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WO2011101540A1 - Système de gazéification sur lit fluidisé et procédé de gazéification de combustible dans un système de gazéification sur lit fluidisé - Google Patents

Système de gazéification sur lit fluidisé et procédé de gazéification de combustible dans un système de gazéification sur lit fluidisé Download PDF

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Publication number
WO2011101540A1
WO2011101540A1 PCT/FI2011/050138 FI2011050138W WO2011101540A1 WO 2011101540 A1 WO2011101540 A1 WO 2011101540A1 FI 2011050138 W FI2011050138 W FI 2011050138W WO 2011101540 A1 WO2011101540 A1 WO 2011101540A1
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Prior art keywords
fluidized bed
reactor
reaction chamber
bed reactor
gasification
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PCT/FI2011/050138
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English (en)
Inventor
Arto Ahvenainen
Eero Berg
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Amec Foster Wheeler Energia Oy
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Foster Wheeler Energia Oy
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    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
    • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
    • 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
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • 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
    • B01J8/1836—Heating and cooling the reactor
    • 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
    • B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • 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
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194—Tubes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
    • 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
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/501—Fluidised bed furnace with external recirculation of entrained bed material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/503—Fluidised bed furnace with two or more fluidised beds

Definitions

  • the present invention relates to a fluidized bed gasification sys- tern and a method of gasifying fuel in a fluidized bed gasification system according to the preambles of the independent patent claims.
  • the invention especially relates to a fluidized bed gasification system
  • a fluidized bed gasification reactor provided with a reaction chamber, means for supplying fuel to be gasified to the reaction chamber, means for fluidizing a particle bed being formed in the reaction chamber, means for gasifying the fuel to be gasified and a gas channel connected to the upper portion of the reaction chamber for removing gas produced in the gasification and particles entrained therewith from the reaction chamber; and a fluidized bed combustion reactor, provided with a reaction chamber, means for supplying fuel to be combusted to the reaction chamber, means for fluidizing a particle bed being formed in the reaction chamber, means for combusting the fuel to be combusted, and a gas channel connected to the upper portion of the reaction chamber for removing gas gener- ated in the combustion and particles entrained therewith from the reaction chamber; and in which a first fluidized bed reactor of said fluidized bed gasification reactor and fluidized bed combustion reactor is a circulating fluidized bed reactor, comprising recirculating means for particles, which
  • the invention especially relates to a method of gasifying fuel in a fluidized bed gasification system, comprising a fluidized bed gasification reactor provided with a reaction chamber and a gas channel connected to the upper portion of the reaction chamber for removing gas produced in the gasification and particles entrained therewith from the reaction chamber, and a fluidized bed combustion reactor provided with a reaction chamber and a gas channel connected to the upper portion of the reaction chamber for removing gas generated in the combustion and particles entrained therewith from the reaction chamber, in which a first fluidized bed reactor of said fluidized bed gasification reactor and fluidized bed combustion reactor is a circulating fluidized bed reactor, comprising recirculating means for particles, which have a particle separator arranged in the gas channel connected to the upper portion of the reaction chamber of the first fluidized bed reactor for separating particles entrained with the gas from the gas, and a return channel for recirculating separated particles from the particle separator to the lower portion of the reaction chamber of the first fluidized bed reactor, in which method fuel to be gas
  • the gasification of fuel is an endothermic process, which requires external thermal energy.
  • a conventional method to produce the required thermal energy is to combust a portion of the fuel to be gasified in a gasification reactor.
  • a disadvantage of this method is that the amount of the product gas gained from a certain amount of fuel decreases and carbon dio- xide generating in the combustion is mixed with the product gas, which degrades the quality of the product gas and diminishes the heat value thereof.
  • Another conventional solution is to combust suitable fuel in a separate combustion reactor and transfer hot ash from the combustion reactor to the gasifi- cation reactor. The transfer of hot ash from the combustion reactor to the reaction chamber of the gasification reactor requires, however, rather complicated equipment, especially if the reactors operate at different pressures. The manufacture of the apparatus and the maintenance thereof can, thus, be ex- pensive.
  • US Patent No. 4,459,201 discloses a pyrolyzer, in which residual carbon generated in a pyrolyzer is combusted in a separate combustion reactor and in a combustion space situated in the reaction chamber of the py- rolyzer, said space being formed either of a multipart combustion zone or of multiple parallel combustion tubes. Thereby, thermal energy is transferred through the walls of the multipart combustion space situated in the reaction chamber of the pyrolyzer to the pyrolyzer.
