WO2000006671A1 - Procede et dispositif pour la formation de gaz de synthese a partir de biomasse et de matieres residuelles - Google Patents

Procede et dispositif pour la formation de gaz de synthese a partir de biomasse et de matieres residuelles Download PDF

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Publication number
WO2000006671A1
WO2000006671A1 PCT/NL1999/000481 NL9900481W WO0006671A1 WO 2000006671 A1 WO2000006671 A1 WO 2000006671A1 NL 9900481 W NL9900481 W NL 9900481W WO 0006671 A1 WO0006671 A1 WO 0006671A1
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Prior art keywords
zone
pyrolysis
gasification
feed
discharge
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Ceased
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PCT/NL1999/000481
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English (en)
Inventor
Katrien Hemmes
Hubertus Johannes Veringa
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Energy Research Centre of the Netherlands
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Energy Research Centre of the Netherlands
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Publication date
Application filed by Energy Research Centre of the Netherlands filed Critical Energy Research Centre of the Netherlands
Priority to AU51992/99A priority Critical patent/AU5199299A/en
Priority to EP99937102A priority patent/EP1114128A1/fr
Priority to JP2000562455A priority patent/JP2002521553A/ja
Publication of WO2000006671A1 publication Critical patent/WO2000006671A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • C10J3/46—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
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to a method and a device for forming synthesis gas from non-fossil, carbon-containing biological material (biomass), which device comprises:
  • a pyrolysis zone having a first feed for the carbon- containing material, having a second feed for an inert heat- transfer material, for forming gaseous pyrolysis products and a solid carbonization product (char) virtually in the absence of oxygen, and having a discharge for the heat-transfer material and the carbonization product,
  • - a gasification zone having a first feed for a gasification agent, having a second feed, which is connected to the pyrolysis zone, for feeding the heat-transfer material and the carbonization product formed in the pyrolysis zone, having a first discharge for product gas formed in the gasification zone, and having a second discharge for the heat-transfer material, and also having a first discharge for combustion gases formed in the combustion zone, and having a second discharge for the heat-transfer material, and - a return path, which is located between the second discharge of the gasification zone and the second feed of the pyrolysis zone, for feeding the heat-transfer material from the gasification zone to the pyrolysis zone.
  • the ideal product gas as a raw material for producing liquid energy carriers i.e. "downstream processes” has a high calorific value (without nitrogen) , so that a relatively small volumetric flow is required in a compact “downstream” installation, and is clean, without tar- like materials.
  • US-A-3, 853, 498 discloses a device with two fluidized-bed reactors which are coupled together.
  • finely ground biomass is converted by pyrolysis in a fluidized sand bed, in the absence of oxygen, into gaseous pyrolysis products, such as CO, C02 and other gaseous pyrolysis products, and into a solid carbonization product (char) .
  • gaseous pyrolysis products such as CO, C02 and other gaseous pyrolysis products
  • char solid carbonization product
  • the solid carbonization product is fed with the sand from the first reactor to a combustion zone in the second reactor, where the carbonization product is burnt by adding air via a booster.
  • the heat-transfer material (sand) which has been heated in the fluidized-bed combustion zone, is returned to the pyrolysis reactor, in order to provide the energy required for the endothermic pyrolysis reaction.
  • Gaseous pyrolysis products from the pyrolysis reactor are converted into methane in a water gas shift reactor, a C02 scrubber and a methanization reactor.
  • Japanese patent application No. 56038719 discloses a fluidized-bed reactor in accordance with the preamble of Claim 1, for gasification of particulate material, with three annular outer zones, which are separate from one another, and, coaxially with the outer zones, three inner zones, which are separated by partitions.
  • the combustible carbon-containing organic material is converted by pyrolysis into gaseous pyrolysis products and a carbonization product.
  • some of the carbonization product is burnt, with the result that the bed material is heated, and then the bed material, together with the remaining solid carbonization product, is fed to a gasification zone in which steam or C02 is introduced as the gasification agent.
  • the product gas is discharged from the gasification zone, while the cooled bed material is recirculated to the pyrolysis zone.
  • European patent application EP-A-0, 219, 163 discloses a process for cracking hydrocarbons in which the carbonization products, which have been deposited on a solid material, are fed from the pyrolysis zone to a gasification zone for forming hydrogen-containing product gas while steam is being fed in.
