WO2006043112A1 - Procede et installation permettant de traiter la biomasse - Google Patents

Procede et installation permettant de traiter la biomasse Download PDF

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Publication number
WO2006043112A1
WO2006043112A1 PCT/GB2005/050177 GB2005050177W WO2006043112A1 WO 2006043112 A1 WO2006043112 A1 WO 2006043112A1 GB 2005050177 W GB2005050177 W GB 2005050177W WO 2006043112 A1 WO2006043112 A1 WO 2006043112A1
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Prior art keywords
gasifier
stream
fischer
gas stream
gas
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PCT/GB2005/050177
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English (en)
Inventor
Michael Joseph Bowe
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Compactgtl Plc
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Publication of WO2006043112A1 publication Critical patent/WO2006043112A1/fr

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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
    • C10J3/46—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
    • C10J3/72—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
    • 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
    • C10J3/86—Other features combined with waste-heat boilers
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/023—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—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
    • C10J2300/0953—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
    • C10J2300/0959—Oxygen
    • 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
    • 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
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
    • 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
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • 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
    • C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
    • 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
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam

Definitions

  • the present invention relates to a process and a plant for treating biomass, in particular solid biomass materials, so as to enable a liquid hydrocarbon to be produced, and also to generate electricity.
  • biomass is suitable for use in the present invention, such as forestry waste, corn husks, wood chips, and products such as willow grown and coppiced for fuel. All such biomass contains complex organic compounds (such as lignin and cellulose in the case of such plant materials) , and can be provided in the form of solid particles, chips or pieces. Hitherto it has not been easy to obtain useful and valuable products economically from such sources of biomass.
  • a process for treating solid biomass comprising supplying the biomass in the form of solid pieces into a fluidised bed gasifier, while also generating a gas stream comprising hot steam, heating this gas stream to a temperature above 800 0 C, and feeding this gas stream at above 800 0 C into the gasifier to fluidise the bed of solid pieces and to produce a gas mixture including hydrogen and carbon monoxide, subjecting this gas mixture to Fischer-Tropsch synthesis, separating the output from the Fischer-Tropsch synthesis into a water stream, a liquid hydrocarbon stream and a gaseous output stream, and using the water stream to provide steam for the gas stream to be fed to the gasifier.
  • the gasification reaction between the complex organic compounds in the biomass and the steam generates a mixture primarily comprising carbon monoxide and hydrogen.
  • the gas stream contains only steam, the reaction is endothermic, but the thermal energy required for the reaction is provided by the very high temperature of the steam.
  • the gas stream also contains a small proportion of air, not more than 30% by mass and more preferably not more than 10% by mass, as this enables an exothermic oxidation reaction to occur, and so provides more energy for gasification.
  • the addition of air should be minimised, as it may lead to the production of carbon dioxide (which is undesirable) , and dilution of the gas stream with nitrogen.
  • the resulting gas mixture from the gasifier is cooled by passage through a heat exchanger, the heat being used to generate steam for the gas stream.
  • the steam is generated at high pressure and a temperature of above 25O 0 C, for example at 300 0 C, and this high-pressure steam can be passed through a turbine to generate electricity and to reduce its pressure to approximately atmospheric pressure for supplying to the fluidised bed gasifier.
  • the gas mixture is cooled to below 100 0 C, and then the remaining gases are compressed to above 17 atmospheres pressure, and subjected to Fischer-Tropsch synthesis.
  • the Fischer-Tropsch synthesis is performed in two successive stages, each stage being performed at an elevated temperature above 215 0 C and with a gas hourly space velocity greater than 10 000 hr "1 , so as to provide a conversion of carbon monoxide that is no greater than 60%.
  • the space velocity in this specification, is defined as the volume flow rate of the gases supplied to the reactor (measured at STP) , divided by the void volume of the reactor.
  • the Fischer-Tropsch synthesis is performed at a pressure in the range 17-21 atmospheres (this being the absolute pressure) .
  • the chain growth probability factor (Alpha) is only about 0.6 to 0.7. Consequently the hydrocarbons are primarily short chain; the selectivity to the production of C5+ hydrocarbons is less than 65% (the term C5+ referring to the hydrocarbons containing five or more carbon atoms) . Operation in this mode therefore generates a significant proportion of hydrocarbons that are gaseous under ambient conditions; but on the other hand it ensures that the proportion of waxy hydrocarbons (say above C17) is less than 1% of the product.
  • liquid hydrocarbons produced by condensing the products of the Fischer-Tropsch synthesis can be used directly as a vehicle fuel without requiring further chemical processing.