  • This apparatus is rather complicated, difficult to control and liable to disturbances.
  • the mainten- ance of the multipart combustion space arranged in the reaction chamber of the pyrolyzer, and possible repairing operations thereof, are difficult to perform.
  • EP patent no. 1 377 650 B1 discloses a solution, in which the reaction chamber of a pyrolyzer is arranged in the reaction chamber of a flui- dized bed reactor combusting residual carbon of the pyrolyzer.
  • the heat exchange surface between the reaction chamber of the pyrolyzer and the reaction chamber of the combustion reactor is relatively small, whereby the heat exchange efficiency may in some cases be inade- quate.
  • too hot or poorly fluidized areas may be generated close to the heat exchange surfaces. There the temperature of the gasification reactor may locally rise too high, which can decrease the product gas yield.
  • An object of the present invention is to provide an efficient fluidized bed gasification system and a method of gasifying fuel in a fluidized bed gasification system, in which problems of the prior art have been minimized.
  • a fluidized bed gasification system in accordance with the characterizing part of the independent apparatus claim is provided.
  • the means for gasifying the fuel to be gasified comprise a first portion of the recirculating means of the first fluidized bed reactor, which first portion is arranged gas-tight inside the reaction chamber of a second fluidized bed reactor of said fluidized bed gasification reactor and fluidized bed combustion reactor, which second fluidized bed reactor is not the above-mentioned first fluidized bed reactor, for gasifying the fuel to be gasified by transferring heat from the particles of the fluidized bed combustion reactor through an outer wall of the first portion to the particles of the fluidized bed gasification reactor.
  • a method in accordance with the characterizing part of the independent method claim is provided in order to diminish above-mentioned problems of the prior art.
  • a method of gasifying fuel is provided, in which the fuel to be gasified is gasified by transferring heat from the particles of the fluidized bed combustion reactor to the particles of the fluidized bed gasification reactor through the outer wall of a first portion of the recirculating means of the first fluidized bed reactor, which first portion is arranged gas-tight inside the reaction chamber of a second fluidized bed reactor of said fluidized bed gasification reactor and fluidized bed combustion reactor, which second fluidized bed reactor is not the above-mentioned first fluidized bed reactor.
  • heat is transferred thus from the hot particulate bed material of the fluidized bed combustion reactor, which is hereafter also referred to as combustion reactor, by conduction to the particulate bed material of the fluidized bed gasi- fication reactor, which is hereafter also referred to as gasification reactor, through the outer wall limiting the first portion of the recirculating means of the first fluidized bed reactor arranged inside the reaction chamber of the second fluidized bed reactor.
  • combustion reactor which is hereafter also referred to as combustion reactor
  • gasification reactor the particulate bed material of the fluidized bed gasi- fication reactor
  • the temperatures of the reaction chamber and the recirculating means of the fluidized bed reactor can be well controlled, the temperatures in different sides of the metal heat exchange surface can advantageously be continuously adjusted to be stable and such that the desired heat exchange efficiency can be obtained, but the temperature of the heat exchange surface will not rise too high in view of the gasification of the fuel.
  • the gas-tight arrangement of the first portion of the recirculating means of the first fluidized bed reactor inside the reaction chamber of the second fluidized bed reactor refers to that no direct transfer of gas or any oth- er substance takes place between the first portion of the recirculating means of the first fluidized bed reactor and the reaction chamber of the second fluidized bed reactor.
  • Merely thermal energy is transferred by conduction through the wall limiting the first portion of the recirculating means, in other words through the outer wall thereof.
  • the processes of the first fluidized bed reactor and the second fluidized bed reactor do not affect each other otherwise, and the processes can be, for example, at different pressures.
  • the heat exchange surface is the outer wall limiting the first portion of the recirculating means of the first fluidized bed reactor
  • the heat exchange efficiency can be advantageous- ly controlled by adjusting the amount of the material recirculating in the recirculating means of the first fluidized bed reactor, in other words the amount of the particles separating in the particle separator of the fluidized bed reactor. This may be advantageously carried out, for example, by varying the total amount of the bed material in the first fluidized bed reactor.
  • the first fluidized bed reactor is a combustion reactor and the second fluidized bed reactor is a gasification reactor.