  • the process heat which is required is supplied by combustion of at least some of the product gas (synthesis gas) , specifically in such a manner that pyrolysis takes place at the highest process temperatures and gasification at the lowest process temperatures.
  • the product gas from the gasification zone comprises relatively large amounts of tar-like materials and that relatively complex gas-purification installations are required in order to purify the product gas, which product gas is not directly suitable as an "upstream" process for the production of liquid energy carriers.
  • the product gas when air is used as the oxidizing agent, comprises relatively large amounts of nitrogen, with the result that the calorific value is reduced.
  • the known processes are relatively inefficient.
  • the yield of pure product gas is relatively low owing to the unfavourable temperature distribution.
  • one object of the present invention is to provide a relatively simple device for efficiently forming synthesis gas from biomass which results in a clean product gas with a high calorific value.
  • the device according to the present invention is characterized in that the pyrolysis zone and the combustion zone are connected to the gasification zone in such a manner that at least virtually no gaseous products are able to pass from the combustion zone and the pyrolysis zone to the gasification zone, a gas discharge of the pyrolysis zone being connected to a third feed leading to the combustion zone, in order to feed the solid carbonization product to the combustion zone separately from substantially completely gaseous pyrolysis products.
  • the invention is based on the insight that the pyrolysis zone and the combustion zone are separated from the gasification zone in such a manner that it is impossible for gaseous pyrolysis products or combustion gases to reach the gasification zone and that at least substantially only the solid carbonization product is converted into product gas in the gasification zone. Since the solid carbonization product is relatively pure and is free from tar-like and/or cyclic hydrocarbon compounds, a pure product gas which comprises CO, C02 and H2 is obtained at the gas discharge from the gasification zone. Since no off-gases from the combustion zone are fed to the gasification zone, the product gas does not contain any nitrogen, so that it may have a high calorific value.
  • the product gas or synthesis gas can be converted directly into desired hydrocarbon products, without using complex gas-purification and air-separation installations .
  • the heat-transfer or bed material in addition to its function in a normal fluidized-bed system, also has the dual function of both heat transfer and mass transfer.
  • the heat produced in the combustion zone is transferred to the bed material and is then transferred to the gasification zone together with the carbonization products, by means of the bed material.
  • the bed material is cooled by the endothermic gasification process, after which the cooled bed material is recirculated to the pyrolysis zone ("coke producer") . Together with the hot bed material, the carbonization product formed in the pyrolysis zone is transported from the pyrolysis zone to the gasifier.
  • the pyrolysis according to the invention takes place at relatively low temperatures, such as between 300°C and 500°C.
  • the gasification takes place at relatively high temperatures, such as for example around 850°C.
  • the device according to the present invention therefore results in optimum separation of product gas and undesirable components, such as tar from the biomass and nitrogen from the air. Since the pyrolysis product comprises a condensable fraction and a non- condensable fraction, and excess heat is produced in the process, it may be useful also to separate the hot pyrolysis gas and to use one of the components for combustion and another for an alternative application.
  • the combustion zone is located in a separate burner, the discharge of the heat-transfer agent and the carbonization product from the pyrolysis zone being connected to the gasifier.
  • the heat for this gasifier is transferred from the burner via the bed material.
  • This cooled bed material is passed on to the pyrolysis reactor.
  • Bed material from the gasifier, from which its carbonization product has been removed, is also returned to the burner.
  • the heat which is generated in the burner and is not required for pyrolysis and the gasification process is available as a high-grade energy carrier, but may also be used within the process for pretreatment of the biomass and for steam production.
  • the heat can also be used to drive a pneumatic particle conveyor for the heat transfer material, and may furthermore be used to enable the system to operate at pressure (approx. 7 bar) and to compress the product gas to approximately 40 bar.
  • the latter compression step provides a base material which can be converted directly to methanol or another hydrocarbon.
  • the burner is located within the pyrolysis zone.
  • a second burner is connected to the gas discharge of the pyrolysis zone for combustion of some of the gaseous pyrolysis products, which second burner is thermally connected to a water feed for the generation of steam, which steam, via a steam line, is connected to the first feed of the gasification zone.
