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WO2014069840A1 - Double réacteur de gazéification de la biomasse comportant une plaque de distribution en nickel et gazéificateur de biomasse l'utilisant - Google Patents

Double réacteur de gazéification de la biomasse comportant une plaque de distribution en nickel et gazéificateur de biomasse l'utilisant Download PDF

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Publication number
WO2014069840A1
WO2014069840A1 PCT/KR2013/009559 KR2013009559W WO2014069840A1 WO 2014069840 A1 WO2014069840 A1 WO 2014069840A1 KR 2013009559 W KR2013009559 W KR 2013009559W WO 2014069840 A1 WO2014069840 A1 WO 2014069840A1
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Prior art keywords
reactor
biomass
distribution plate
dual
tar
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English (en)
Korean (ko)
Inventor
김주식
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Industry Cooperation Foundation of University of Seoul
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Industry Cooperation Foundation of University of Seoul
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    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • 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
    • B01J7/00—Apparatus for generating gases
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • C10K1/30—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses with moving purifying masses
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/0923—Sludge, e.g. from water treatment plant
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • 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
    • C10J2300/1253—Heating the gasifier by injecting hot gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/028—Dust removal by electrostatic precipitation
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the present invention relates to a dual biomass gasification reactor having a nickel distribution plate and a biomass gasification apparatus having the same. More specifically, the present invention relates to a dual biomass gasification reactor having a nickel distribution plate which can minimize tar and ammonia generation and has excellent durability, and a biomass gasification apparatus having the same.
  • Fluidized bed gasifiers have been used in energy conversion and energy recovery processes associated with gasification of coal, sludge or waste polymers, waste wood and waste tires in many chemical processes such as alternative energy development and biomass treatment. There is extensive research on this. Fluidized bed gasifiers have better heat transfer characteristics than fixed bed gasifiers such as up-draft and down-draft gasifiers, and because of the uniform temperature distribution in the reactor, The yield and composition of the producer gas) is constant, and the residence time of the solid reactant in the reactor is long, and the solid has a fluid-like flow, and thus the solid treatment is easy.
  • the fluidized bed gasifier has been researched and developed in various ways, such as having an internal circulation structure or using a catalyst for high calorific value and yield increase of calorific gas.
  • a gasifier using an inner circulating fluidized bed is known from South African Patent No. 857,717.
  • the internal circulation fluidized bed gasifier known in this patent is configured to allow internal circulation in the fluidized bed by inserting a draft tube into the fluidized bed to divide the fluidized bed into two parts and injecting fluidized gas velocities at different rates.
  • Korean Patent Registration No. 208654 discloses an internal circulation fluidized bed gasification reactor having a bottom perforated draft tube
  • Korean Patent Registration No. 340594 discloses a gasification method of coal using an internal circulation fluidized bed reactor.
  • FIG. 1 is a conceptual diagram showing the configuration of a general fluidized bed gasifier disclosed in the above known art.
  • oxidation, partial oxidation, pyrolysis, and drying occur almost simultaneously during gasification.
  • Table 1 showing the gas characteristics and the tar content according to the type of gasification reactor, it has a smaller tar content in the generated gas than the ascending type gasifier.
  • this tar content is still high for power generation and the like, when tar is produced using gas turbines and gas engines using the generated gas obtained from the conventional fluidized bed gasifier, the gas turbine and gas due to tar are used. There is a problem that process failures such as plugging and fouling problems of the engine are likely to occur.
  • Table 1 Type of gasifier Gas component (VOL.% Dry) High calorific value (MJ / m3) Gas properties H 2 CO CO 2 CH 4 N 2 tar dust Rising Airflow Type (Air Supply) 11 24 9 3 53 5.5 High ( ⁇ 50 g / m3) that Downdraft type (air supply) 17 21 13 One 48 5.7 Low ( ⁇ 1g / m3) medium Fluid type (air supply) 9 14 20 7 50 5.4 Medium ( ⁇ 10 g / m3) Go
  • one object of the present invention is to provide a dual biomass gasification reactor in which tar and ammonia generation can be minimized in order to solve the problems of the prior art.
  • Another object of the present invention is to provide a gasification apparatus for producing a high calorific value gas having a low tar and ammonia content by using the dual biomass gasification reactor stably used for power generation.