  • the operating temperature is higher than would conventionally be appropriate, and the reaction kinetics increase rapidly with temperature, so it is necessary to operate at a high space velocity to limit carbon monoxide conversion and restrict the production of water and the associated risk of damaging the catalyst.
  • the conversion of carbon monoxide to hydrocarbons may be in the range 40% to 60%. This ensures that the proportion of water vapour does not reach the levels at which hydrothermal ageing of the catalyst is likely. Somewhat greater carbon monoxide conversion overall can be obtained by condensing and separating the liquids formed by the Fischer-Tropsch synthesis, and then subjecting the remaining gases to a further Fischer- Tropsch synthesis at the same operating conditions. Condensing and removing the water in this way hence has the benefit of avoiding hydrothermal ageing of the catalyst. Hence operation in two successive stages provides efficient conversion of carbon monoxide, while ensuring the catalyst for the Fischer-Tropsch synthesis does not need frequent replacement.
  • the Fischer-Tropsch synthesis generates both short chain hydrocarbons, which may be referred to as "lights", and longer-chain higher molecular weight C5+ hydrocarbons which are a useful product and may for example be blended with conventional diesel fuel.
  • the gaseous output stream (which contains these lights) is used as the fuel to heat the gas stream for the gasifier.
  • this is done by catalytic combustion, as this avoids the presence of a flame front during combustion, thereby simplifying the heater, improving heat transfer and reducing the peak temperature.
  • any suspended ash particles may be removed using a cyclone separator and/or a filter, and tar and sulphur-containing compounds may be removed by passing over a tar-cracking catalyst and a desulphurising adsorber material, respectively.
  • Excess steam is preferably also removed at this stage, for example by cooling followed by a cyclone to remove water droplets. Partial water condensation can also be used to assist gas cleaning, as the droplets help remove ash particles.
  • the present invention also provides a plant for performing this process.
  • Figure 1 shows a flow diagram of a plant and process of the invention, showing the items of equipment forming the plant, and the connections between them.
  • a plant for treating wood waste chips or other solid particles of biomass includes a fluidised bed gasifier 10 into which the wood waste chips (or other solid biomass pieces) are fed through a loading chute 12.
  • a gas stream consisting primarily of steam, and also with about 8% (by mass) air, heated to 900 0 C, is also fed into the gasifier 10 through a duct 14, and provides the fluidising medium.
  • the gasifier 10 preferably also contains a bed of sand particles to provide thermal inertia and efficient mixing of the biomass particles, the particles of sand being sufficiently large not to be carried out of the gasifier 10.
  • the hot product gases emerge from an outlet duct 16 and are then passed through a cyclone 18 to separate and remove ash.
  • the gases are then passed over a tar cracking catalyst in a catalyst column 20.
  • the product gases are then passed through a heat exchanger 22 such as a shell and tube heat exchanger, used to generate steam at elevated pressure and a temperature of about 300 0 C.
  • the product gases are then passed through a desulphurising bed 24. They are then passed through a further heat exchanger 26 to cool them to about 5O 0 C, and then a further cyclone 27 to condense the excess steam.
  • This may alternatively be carried out in two stages, the first stage condensing part of the excess steam, the resulting water droplets scrubbing any remaining ash particles and then being removed by a first cyclone; the second stage condensing the bulk of the excess steam, the resulting water droplets being removed by a second cyclone.
  • the water from the second cyclone may be recycled as a source of water for generating the steam required for the gasifier 10.
  • the product gas stream emerging from the cyclone 27 consists predominantly of hydrogen and carbon monoxide, and may be referred to as synthesis gas.
  • This synthesis gas is then compressed in an electrically driven multi ⁇ stage compressor 28 to a pressure such as 18 atmospheres, and then supplied to a Fischer-Tropsch synthesis reactor 30.
  • a reactor suitable for the Fischer-Tropsch synthesis comprises a stack of plates defining coolant channels alternating with reaction channels, and with gas- permeable catalyst structures (such as corrugated foil, felt or mesh) in the reaction channels.
  • the plates may be flat, with channels defined by grooves; alternatively some of the plates may be corrugated so as to define channels.
  • the plates are bonded together typically by diffusion bonding or brazing, and are provided with suitable headers for the reactant gases and the coolant.
  • the reactor 30 consists of a stack of flat plates each 1 mm thick, separated by plates corrugated in the form of rectangular castellations to define reaction channels alternating with coolant channels.
  • the corrugated plates in the coolant channels are 0.3 mm thick and have 1.5 mm high castellations each of width 5 mm, while the corrugated plates in the reaction channels are 0.5 mm thick and have 6 mm high castellations each of width 25 mm.
  • the coolant channels are transverse to the direction of the reaction channels, so the coolant is crossflow relative to the reactants.
  • corrugated Fecralloy alloy foils 50 ⁇ m thick coated with a ceramic coating impregnated with a catalyst material are then be inserted into the reaction channels before the headers are attached, and can be replaced if the catalyst becomes spent.
  • a preferred catalyst comprises a coating of lanthanum-stabilised gamma-alumina of specific surface area 140 - 450 m 2 /g with about 10-40% (by weight compared to the weight of alumina) of cobalt, and with a ruthenium/platinum promoter, the promoter being between 0.01% to 10% of the weight of the cobalt.