  • An advantageous and compact device is formed by an "interconnected fluid bed” (IFB ) reactor as an alternative to reactor systems with pneumatic particle transport.
  • the IFB reactors provide particle transport, and therefore, in this case, mass transfer and heat transfer, by regulating the gas velocities for fluidization, with the result that there is very little damage to the particles of the heat-transfer material, and loss of material remains limited.
  • the IFB reactors are relatively small, so that they take up little floor space.
  • both the pyrolysis zone and the gasification zone form a two-stage reactor, in which the heat-transfer medium can flow from the first, high column, via a common free edge, into the adjoining column of lower height.
  • the heat-transfer material and the carbonization product can pass to the higher column of the gasification zone.
  • the cooled heat-transfer material can move back into the higher column of the pyrolysis zone through an opening located in the vicinity of the underside.
  • the four columns ( or a multiplicity thereof) are connected to one an o ther in a thermall y conductive manner via a partition s o that, if des i red, complete thermal integration takes place. Due to the absence of mechanical transport means, there is little wear to components and particles.
  • the compact, insulated IFB reactor exhibits a minimal heat loss to the environment and is simple to control.
  • Fig. 1 shows a diagrammatic depiction of the method and of the operating principle of the device according to the present invention
  • Fig. 2 shows a diagrammatic depiction of a device for forming synthesis gas according to the present invention
  • Fig. 3 shows a device according to the present invent i on with an external burner
  • Fig. 4 shows an interconnected fluidized-bed reactor [ ( IFB ) reactor] which operates using the principle shown in
  • Fig 5 shows a second embodiment of a device accord i ng to the present invention, with a burner integrated in the pyrolysis zone.
  • Fig 1 shows an integrated pyrolysis zone and burner, otherwise known as "coke producer" 1, having a first feed 2 for biomass and having a second feed 3 for a bed material, such as for example sand or a catalytically active mater i al for controlling the product quality.
  • biomass is intended to mean a carbon-containing mater i al, other than fossil carbon sources, derived for example from vegetable, fruit and garden waste, cellulose residues, domestic waste containing plastics, and the like.
  • an oxidizing agent such as air or pure oxygen, is fed to the combustion zone of the coke producer 1.
  • the solid pyrolysis products, together with the heated bed material, are discharged from the coke producer 1 to a feed 9 of a gasifier 7.
  • a feed 8 steam is fed to the gasifier 7 as a gasification agent for converting the coke or char into a product gas which is clean (i.e. free from tar-like materials) and has a high calorific value (i.e. without nitrogen) .
  • the heat required for the endothermic gasification reaction is supplied by the bed material, the temperature of which, at the location of the gasifier, is at most 1200°C, for example approx. 850°C.
  • gasification of the solid pyrolysis products or coke results in a very pure product gas and that, as a result of the off-gases from the coke producer 1, including the gaseous pyrolysis products and combustion products, being separated from the gasification zone, the product gas has a high calorific value.
  • Fig. 2 shows a diagrammatic embodiment of a device according to the present invention, having a pyrolysis reactor 12, a burner 13 and a gasifier 14.
  • the biomass which is fed to the pyrolysis zone 12 via a feed 15 is converted into gaseous pyrolysis products, including tar-like materials, which, via a discharge 16, are guided to a feed 17 of the burner 13.
  • the gaseou.s pyrolysis products are burnt with air.
  • the heat QH produced is transferred to the gasifier 14, in which the st;eam and solid carbonization products introduced via feeds 10 and 20 are converted into product gas. Some of the heat OH generated in the burner 13 is transferred to the pyrolysis reactor 12.
  • the combustion gases are discharged from the burner 13 via a discharge 21, while the product gas is discharged from the gasifier via a discharge 22, to a downstream process stage, such as in order to supply liquid product.
  • the pyrolysis reactor 12 and the gasifier 14 may be designed as circulating fluidized beds which are known per se, while the burner 13 may be designed as a riser.
  • the pyrolysis reactor 12 may be connected to the gasifier 14 and the burner 13 via cyclones.
  • Fig. 3 shows a first embodiment of a device according to the present invention having a pyrolysis reactor 23, a gasifier 24 and a separate burner 25.