  • a distribution plate provided at a communication site between the first and second reactors, the distribution plate prevents flow of the biochar and the sand or tar decomposition catalyst toward the second reactor in the first reactor, and the carbon in the second reactor.
  • the distribution plate provides a dual biomass gasification reactor, characterized in that the nickel plate.
  • the second reactor is fixed to the inner top of the first reactor so as to be located in the upper side in the interior of the first reactor, with a gap from the inner circumference of the first reactor It may be fixed spaced apart.
  • the second reactor may be installed on the top of the first reactor to form a two-stage configuration.
  • the distribution plate is preferably a nickel plate plated on an iron-based metal plate.
  • the distribution plate may have a shape of a porous plate having a plurality of holes.
  • a hook-shaped pipe may protrude toward the second reactor 220a at the upper end of each hole of the distribution plate.
  • the distribution plate may be attached to the hook (hook) bent a plurality of top.
  • the carbon adsorbent may be activated carbon or biochar.
  • the first reactor comprises: a first pipe installed in communication with the interior of the first reactor for discharging excess biochar to the outside such that the biochar inside maintains a constant amount;
  • the storage unit may further include an accommodation unit configured to store the surplus biochar discharged by gravity along the first pipe.
  • the second reactor may be further provided with a cyclone to discharge the generated gas of reduced tar content in a subsequent process and prevent the outflow of the carbon adsorbent charged therein.
  • a second pipe for communicating the first and second reactors with each other to flow surplus carbon adsorbent toward the first reactor so that the carbon adsorbent in the second reactor maintains a certain amount. It can be provided.
  • Dual biomass gasification reactor for gasifying the biomass injected through the biomass injection means using an external heat source and the heat source of the biomass itself;
  • Heat source supply means for supplying preheated air to the gasification reactor
  • It provides a biomass gasification apparatus comprising a purifying means for purifying the exhaust gas discharged from the gasification reactor.
  • FIG. 1 is a conceptual diagram of a general fluidized bed gasifier.
  • FIG. 2 is a conceptual diagram of a gasifier having a dual biomass gasification reactor according to a first embodiment of the present invention.
  • FIG. 3 is a detailed view of the dual biomass gasification reactor shown in FIG. 2.
  • FIG. 4 is a conceptual diagram of a gasifier having a dual biomass gasification reactor according to a second embodiment of the present invention.
  • FIG. 5 is a conceptual diagram of a gasifier applied to the experimental example of the present invention.
  • FIG. 2 is a conceptual diagram of a gasification apparatus having a dual biomass gasification reactor according to a first embodiment of the present invention
  • FIG. 3 is a detailed view of the dual biomass gasification reactor shown in FIG.
  • the gasification apparatus of the present embodiment includes a biomass injection means 10 for injecting biomass such as sewage sludge and waste wood, and a biomass injected through the biomass injection means 10.
  • a dual biomass gasification reactor 20 to gasify using a heat source and a heat source of the biomass itself, and to reduce the content of tar and ammonia by adsorption or cracking of tar and ammonia in the generated product gas, and a gasification reactor
  • a heat source supply means 30 for supplying preheated air as an oxidant to the 20 and also supplying steam as needed, and refining means for purifying the exhaust gas discharged from the gasification reactor 20 to be used for power production or the like. It consists of
  • the biomass injection means 10 is a pulverized biomass such as sewage sludge or waste wood to be injected into a predetermined size and is composed of a general configuration relationship used in the gasifier.
  • the gasification reactor 20 includes a first reactor 210 having a volume of a predetermined size, and a second reactor 220 installed inside the first reactor 210.
  • the first reactor 210 serves to generate a gas by gasifying the biomass using the preliminary heat source, air and water vapor supplied from the heat source supply means 30, and the heat content of the biomass itself.
  • the first reactor 210 is filled with a predetermined amount of sand or tar decomposition catalyst therein, and is configured to receive the preheated air and steam from the heat source supply means 30 to one side.
  • the sand or tar decomposition catalyst serves to facilitate the gasification of the biomass while flowing along the air stream of the air and water vapor supplied from the heat source supply means (30). That is, the first reactor 210 undergoes typical biomass gasification as a fluidized bed reactor and produces bio-char as a gasification byproduct during the process.