  • a basicity promoter such as gadolinium oxide.
  • the activity and selectivity of the catalyst depends upon the degree of dispersion of cobalt metal upon the support, the optimum level of cobalt dispersion being typically in the range 0.1 to 0.2, so that between 10% and 20% of the cobalt metal atoms present are at a surface.
  • Cobalt particles of such a size provide a high level of catalytic activity, but may be oxidised in the presence of water vapour, and this leads to a dramatic reduction in their catalytic activity.
  • the extent of this oxidation depends upon the proportions of hydrogen and water vapour adjacent to the catalyst particles, and also their temperature, higher temperatures and higher proportions of water vapour both increasing the extent of oxidation.
  • the synthesis gas flows through the reactor 30 at an hourly space velocity in the range 10 000 to 20 000 hr "1 , and a temperature in the range 215-26O 0 C.
  • a single phase coolant fluid is employed to remove the exothermic heat to maintain the temperature in the Fischer-Tropsch reaction channels as close to isothermal as possible.
  • the coolant fluid is recirculated, its temperature being maintained at the required value by heat exchange with ambient air through a forced draft air cooler 32.
  • the reaction products from the Fischer-Tropsch synthesis are cooled to condense the liquids by passage through a heat exchanger 34 and a cyclone separator 36 followed by a separating chamber 38 in which the three phases water 39, hydrocarbons 40 and tail gases 42 separate, and the liquid hydrocarbon product 40 is stabilised at atmospheric pressure.
  • the hydrocarbon products produced by Fischer-Tropsch synthesis depend upon the chain growth probability factor (Alpha) ; the larger this probability factor, the higher the proportion of the product at longer chain lengths.
  • the reaction temperature and pressure lead to a comparatively low value of Alpha of about 0.6-0.7, so that the highest mass fractions are those of hydrocarbons that are gases under ambient conditions - methane, ethane, propane, butane - and which therefore emerge in the tail gases.
  • the mass fraction of long chain hydrocarbons above about C22 is negligible.
  • the product 40 does not contain significant amounts of waxy hydrocarbons.
  • the tail gases 42 contain not only the short-chain hydrocarbons, but also hydrogen, and (because of the comparatively low conversion of carbon monoxide) also contain a significant quantity of carbon monoxide. They can therefore be subjected to a second Fischer-Tropsch synthesis by passage through a second such reactor (not shown) , so that the overall carbon monoxide conversion is increased, and somewhat more of the desired product 40 is obtained.
  • hydrocarbons that remain in the gas phase and unreacted hydrogen and carbon monoxide are passed through a pressure reduction valve 44. They are then mixed with air and used as fuel for catalytic combustion (as described below) .
  • the water 39 is fed through the heat exchanger 22, to form high-pressure steam at about 300 0 C, as described above.
  • This high-pressure steam is passed through a steam turbine 46 used to generate electricity; this reduces the pressure down to about atmospheric pressure, so the steam can be fed to the gasifier 10. This electricity may be used to drive the compressor 28.
  • the low pressure steam, mixed with a small amount of air (as described above) is passed through a compact catalytic combustion heat exchange unit 48 (represented diagrammatically) , the steam passing through the heat exchange passages and so being heated up to the high- temperature (in the range 800° - 95O 0 C) to be supplied to the inlet duct 14.
  • This unit 48 may comprise a stack of plates defining alternate reaction channels and coolant channels, and with a catalyst structure in each reaction channel (similar to those described above as suitable for the Fischer-Tropsch reactor 30), but the catalyst structure incorporating a combustion catalyst, and the unit 48 being bonded together by diffusion bonding or brazing.
  • the plates may be made of a material such as Haynes HR-120 or Inconel 800HT (trade marks), iron/nickel/chromium alloys for high-temperature use, or similar materials. (Such materials may also be used for the gasifier 10, as this is at a similarly high temperature) .
  • the tail gases 42 mixed with air are passed through the catalytic combustion channels of the unit 48, where they undergo combustion to provide the necessary heat.
  • the dimensions and relative directions of the flow paths of the coolant (i.e. the steam) and combustion gases are such as to minimise the temperature difference between them, to ensure the combustion catalyst is not heated to excessive temperatures.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne de la biomasse solide telle que des copeaux de bois fournis à un gazogène (10) à lit fluidisé, tout en fournissant également un flux gazeux comprenant de la vapeur chauffée à plus de 800 °C dans un gazogène afin de fluidiser le lit de matériau solide. Le mélange de gaz chauds provenant du gazogène (10) peut être refroidi (22) afin de générer de la vapeur haute pression destinée à entraîner une turbine (46). Le mélange gazeux est, de préférence, refroidi à une température inférieure à 100 °C, compressé (28) à au moins 1.7 Mpa, puis soumis à une synthèse Fischer-Tropsch (30), ce qui génère un produit liquide (40) hydrocarboné et des gaz résiduaires (42). Le flux gazeux chaud destiné au gazogène (10) peut être fourni par soumission des gaz résiduaires (42) à une combustion dans un échangeur de chaleur (42) à réacteur catalytique compact. De ce fait, on utilise la biomasse pour produire de l'électricité et un hydrocarbure liquide pouvant être utilisé comme combustible.
PCT/GB2005/050177 2004-10-18 2005-10-10 Procede et installation permettant de traiter la biomasse WO2006043112A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB0423037A GB0423037D0 (en) 2004-10-18 2004-10-18 Process and plant for treating biomass
GB0423037.1 2004-10-18