  • the pyrolysis reactor 23 comprises a first feed 26 for biomass, a second feed 27 for feeding bed material, and a third feed 28, along which some of the gaseous pyrolysis products are recirculated to the pyrolysis reactor 23. Recirculation of the gaseous pyrolysis products is used where the pyrolysis reactor is of the fluidized-bed type, in order to obtain fluidization.
  • the gaseous pyrolysis products may be condensed out, in which case, if desired, the gaseous or condensed fraction may be used for some other purpose. That fraction of the pyrolysis products which is used within the process is fed to the burner 25 via a feed 29.
  • the bed material and air are introduced into the burner 25 via feeds 30 and 31, for combustion of the gaseous pyrolysis products.
  • the off-gases are discharged from the burner 25 via discharge 32.
  • heated bed material is fed to the gasifier 24 via feed 33.
  • the hot outlet of the riser is also the highest point, so that i is possible to transport particles under the influence of the force of gravity.
  • the cold inlet is the lowest point, with the result that here too the particles flow from the gasifier to the riser under the influence of gravity.
  • a feed 35 steam is fed to the gasifier 24, and via a feed 36 bed material, containing the solid carbonization products, enters the gasifier 24.
  • the product gases leave the gasiJ i.er 24 via a product-gas discharge 37, while the cooled bed material is guided to the burner 25 via discharge 34.
  • hot bed material is guided from the burner 25 i.o the gasifier 24 and, after it has released heat in the gasifier, is guided to the pyrolysis reactor 23. It is also possible to guide sub-streams from the burner direct to the gasifier and the pyrolysis reactor, which may provide advantages in terms of control engineering. As a result of fluidization, the bed material is mixed with the solid carbonization products in the pyrolysis reactor 23, which are transferred from the pyrolysis reactor to the gasifier 24 via discharge 39.
  • An excess of gaseous pyrolysis products formed in the process may be discharged via a blow-off pipe 40.
  • FIG. 4 shows this with a diagrammatic, perspective illustration of an IFB reactor, which integrates the gasification and pyrolysis.
  • An IFB reactor in accordance with Fig. 4 comprises the compartments 40 and 41 of the pyrolysis reactor, as well as the compartments 42 and 43 of the gasifier, which are separated from one another, and a single, common heat- transferring wall.
  • a common partition 58 separates the compartments 40, 41 from the compartments 42 and 43. All the compartments 40-43 are surrounded by a common outer wall 57. Consequently, the total height of all the compartments is in principle equal.
  • the compartments 40, 41 are in communication with one another via a common free edge 59.
  • the compartments 42 and 43 are connected via a free edge 60.
  • the compartment 41 of the pyrolysis zone is in communication with the compartment 42 of the gasification zone via one or more openings in the partition 58, slightly above the gas- distribution plate of the fluid bed.
  • the action of the reactor shown in Fig. 4 may be presented as a system of four communicating vessels.
  • gas- fluidized solids systems it is possible to create density differences between two adjoining compartments by fluidizing each of the compartments with a different gas velocity.
  • particle transport takes place through the system of the four compartments, from the compartment 40 via the free edge 59, to the compartment 41, and, via the opening located on the underside, to the underside of the compartment 42. From the compartment 42, particle transport takes place via the free edge 60 and, from the underside of the compartment 43, via the openings 54 and 55, back to the compartment 40.
  • the IFB reactor is closed off by a cap 60 with a first compartment 61 which adjoins compartments 40, 41 and is separate from a second compartment 62 which adjoins the compartments 42, 43 of the gasification zone.
  • the cap 60 is provided with an intermediate wall 63 which adjoins the partition 58.
  • the burner in order to supply the heat for the endothermic reactions (pyrolysis and gasification) , may be located either outside the reactor, in a separate riser, as shown by the diagrammatic representation of Fig. 3, or inside the compartment 41 of the pyrolysis zone, as shown by the diagrammatic representation in Fig. 5.
  • the pyrolysis zone 41 and the gasification zone 43 are fluidized at a relatively low velocity, while the pyrolysis zone 40 and the gasification zone 42 are fluidized at a relatively high velocity, results in particle transport through the system in the direction of the first pyrolysis zone 40, towards the second gasification zone 43.