  • the first reactor 210 is configured such that the surplus biochar flows along the first pipe 211 and is stored in the accommodating part 212 so that the biochar generated during the process maintains a constant amount at all times so as not to burden the process. That is, one end of the first pipe 211 is configured to communicate with the inside at a predetermined height of the first reactor 210. At this time, the first pipe 211 has a bent shape so as not to be disturbed by upflow. Therefore, the surplus biochar is stored in the accommodating portion 212 by gravity along the first pipe 211 and not the mechanical device, so that it does not burden the process.
  • the second reactor 220 is fixed to the inner top of the first reactor 210 to be installed on the upper side of the inside of the first reactor 210. Therefore, the second reactor 220 uses the heat source of the first reactor 210 as it is.
  • the second reactor 220 is installed at a predetermined distance from the inner circumference of the first reactor 210, except for the lower portion has a structure that is closed with the first reactor 210. That is, the second reactor 220 has a distribution plate 221 communicating with the first reactor 210 at the bottom thereof.
  • the distribution plate 221 flows smoothly through the product gas generated in the first reactor 210 flows in the upward air flow, but a plurality of micrometer-sized holes, for example, a plurality of holes so that biochar does not pass through. It has the shape of a perforated plate having a hole of. In addition, the hole of the distribution plate 221 has a size that the carbon adsorbent filled in the second reactor 220 does not flow out to the lower first reactor 210.
  • This distribution plate 221 is a nickel plate having a plurality of holes. In terms of economy, the distribution plate 221 is a nickel plate plated on an iron metal plate. For example, the distribution plate 221 is a nickel plate plated on a stainless steel plate.
  • the nickel distribution plate partitioning the first reactor and the second reactor can simultaneously undergo tar reduction and ammonia decomposition. That is, the nickel distribution plate decomposes the tar generated in the first reactor 210 by reducing the tar content in the product gas by decomposing the tar generated in the first reactor 210 and the ammonia generated in the first reactor 210 according to the reaction scheme shown below. Thereby exhibiting an ammonia decomposition catalytic action that reduces the ammonia content in the product gas, thereby reducing the content of tar and ammonia in the gas obtained from the biomass.
  • Reaction ii) is a reverse reaction of ammonia synthesis from hydrogen gas and nitrogen gas.
  • Nickel distribution plates are important in the gasification of sewage sludge containing a lot of nitrogen, especially since they can dramatically reduce the content of ammonia.
  • the use of the nickel distribution plate disclosed in the present invention can reduce nickel loss and nickel deactivation phenomena as compared to a configuration using a nickel catalyst particle layer inside a fluidized bed reactor or a configuration using a separate fixed bed nickel catalyst tower outside the reactor.
  • the nickel distribution plate 221 can prevent the loss of the nickel catalyst accompanying the swept away by the fluid (fluid medium) flow in the fluidized bed when adopting a configuration using a nickel catalyst particle layer in the fluidized bed reactor.
  • a second fixed bed nickel catalyst tower may be additionally installed to solve the energy problem of operating.
  • the nickel distribution plate according to the present invention is because the energy required for tar decomposition by nickel can utilize the energy generated by oxidation in the fluidized bed reactor.
  • the nickel distribution plate according to the present invention has the advantage that the deactivation (deactivation) of the nickel generated by the coke is deposited on the nickel distribution plate is reduced.
  • the nickel catalyst is rapidly deactivated by sulfur, tar, etc., and when the biomass such as wood with low sulfur content and polyolefin waste plastics are gasified, the main deactivation route is generation of coke due to tar deposition.
  • deactivation may be drastically reduced since continuous collision with the nickel distribution plate occurs due to active movement of fluidized bed materials such as sand and / or tar decomposition catalysts, and the coke is separated. It is also possible to continuously oxidize the carbon deposits formed in the nickel distribution plate by air which is often supplied to the first reactor, so that coke deposition can be further reduced. In addition, CO 2 and H 2 O generated from the first gasification reactor may react with coke (C) deposited on the nickel distribution plate to cause coke decomposition.
  • C coke
  • the second reactor 220 serves to reduce the content of tar by adsorbing or cracking tar in the generated gas generated in the first reactor 210, and a predetermined amount of carbon adsorbent (activated carbon) is contained therein. And / or biochar).
  • the carbon adsorbent serves to catalyze the tar in the product gas to reduce the content of tar or promote the decomposition of tar, thereby reducing the content and promoting the reaction with moisture in the product gas, thereby helping to produce hydrogen. do.