  • the combustion reactor is a circulating fluidized bed reactor.
  • the gasification reactor may be either a circulating fluidized bed reactor or a fluidized bed reactor of another kind , for example, a bubbling fluidized bed reactor.
  • a portion of the recirculating means of the fluidized bed combustion reactor, a so called first portion of the recirculating means, is arranged gas- tight inside the reaction chamber of the gasification reactor.
  • the first fluidized bed reactor is a gasification reactor and the second fluidized bed reactor is a combustion reactor.
  • the gasification reactor is a circulating fluidized bed reactor.
  • the combustion reactor can be either a circulating fluidized bed reactor or a fluidized bed reactor of another kind, for example, a bubbling fluidized bed reactor.
  • the first portion of the recirculating means of the fluidized bed gasification reactor is arranged gas-tight inside the reaction chamber of the combustion reactor.
  • Said first portion of the recirculating means of the first fluidized bed reactor preferably comprises at least a portion of the return channel of the recirculating means.
  • Said portion of the return channel can be either a conventional, simple tube channel, but according to a preferred embodiment of the invention, said portion of the return channel is at least partially divided into two or more parallel channel branches.
  • Such a return channel, which is divided into channel branches provides a larger heat exchange surface than a simple return channel and, thus, intensifies the heat exchange between the particles flowing in the return channel and the particles in the reaction chamber of the second fluidized bed reactor.
  • the portion of the return channel comprising the first portion of the recirculating means also other means, with which heat exchange between the particles of the first fluidized bed reactor flowing in the return channel and the particles in reaction chamber of the second fluidized bed reactor is improved.
  • Such means can be, for example, guiding means or chambers arranged in the return channel or on the walls thereof, by means of which heat exchange between the particles flowing in the return channel and the walls of the return channel, is improved.
  • the temperature of the fluidized bed combustion reactor is preferably adjusted such that a required amount of heat for maintaining the gasification process is transferred from the hot particles of the combustion reactor to the gasification reactor, but the temperature of the bed of the gasification reactor does not rise too high at any point. Since in the arrangements in accordance with the present invention, the heat exchange always takes place between the particles of the fluidized bed and the particles flowing in the recirculating means, the heat exchange is efficient and accurately adjustable.
  • the particle separator of the recirculating means of the first fluidized bed reactor is preferably a cyclone, but it can in some cases also be of other type, such as a multicyclone or an impact separator.
  • the first portion of the recirculating means of the first fluidized bed reactor in other words, the portion of the recirculating means of the fluidized bed reactor remaining inside the reaction chamber of the second fluidized bed reactor, comprises a particle separator or at least a portion of the particle separator.
  • the particle separator remaining either completely or partially inside the reaction chamber of the second fluidized bed reactor is advantageously a cyclone, the geometry of which can be conven- tional.
  • the particle separator is, however, preferably a cyclone, the height of which is greater than that of a conventional separator in order to improve the heat exchange, more preferably at least 30%, and most preferably at least 50% of the height of the reaction chamber of the second fluidized bed reactor.
  • the shape of the reaction chamber of the second fluidized bed reactor comprising a particle separator of the recirculating means of the first fluidized bed reactor or a portion thereof may be conventional, in other words the cross-section of the reaction chamber may be constant in the majority of the reaction chamber.
  • the cross-sectional area of the upper portion of the reaction chamber of the second fluidized bed reactor is, however, greater than the cross-sectional area of the rest of the reaction chamber.
  • the particle separator of the recirculating means of the first fluidized bed reactor is preferably arranged in the upper portion of the above-mentioned reaction chamber of the second fluidized bed reactor, in which upper portion the horizontal cross-sectional area of the reaction chamber is greater than that in the portion of the reaction chamber below the particle separator.
  • the second fluidized bed reactor is a circulating fluidized bed reactor, comprising recirculating means for particles provided with a particle separator arranged in the gas channel connecting to the upper portion of the reaction chamber of the second fluidized bed reactor for separating particles entrained with the gas and a return channel for returning separated particles to the lower portion of the reaction chamber of the second fluidized bed reactor, and a first portion of the recirculating means of the second fluidized bed reactor is arranged gas-tight inside the reaction chamber of the first fluidized bed reac- tor.