  • the primary function of the pyrolysis zone 41 and the gasification zone 43 is to transport particles, but they also form an additional reactor stage in the two-stage conversion, and considerable heat exchange takes place between the bed material and the solid pyrolysis products. Since the average residence time of the particles in the pyrolysis reactor 41 and in the gasifier 43 is generally short, the dimensions (i.e. the bed surface) are relatively small, so that only small quantities of gas are required for fluidization.
  • one of the compartments 41, 43 which are fluidized at a low velocity may be used for controlling the particle transport through the reactor. Fluidization of the pyrolysis reactor and/or gasification reactor can be increased by recirculation of the pyrolysis gases or the gasification product. The latter takes place together with the steam which has to be supplied m any case.
  • Fig 5 shows an interconnected fluid bed system ( IFB ) with two pyrolysis zones 40, 41 and two gasification zones 42, 43.
  • the biomass is introduced into the first pyrolys i s zone 1 via a first feed 44.
  • the gaseous pyrolysis products are guided out of the pyrolysis zones 40, 41 to an external b urner 46 via a discharge 45, and are partially recirculated to feeds 47 and 48.
  • the recirculated pyrolysis gas is burnt in an internal combustion zone 41 with the addition of air via feed 50.
  • V ia a feed 51, which is located in the vicinity of the underside of the gasifier 42, hot b ed material and solid carbonization products enter the first gasifier 42, inside which they are partially converted into product gas.
  • the remaining carbonization products enter the second gasification zone 43 at the top of the first gasification zone.
  • the product gas i s discharge d from the gasification zones 42 and 43 via a discharge 53.
  • the cooled bed material is returned to a feed 55 of the first pyrolysis zone 40 via a discharge 54.
  • Steam i s generated using the external burner 46 which, via a steam line 56, is connected to the first and second gasifiers 42, 43.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Coke Industry (AREA)

Abstract

L'invention concerne un procédé et un dispositif de formation de gaz de synthèse à partir de biomasse. Dans une zone de pyrolyse, la biomasse est convertie en un produit de carbonisation solide (charbon) et en produits de pyrolyse gazeux. Les produits de pyrolyse gazeux sont brûlés dans une zone de brûleur et fournissent la chaleur nécessaire au procédé de pyrolyse endothermique et au procédé de gazéification endothermique, pour la formation de gaz de synthèse. Les produits de carbonisation sont envoyés dans la zone de gazéification, de sorte qu'ils soient convertis, par exemple au moyen de vapeur, en H2 et CO. Le fait que les produits de pyrolyse gazeux et les effluents gazeux provenant de la zone de combustion soient séparés de la zone de gazéification, permet la production d'un gaz fini possédant une valeur calorifique élevée et sensiblement exempt d'azote. Le fait que les produits de carbonisation solides issus de la pyrolyse soient envoyés au gazéificateur, permet la production d'un gaz fini très pur et exempt des polluants qui se forment généralement lorsque des produits de pyrolyse gazeux sont convertis en gaz de synthèse. Le dispositif de l'invention peut ainsi être exploité sans que l'utilisation d'installations de purification complexes soit nécessaire.
PCT/NL1999/000481 1998-07-27 1999-07-27 Procede et dispositif pour la formation de gaz de synthese a partir de biomasse et de matieres residuelles Ceased WO2000006671A1 (fr)

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AU51992/99A AU5199299A (en) 1998-07-27 1999-07-27 Method and device for forming synthesis gas from biomass and residual materials
EP99937102A EP1114128A1 (fr) 1998-07-27 1999-07-27 Procede et dispositif pour la formation de gaz de synthese a partir de biomasse et de matieres residuelles
JP2000562455A JP2002521553A (ja) 1998-07-27 1999-07-27 バイオマスおよび残留物質から合成ガスを生成させるための方法および装置

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NL1009745A NL1009745C2 (nl) 1998-07-27 1998-07-27 Werkwijze en inrichting voor het vormen van synthesegas uit biomassa en reststoffen.