  • a cyclone 222 is installed inside the second reactor 220 to prevent the outflow of the carbon adsorbent charged therein and to supply the product gas having a reduced tar content to the purifying means 40.
  • the cyclone 222 preferably has a structure in which its lower end is bent so as not to be disturbed by upflow.
  • the excess carbon adsorbent flows along the second pipe 223 toward the first reactor 210 so as not to impede the process by maintaining a constant amount of the carbon adsorbent charged therein at all times. It is configured to be stored in the receiving portion (212).
  • one end of the second pipe 211 is in communication with the inside at a certain height of the second reactor 220, the other end is configured to communicate with the inside at a certain height of the first reactor (210).
  • the second pipe 223 has a bent shape so as not to be disturbed by upflow.
  • the dual biomass gasification reactor 20 having the above configuration has a predetermined amount of carbon adsorbent inside the second reactor 220 to adsorb tar in the product gas to reduce the content of tar or promote tar decomposition. It acts as a catalyst to reduce the content and promotes the reaction with moisture in the generated gas to help the production of hydrogen to produce a high calorific value gas.
  • the dual biomass gasification reactor 20 can reduce the amount of particles contained in the product gas through the following components. That is, the surplus biochar in the first reactor 210 is discharged to the receiving portion 212 through the first first pipe 211, and the first reactor (through the distribution plate 221 of the second reactor 220). The biochar in the product gas generated in 210 to be flowed into the second reactor 220 along the rising air flow is filtered, and the third cyclone 222 prevents the outflow of the carbon adsorbent inside the second reactor 220. For example, the amount of particles included in the generated gas may be reduced by discharging the excess carbon adsorbent in the second reactor 210 through the second pipe 223 to the accommodation portion 212 through the first reactor 210.
  • the heat source supply means 30 serves to supply a preliminary heat source and air to the first reactor 210 and also to supply water vapor as necessary, and is configured in a general configuration relationship used in a fluidized bed gasifier.
  • the purifying means 40 serves to purify the exhaust gas discharged from the second reactor 220 to be used for electric power production, etc., and is configured in a general configuration relationship used in the fluidized bed gasifier.
  • the gasifier according to the second embodiment of the present invention has the same concept as the gasifier of the first embodiment except for the partial structure of the reactor. Therefore, the same or similar components as those in the first embodiment will be denoted by the same reference numerals and the description thereof will be omitted.
  • the dual biomass gasification reactor 20a includes a biomass injected through the biomass injection means 10a and an external heat source supplied from the heat source supply means 30a and the biomass itself. It comprises a first reactor (210a) for gasification using a heat source, and a second reactor (220a) to reduce the content of tar by adsorption or decomposition of the tar in the product gas generated in the first reactor (210a).
  • the second reactor 220a has a wider size and volume than the first reactor 210a and is installed directly above the first reactor 210a. Therefore, the first and second reactors 210a and 220a form two stages up and down, and the connection portion has a tapered shape.
  • the first reactor 210a is filled with a certain amount of sand therein, and the surplus biochar generated during the process is stored in the receiving portion 212a along the first pipe 211a. 1 is configured to serve the same function as the reactor (210).
  • the second reactor 220a is filled with a predetermined amount of carbon adsorbent (activated carbon and / or biochar) therein, and a nickel distribution plate 221a communicating with the first reactor 210a at the lower portion thereof, and carbon Cyclone 222a for supplying the generated gas having reduced tar content to the refining means 40a as well as preventing the outflow of the adsorbent, and a second pipe 223a connecting the first and second reactors 210a and 220a. It is configured to serve the same function as the second reactor 220 of the first embodiment, and the like.
  • the nickel distribution plate 221a may be configured in a form in which a hook-shaped pipe protrudes toward the second reactor 220a at the upper end of each hole, unlike the nickel distribution plate 221 of the first embodiment. have.
  • the air supply line 310a to reduce the tar content in the product gas is installed in communication with the heat source supply means (30a).
  • the dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same can produce a product gas that minimizes the tar and ammonia content from the biomass by economically and efficiently adopting a nickel distribution plate.
  • the dual biomass gasification reactor of the present invention and the biomass gasification apparatus having the same has a separate internal reactor or two stages of the reactor inside, but by containing a carbon adsorbent in the upper reactor content of tar in the generated gas It can reduce and generate high calorific value gas and can be designed to have a medium-sized power generation capacity. This overcomes the limitation that existing fixed bed gasifiers can only be used in small power generation systems.