  • a fluidized bed gasification system in accordance with this embodiment thus comprises two circulating fluidized bed reactors, of which the first portion of the recirculating means of the first fluidized bed reactor is arranged inside the reaction chamber of the second fluidized bed reactor and the first portion of the recirculating means of the second fluidized bed reactor is arranged inside the reaction chamber of the first fluidized bed reactor.
  • the first portion of the recirculating means of both fluidized bed reactors can comprise a portion of the return channel and/or at least a portion of the particle separator.
  • the first portions of the recirculating means of the fluidized bed reactors can vary, for example, in such a way that the first portion of the recirculating means of the first fluidized bed reactor comprises a portion of the return channel and the first portion of the recirculating means of the second fluidized bed reactor comprises at least a portion of the particle separator.
  • the portion of the return channel of either of the reactors being inside the reaction chamber of the other reactor can be a simple tube structure or it may be formed of parallel channel branches in the above-described manner.
  • the particle separator of either of the reactors being at least partially inside the reaction chamber of the other reactor can be of conventional shape, or it can be clearly higher than the conventional in the above- described manner.
  • the cross-sectional area of the reaction chamber of either of the fluidized bed reactors containing at least a portion of the particle sepa- rator of the other fluidized bed reactor can be mainly constant as in the conventional cases, or it can be greater than the cross-sectional area of the rest of the reaction chamber in the above-described manner.
  • the fuel used in the fluidized bed combustion reactor can be any suitable solid fuel.
  • the fuel used in a combustion reactor in accordance with a preferred embodiment is ash containing unburned carbon removed from the gasification reactor.
  • the gasification reactor is a py- rolysis reactor, it is possible to advantageously use residual carbon produced by the pyrolysis reactor as fuel for the combustion reactor.
  • the gasification reactor relates to a Fischer-Tropsch (FT) process, whereby methane and other tail gases obtained as a side product from the FT process can preferably be used as fuels of the combustion reactor.
  • the operational temperature of the fluidized bed combustion reactor is preferably about 700 - 800 °C.
  • the fuel to be gasified in the fluidized bed gasification reactor is preferably solid carbonaceous fuel, for example, biofuel.
  • the operational temperature of the fluidized bed gasification reactor is preferably 400-500 °C, whereby the fuel to be gasified pyrolyzes due to the heat and is ground to fine residual carbon (coke dust).
  • the gasification process can be intensified, if necessary, for example, by means of oxygen or oxygen/steam mixture used as fluidizing gas.
  • the gasification reactor is a pyrolysis reactor, it is also possible to use purified product gas at an appropriate pressure or, for example, tail gas removed from the FT process as a fluidizing gas for the reactor.
  • the gasification process is pressurized.
  • the combustion process and the gasification process can be separated as for material flows, and therefore the gasification process can preferably be carried out pressurized.
  • the above described gasification process in which heat is transferred to the particles of the fluidized bed gasification reactor heat from the hot particles of the fluidized bed combustion reactor, can be completed by supplying heat to the gasification reactor in some other known manner, for example, by means of superheated steam generated by the combustion reactor or by some other separately generated hot medium.
  • FIG. 2 schematically illustrates a fluidized bed gasification system in accordance with a second preferred embodiment of the present invention
  • FIG. 3 schematically illustrates a fluidized bed gasification system in accordance with a third preferred embodiment of the present invention
  • FIG. 4 schematically illustrates a fluidized bed gasification system in accordance with a fourth preferred embodiment of the present invention
  • FIG. 5 schematically illustrates a fluidized bed gasification system in accordance with a fifth preferred embodiment of the present invention
  • Fig. 1 shows a fluidized bed gasification system in accordance with a preferred embodiment of the present invention, which comprises a fluidized bed gasification reactor 10 and a fluidized bed combustion reactor 30, which both are circulating fluidized bed reactors.
  • the lower portion of the reaction chamber comprises means for fluidizing the particle bed forming to the reaction chamber 12, in other words a grid 20, an inlet means 22 for fluidizing gas and a wind box 24.
  • the reaction chamber also comprises means 26 for introducing the fuel to be gasified, for example, a feed channel or feed screw for fuel, and means 28 for removing the bottom ash generated in the gasification, for example, a bottom ash screw.
  • the lower portion of the reaction chamber comprises means for fluidizing the particle bed forming to the reaction chamber 32, in other words a grid 40, an inlet means 42 for fluidizing gas and a wind box 44.
  • the reaction chamber comprises also means 46 for introducing the fuel to be gasified, for example, a feed channel or feed screw for fuel, and means 48 for removing the bottom ash generated in the combustion, for example, a bottom ash screw.