NL1009745 1998-07-27

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WO2001018151A1 (fr) * 1999-09-06 2001-03-15 Schenck Guenther O Procede d'accumulation d'energie solaire
EP1312662A3 (fr) * 2001-05-07 2003-09-24 Cirad-Foret Procédé de gazéification de biomasse, appareil et utilisation
EP1696177A1 (fr) * 2005-02-28 2006-08-30 Drechsler, Daniel Procédé intégré de gazification polycombustible
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser
CN100445351C (zh) * 2005-10-18 2008-12-24 中国石油大学(华东) 双上升管循环流化床煤气化装置
ES2327019A1 (es) * 2008-04-21 2009-10-22 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
EP1775336A3 (fr) * 2005-10-07 2010-01-06 Solenia S.A. Procédé et installation de transformation de matière organique en gaz et charbon
WO2010063207A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification à haute température avec de la biomasse et système correspondant
WO2010063206A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification de la biomasse à température élevée et son système
WO2010063205A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification à haute température avec de la biomasse et système correspondant
WO2009103529A3 (fr) * 2008-02-19 2010-09-02 Karl-Heinz Tetzlaff Procédé et dispositif pour utiliser des déchets afin de produire du gaz de synthèse
EP1940736A4 (fr) * 2005-10-21 2011-02-23 Taylor Biomass Energy Llc Procede et systeme de gazeification associee a une extraction de goudron in-situ
CN101157866B (zh) * 2007-11-08 2011-06-01 杨明得 大规模秸秆炭化生产方法及炭化窑
WO2011116690A1 (fr) * 2010-03-23 2011-09-29 武汉凯迪工程技术研究总院有限公司 Procédé et système pour produire du gaz de synthèse à partir de biomasse par carbonisation
WO2011159154A1 (fr) 2010-06-16 2011-12-22 Stichting Energieonderzoek Centrum Nederland Pyrolyse de lignine
WO2013091879A1 (fr) * 2011-12-20 2013-06-27 CCP Technology GmbH Procédé et installation de production de gaz de synthèse
CN103436279A (zh) * 2013-08-07 2013-12-11 何巨堂 一种碳料干馏过程和碳料气化过程的煤气串联使用工艺
CN103923705A (zh) * 2014-03-25 2014-07-16 东南大学 生物质气化制取富氢气体的装置及方法
WO2015078962A1 (fr) * 2013-11-28 2015-06-04 Ccp Technology Haut fourneau et son procédé de fonctionnement
CN104039689B (zh) * 2011-12-20 2016-11-30 Ccp技术有限公司 用于产生合成气体的过程和系统
US10023803B2 (en) 2012-11-09 2018-07-17 Valmet Technologies, Inc. Method for performing pyrolysis and a pyrolysis apparatus
WO2022019787A1 (fr) 2020-07-21 2022-01-27 Politechnika Gdanska Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone

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JP4965873B2 (ja) * 2006-03-10 2012-07-04 国立大学法人東京工業大学 木質バイオマスエネルギー転換方法及び転換システムに用いるエネルギーキャリアと転換材料
US10336579B2 (en) 2016-03-29 2019-07-02 Otis Elevator Company Metal coating of load bearing member for elevator system

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US4002438A (en) * 1975-01-22 1977-01-11 Joseph Fleming Organic conversion system
US4211606A (en) * 1975-08-19 1980-07-08 Chikul Olga S Method for thermal processing bitumen-containing materials and device for realization of same
WO1980002563A1 (fr) * 1979-05-22 1980-11-27 Lambiotte Usines Procede de gazeification complete de matieres carbonees
US4405339A (en) * 1980-08-07 1983-09-20 Mittetu Chemical Engineering, Ltd. Process and apparatus for gasifying combustible materials
US4397656A (en) * 1982-02-01 1983-08-09 Mobil Oil Corporation Process for the combined coking and gasification of coal
EP0219163A2 (fr) * 1985-10-09 1987-04-22 Shell Internationale Researchmaatschappij B.V. Procédé et appareil pour la production d'un gaz contenant de l'hydrogène
DE19618213A1 (de) * 1996-05-07 1997-11-13 Petersen Hugo Verfahrenstech Verfahren zur Erzeugung von Brenngas und Anlage zur Durchführung des Verfahrens

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001018151A1 (fr) * 1999-09-06 2001-03-15 Schenck Guenther O Procede d'accumulation d'energie solaire
