) Method of solid fuel gasification including gas purification and gasifier employing the method
US20040244289A1 (en) Process for reforming inflammable gas, apparatus for reforming inflammable gas and gasification apparatus
US4597771A (en) Fluidized bed reactor system for integrated gasification

Legal Events

Date Code Title Description
TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20081202

A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20081226

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20120109

Year of fee payment: 3

R150 Certificate of patent or registration of utility model

Free format text: JAPANESE INTERMEDIATE CODE: R150

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20130109

Year of fee payment: 4

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20130109

Year of fee payment: 4

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250