  • a portion of the return channel 18 of the gasification reactor 10 a so called first portion 50 is arranged inside the reaction chamber of the combustion reactor 30.
  • the height of the first portion 50 of the return channel 18 of the gasification reactor 10 is preferably a considerable portion of the height of the reaction chamber 32, preferably at least 50%, more preferably at least 70% of the height of the reaction chamber 32. It is possible to control the heat exchange efficiency in the first portion 50 of the return channel, and, thus, the temperature of the gasification reactor by adjusting the amount of the particles to be separated in the particle separator 16 of the gasification reactor. This can be performed, for example, by changing the volume or particle size of the particle bed formed in the gasification reactor. Another possibility to control the temperature of the gasification reactor is to vary the temperature in the combustion reactor or the volume or particle size or fluidization velocity of the particle bed in the combustion reactor.
  • the fluidized bed gasification systems in accordance with the present invention also comprise many other portions and details known per se, which, however, are not important in view of the present invention, and have therefore not been shown in Figs. 1 -6.
  • Figs. 2-6 same reference numbers as in Fig. 1 have been used with elements that are similar to the corresponding elements in Fig. 1 .
  • the combustion reactor 30 in the arrangement shown in Fig. 1 is a circulating fluidized bed reactor, but it could also be other type of fluidized bed reactor, for example, a bubbling bed reactor.
  • a portion of the return channel 18 of the gasification reactor 10 is arranged inside the reaction chamber 32 of the combustions reactor 30.
  • a second alternative arrangement, which comes into question when the combustion reac- tor is a circulating fluidized bed reactor, is that a portion of the return channel of the combustion reactor is arranged inside the reaction chamber of the gasification reactor.
  • the gasification reactor may then be also of other fluidized bed reactor type, such as a bubbling bed reactor.
  • a fluidized bed gasification system in accordance with a second preferred embodiment of the present invention shown in Fig. 2 differs from the gasification system shown in Fig. 1 especially in that the portion of the return channel 18 of the gasification reactor 10 in the reaction chamber 32 of the combustion reactor 30 is divided into a number of parallel channel branches 54.
  • the particle separator of Fig. 2 is preferably a multicyclone 56.
  • the channel branches 52 preferably continue through the wind box 44 of the combustion reactor to a bottom funnel 58, from which they are returned along a common final portion of the return channel 18 to the gasification reactor 10.
  • the combustion reactor 30 is a circulating fluidized bed reactor, but, as in case of Fig. 1 , it could also be of other fluidized bed reactor type, such as a bubbling bed reactor.
  • the channel branches 54 of the gasification reactor 10 in the embodiment illu- strated in Fig. 2 are arranged inside the reaction chamber of the combustion reactor 30.
  • An alternative that comes into question when the combustion reactor is a circulating fluidized bed reactor is that the return channel of the combustion reactor is divided into parallel channel branches, which are arranged inside the reaction chamber of the gasification reactor.
  • the gasification reactor can then be also of other fluidized bed reactor type, such as bubbling bed reactor.
  • a fluidized bed gasification system in accordance with a third preferred embodiment of the present invention illustrated in Fig. 3 differs from the gasification system illustrated in Fig .1 in that the particle separator 36 of the combustion reactor 30 and a portion of a return channel 38 are arranged inside the reaction chamber 12 of the gasification reactor 10.
  • thermal energy is transferred from the particles of the combustion reactor to the particles of the gasification reactor both in a portion of the return channel 18 of the gasification reactor 10 and in the par- tide separator 36 of the combustion reactor 30 and in a portion of the return channel 38 of the combustion reactor.
  • the particle separator of a conventional fluidized bed reactor is relatively low compared, for example, with the height of the reaction chamber of the same reactor, typically approximately 20% of the height of the reaction chamber.
  • the circumference of the outer wall of the particle separator is, however, clearly larger than the circumference of the return channel, and therefore the use of the outer surface of the particle separator 36 of the combustion reactor 30 as a heat exchange surface significantly increases the heat exchange surface area between the combustion reactor and the gasification reactor.
  • the heat exchange efficiency of the arrangement disclosed in Fig 3 is clearly greater than, for example, the heat exchange efficiency of the embodiment disclosed in Fig.1 .