EP1312662A3 (fr) * 2001-05-07 2003-09-24 Cirad-Foret Procédé de gazéification de biomasse, appareil et utilisation
EP1696177A1 (fr) * 2005-02-28 2006-08-30 Drechsler, Daniel Procédé intégré de gazification polycombustible
EP1775336A3 (fr) * 2005-10-07 2010-01-06 Solenia S.A. Procédé et installation de transformation de matière organique en gaz et charbon
CN100445351C (zh) * 2005-10-18 2008-12-24 中国石油大学(华东) 双上升管循环流化床煤气化装置
EP1940736A4 (fr) * 2005-10-21 2011-02-23 Taylor Biomass Energy Llc Procede et systeme de gazeification associee a une extraction de goudron in-situ
US8999019B2 (en) 2005-10-21 2015-04-07 Taylor Biomass Energy, Llc Process and system for gasification with in-situ tar removal
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser
CN101157866B (zh) * 2007-11-08 2011-06-01 杨明得 大规模秸秆炭化生产方法及炭化窑
WO2009103529A3 (fr) * 2008-02-19 2010-09-02 Karl-Heinz Tetzlaff Procédé et dispositif pour utiliser des déchets afin de produire du gaz de synthèse
ES2327019A1 (es) * 2008-04-21 2009-10-22 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
ES2327019B1 (es) * 2008-04-21 2010-08-10 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
WO2010063207A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification à haute température avec de la biomasse et système correspondant
WO2010063206A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification de la biomasse à température élevée et son système
WO2010063205A1 (fr) * 2008-12-01 2010-06-10 武汉凯迪科技发展研究院有限公司 Procédé de gazéification à haute température avec de la biomasse et système correspondant
RU2525491C2 (ru) * 2010-03-23 2014-08-20 Ухань Кайди Инджиниринг Текнолоджи Рисерч Инститьют Ко., Лтд. Способ и система получения синтез-газа из биомассы карбонизацией
WO2011116690A1 (fr) * 2010-03-23 2011-09-29 武汉凯迪工程技术研究总院有限公司 Procédé et système pour produire du gaz de synthèse à partir de biomasse par carbonisation
WO2011159154A1 (fr) 2010-06-16 2011-12-22 Stichting Energieonderzoek Centrum Nederland Pyrolyse de lignine
WO2013091879A1 (fr) * 2011-12-20 2013-06-27 CCP Technology GmbH Procédé et installation de production de gaz de synthèse
EA029582B1 (ru) * 2011-12-20 2018-04-30 Ссп Текнолоджи Гмбх Способ и система для генерирования синтез-газа
CN104039689A (zh) * 2011-12-20 2014-09-10 Ccp技术有限公司 用于产生合成气体的过程和系统
AP4015A (en) * 2011-12-20 2017-01-26 CCP Technology GmbH Method and plant for generating synthesis gas
CN104039689B (zh) * 2011-12-20 2016-11-30 Ccp技术有限公司 用于产生合成气体的过程和系统
AU2012359147B2 (en) * 2011-12-20 2015-07-23 CCP Technology GmbH Process and system for generating synthesis gas
US9309125B2 (en) 2011-12-20 2016-04-12 CCP Technology GmbH Process and system for generating synthesis gas
US10023803B2 (en) 2012-11-09 2018-07-17 Valmet Technologies, Inc. Method for performing pyrolysis and a pyrolysis apparatus
CN103436279A (zh) * 2013-08-07 2013-12-11 何巨堂 一种碳料干馏过程和碳料气化过程的煤气串联使用工艺
WO2015078962A1 (fr) * 2013-11-28 2015-06-04 Ccp Technology Haut fourneau et son procédé de fonctionnement
US10287643B2 (en) 2013-11-28 2019-05-14 CCP Technology GmbH Blast furnace and method for operating a blast furnace
CN103923705B (zh) * 2014-03-25 2016-01-06 东南大学 生物质气化制取富氢气体的装置及方法
CN103923705A (zh) * 2014-03-25 2014-07-16 东南大学 生物质气化制取富氢气体的装置及方法
WO2022019787A1 (fr) 2020-07-21 2022-01-27 Politechnika Gdanska Réacteur et procédé de pyrolyse de déchets industriels ou municipaux et de réduction et de purification de gaz de pyrolyse à partir d'hydrocarbures lourds et de particules de carbone

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JP2002521553A (ja) 2002-07-16
AU5199299A (en) 2000-02-21
NL1009745C2 (nl) 2000-01-28
EP1114128A1 (fr) 2001-07-11

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