  • the dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same can also produce a high calorific value gas having a low content of tar and ammonia that can be stably used for electric power production and the like by providing a dual biomass gasification reactor.
  • the dual biomass gasification reactor of the present invention and the biomass gasification apparatus including the same also have a small installation space because the reactor can be dually configured so that the heat source of the lower reactor (first reactor) can be used as it is in the upper reactor (second reactor). The efficiency of the process can be increased.
  • the feedstock used in this experiment was 1kg of dry sewage sludge of 250 ⁇ 425 ⁇ m size as biomass and 500g of activated carbon as carbon adsorbent.
  • the gasifier is configured as shown in Figure 5, using a two-stage gasification reactor made of STS-316.
  • the lower reactor had a size of 100 mm in diameter and 360 mm in height, and was filled with silica sand therein.
  • three thermocouples were installed in the bottom reactor for flow stability testing.
  • the upper reactor was 160 mm in diameter and 340 mm in height and filled with activated carbon therein.
  • two thermocouples were installed in the upper reactor for flow stability testing.
  • Cyclone filtered the particle
  • the hot filter used the product of the specification which filters the particle
  • the condenser cooled the condensate liquid to 0 degreeC.
  • the generated gases were analyzed using GCs and GC-MS systems.
  • Equivalence ratio represents the amount of air that is chemically equivalent to the actual amount of air supplied during gasification / complete oxidation.
  • Example 1 using the nickel-plated stainless distribution plate produced gas compared to Comparative Example 2 (0.06 g / Nm 3 ) tested under the same conditions except that a stainless distribution plate instead of a nickel distribution plate It can be seen that the tar content (about 0.01 g / Nm 3 ) is reduced by about 6 times or more.
  • the ammonia content (about 12 mg / L) of the product gas obtained in Example 1 was confirmed to be reduced by about 58.3 times compared to Comparative Example 2 (700 mg / L).
  • the deactivation of the nickel distribution plate of Example 1 was not observed when the change of the product gas component was observed under the above experimental conditions.
  • Comparative Example 1 using a stainless distribution plate as in Comparative Example 2 but not filled with activated carbon in the upper reactor (second reactor) it was confirmed that the tar content is more.
  • Ammonia content of Comparative Example 1 was not measured, but considering the properties of activated carbon with ammonia adsorption, it is determined that it is 700 mg / L or more.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)

Abstract

La présente invention concerne un double réacteur de gazéification de la biomasse et un gazéificateur de biomasse l'utilisant, ledit réacteur comprenant un premier réacteur qui assure la gazéification de la biomasse introduite en faisant appel à une source de chaleur extérieure et à la chaleur d'oxydation de la biomasse et dans lequel du sable ou un catalyseur de pyrolyse des goudrons est introduit et se déplace avec le flux de chaleur extérieure afin d'assurer la gazéification de la biomasse et de produire du biochar ; un second réacteur en communication avec le premier de façon à utiliser les sources de chaleur de celui-ci et qui est rempli d'un agent adsorbant le carbone afin de faire baisser la teneur en goudron du gaz produit dans le premier réacteur et d'augmenter la production d'hydrogène en vue de l'acheminement du gaz en direction d'un processus ultérieur ; et une plaque de distribution qui se trouve dans la partie assurant la communication entre les premier et second réacteurs afin d'éviter le déplacement du biochar et du sable ou du catalyseur de pyrolyse des goudrons depuis le premier réacteur et en direction du second et afin, également, d'éviter les fuites d'agent adsorbant le carbone depuis le second réacteur et en direction du premier, ladite plaque de distribution étant une plaque en nickel. Il est possible, en utilisant le double réacteur de gazéification de la biomasse de la présente invention et le gazéificateur de biomasse l'utilisant, de produire du gaz à partir de biomasse de façon économique et efficace en minimisant les quantités de goudron et d'ammoniac produites.
PCT/KR2013/009559 2012-10-31 2013-10-25 Double réacteur de gazéification de la biomasse comportant une plaque de distribution en nickel et gazéificateur de biomasse l'utilisant Ceased WO2014069840A1 (fr)

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KR102465670B1 (ko) * 2020-11-11 2022-11-11 한국생산기술연구원 다수의 드래프트 튜브를 갖는 순환 유동층 가스화 장치 및 방법
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