  • the efficiency of the heat exchange from the particles of the combustion reactor 30 to the particles of the gasifica- tion reactor 10, and, thus, the temperature of the gasification reactor may be controlled by adjusting the amount of the particles separated in the particle separator of either of the fluidized bed reactors or by adjusting the temperature of the combustion reactor, in the same manner as shown in connection with Fig. 1 .
  • the cross-sectional area of the return channel arranged inside the reaction chamber of the fluidized bed reactor is generally clearly smaller than the cross-sectional area of the reaction chamber, and therefore the return channel arranged inside the reaction chamber does not considerably disturb the process taking place in the reaction chamber.
  • the cross-sectional area of the particle separator 36 of the combustion reactor 30 arranged in the reaction chamber of the gasification reactor 10 instead can be a considerable portion of the cross-sectional area of the reaction chamber 12.
  • the portion of the reaction chamber 12, in which the particle separator is positioned is called an upper portion 60 of the reaction chamber.
  • the cross-sectional area of the upper portion 60 of the reaction chamber is preferably greater than the cross-sectional area of the portion of the reaction chamber below the upper portion.
  • the portion of the return channel 18 of the gasification reactor 10 inside the reaction chamber 32 of the combustion reactor 30 comprises guiding plates 62, by means of which the heat transfer is intensified from the particles in the reaction chamber 32 of the combustion reactor 30 to the particles flowing in the return channel 18.
  • guiding plates it is also possible to use guiding means of other types, or chambers or other suit- able constructions for intensifying the heat transfer. Such constructions may be arranged either inside the return channel 18 or outside thereof, in the reaction chamber 32 of the combustion reactor 30.
  • a fluidized bed gasification system in accordance with a fourth preferred embodiment of the present invention disclosed in Fig. 4 differs from the gasification system of Fig. 3 in that the height of the particle separator 36 of the combustion reactor 30 arranged inside the reaction chamber 12 of the gasification reactor 10 is clearly greater than that of a conventional separator.
  • the height of the particle separator 36 is preferably at least 30%, most preferably at least 50%, of the height of the reaction chamber 12.
  • the surface area of the wall between reaction chamber 12 of the gasification reactor 10 and the particle separator 36 of the combustion reactor 30 arranged inside the reaction chamber 12 of the gasification reactor 10 is thus greater than that in the arrangement in accordance with Fig.3. This results in that the heat transfer efficiency from the particles of the combustion reactor 32 to the particles of the gasification reactor 10 is greater than in the arrangement in accordance with Fig. 3.
  • the upper portion 60 of the reaction chamber 12 is preferably higher than that in the arrangement in accordance with Fig. 3.
  • the cross-sectional area of which is greater than the cross-sectional area of the rest of the reaction chamber is preferably higher than that in the arrangement in accordance with Fig. 3.
  • the particle separator 16 of the gasification reactor 10 is arranged outside the reaction chamber 32 of the combustion reactor 30, but the return channel 18 of the gasification reactor is mainly inside the reaction chamber 32 of the combustion reactor 30 and the particle separator 36 of the combustion reactor 30 is entirely inside the reaction chamber 12 of the gasification reactor 10.
  • the particle separator of the combustion reactor is ar- ranged outside the reaction chamber of the gasification reactor, but the return channel 38 of the combustion reactor 30 is mainly arranged inside the reaction chamber 12 of the gasification reactor and the particle separator 16 of the gasification reactor 10 is arranged entirely inside the combustion chamber 32 of the combustion reactor 30.
  • the fluidized bed gasification system in accordance with a fifth preferred embodiment of the present invention disclosed in Fig. 5 differs from the gasification systems of Figs. 3 and 4 in that the particle separator 16 of the gasification reactor 10 is partially arranged inside the reaction chamber 32 of the combustion reactor 30. Moreover, the height of the particle separator 16 of the gasification reactor 10 arranged inside the reaction chamber 32 of the combustion reactor 30 is clearly greater than that of a conventional separator. The height of the particle separator 16 is preferably at least 30%, more preferably at least 50%, of the height of the reaction chamber 32. Thus, the heat exchange efficiency from the particles of the combustion reactor 30 to the gasification reactor 10 is still higher than that in the arrangements in accordance with Figs. 3 and 4.
  • the particle separator 16 of the gasification reactor 10 is mainly arranged inside the reaction chamber 32 of the combustion reactor 30 and the particle separator 36 of the combustion reactor 30 is arranged entirely inside the combustion chamber 12 of the gasification reactor 10.
  • the corresponding arrangement can also be realized reversely, in other words in such a way that the particle separator 36 of the combustion reactor 30 is arranged mainly inside the reaction chamber 12 of the gasification reactor 10 and the particle separator 16 of the gasification reactor 10 is arranged entirely inside the combustion chamber 32 of the combustion reactor 30.
  • An arrangement closely related to the present invention which, however, to a certain extent deviates from the above described arrangements, is to arrange the first portion of the recirculating means of the gasifica- tion reactor, which is a circulating fluidized bed reactor, inside the flue gas channel of the combustion reactor, especially to the first portion of a flue gas channel downstream of the particle separator, a so called back pass.
  • the first portion of the recirculating means of the gasifica- tion reactor which is a circulating fluidized bed reactor
  • the first portion of the recirculating means of the gasifica- tion reactor which is a circulating fluidized bed reactor

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un système de gazéification sur lit fluidisé et un procédé de gazéification de combustible dans un système de gazéification sur lit fluidisé, ledit système de gazéification comportant un réacteur de gazéification à lit fluidisé et un réacteur de combustion à lit fluidisé, caractérisé en ce qu'un premier réacteur à lit fluidisé parmi ledit réacteur de gazéification à lit fluidisé et ledit réacteur de combustion à lit fluidisé est un réacteur à lit fluidisé circulant, dont une première partie des moyens de circulation est disposée de manière étanche aux gaz à l'intérieur de la chambre de réaction d'un deuxième réacteur à lit fluidisé servant à gazéifier du combustible à gazéifier en transférant, à travers la paroi extérieure de la première partie, de la chaleur des particules du réacteur de combustion à lit fluidisé aux particules du réacteur de gazéification à lit fluidisé.
PCT/FI2011/050138 2010-02-17 2011-02-15 Système de gazéification sur lit fluidisé et procédé de gazéification de combustible dans un système de gazéification sur lit fluidisé Ceased WO2011101540A1 (fr)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104449872A (zh) * 2014-12-11 2015-03-25 余传林 一种细粒子生物质或固体化石燃料的气化工艺系统
KR102355503B1 (ko) * 2021-03-15 2022-02-08 이정율 복합 운용성 및 병렬 확장성을 가지는 싸이클론 열전달 방식의 폐합성수지 열분해 시스템
WO2025210997A1 (fr) * 2024-04-05 2025-10-09 荏原環境プラント株式会社 Procédé de gazéification par décomposition thermique
WO2025210996A1 (fr) * 2024-04-05 2025-10-09 荏原環境プラント株式会社 Système de gazéification par décomposition thermique

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US4459201A (en) * 1982-03-19 1984-07-10 Exxon Research And Engineering Co. Oil shale retorting process utilizing indirect heat transfer
CN2484328Y (zh) * 2001-07-16 2002-04-03 中国科学院广州能源研究所 自热式循环流化床生物质热解油化装置
US20020078867A1 (en) * 2000-11-17 2002-06-27 Paisley Mark A. Small scale high throughput biomass gasification system and method

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Publication number Priority date Publication date Assignee Title
US4459201A (en) * 1982-03-19 1984-07-10 Exxon Research And Engineering Co. Oil shale retorting process utilizing indirect heat transfer
US20020078867A1 (en) * 2000-11-17 2002-06-27 Paisley Mark A. Small scale high throughput biomass gasification system and method
CN2484328Y (zh) * 2001-07-16 2002-04-03 中国科学院广州能源研究所 自热式循环流化床生物质热解油化装置

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104449872A (zh) * 2014-12-11 2015-03-25 余传林 一种细粒子生物质或固体化石燃料的气化工艺系统
CN104449872B (zh) * 2014-12-11 2016-08-10 余传林 一种细粒子生物质或固体化石燃料的气化工艺系统
KR102355503B1 (ko) * 2021-03-15 2022-02-08 이정율 복합 운용성 및 병렬 확장성을 가지는 싸이클론 열전달 방식의 폐합성수지 열분해 시스템
WO2025210997A1 (fr) * 2024-04-05 2025-10-09 荏原環境プラント株式会社 Procédé de gazéification par décomposition thermique
WO2025210996A1 (fr) * 2024-04-05 2025-10-09 荏原環境プラント株式会社 Système de gazéification par décomposition thermique

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