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WO2006043112A1 true WO2006043112A1 (fr) 2006-04-27

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2910489A1 (fr) * 2006-12-22 2008-06-27 Inst Francais Du Petrole Procede de production d'un gaz de synthese purifie a partir de biomasse incluant une etape de purification en amont de l'oxydation partielle
DE102007050566A1 (de) 2007-10-23 2009-05-07 Stevanović, Dragan, Dr. Verfahren und Vorrichtung zur Vergasung von kohlenstoffhaltigen Rohstoffen
DE102008014297A1 (de) 2007-11-16 2009-05-20 Krones Ag Verfahren und Vorrichtung zur Umwandlung kohlenstoffhaltiger Rohstoffe
WO2009106357A2 (fr) * 2008-02-28 2009-09-03 Krones Ag Procédé et dispositif de transformation de matières brutes carbonées
WO2010049592A1 (fr) * 2008-10-31 2010-05-06 Upm-Kymmene Corporation Procédé et appareil pour la fabrication de biocarburant liquide à partir de biomasse solide
US20110065815A1 (en) * 2007-08-17 2011-03-17 Masayasu Sakai Method and apparatus for production of hydrocarbon from biomass
CN102261267A (zh) * 2010-05-25 2011-11-30 阳碁动力节能科技股份有限公司 电力供应系统和集合式住宅发电系统
WO2012095556A1 (fr) * 2011-01-14 2012-07-19 Vapo Oy Procédé d'utilisation de l'énergie thermique des gaz en produit dans une usine appartenant à la filière btl
US9434615B2 (en) 2007-07-20 2016-09-06 Upm-Kymmene Oyj Method and apparatus for producing liquid biofuel from solid biomass
GR1010414B (el) * 2021-08-02 2023-02-24 ΑΝΩΝΥΜΗ ΕΤΑΙΡΕΙΑ ΠΕΡΙΒΑΛΛΟΝΤΙΚΩΝ ΚΑΙ ΕΝΕΡΓΕΙΑΚΩΝ ΜΕΛΕΤΩΝ ΚΑΙ ΑΝΑΠΤΥΞΗΣ ΛΟΓΙΣΜΙΚΟΥ με δ.τ. ΕΜΙΣΙΑ Α.Ε., Συστημα παραγωγης καθαρου καυσιμου αεριου μικρης κλιμακας με χρηση αεριοποιησης ευελικτου καυσιμου

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WO2008093012A2 (fr) * 2006-12-22 2008-08-07 Ifp Procede de production d'un gaz de synthese purifie a partir de biomasse incluant une etape de purification en amont de l'oxydation partielle
WO2008093012A3 (fr) * 2006-12-22 2008-12-18 Inst Francais Du Petrole Procede de production d'un gaz de synthese purifie a partir de biomasse incluant une etape de purification en amont de l'oxydation partielle
FR2910489A1 (fr) * 2006-12-22 2008-06-27 Inst Francais Du Petrole Procede de production d'un gaz de synthese purifie a partir de biomasse incluant une etape de purification en amont de l'oxydation partielle
EP3135747A1 (fr) 2007-07-20 2017-03-01 UPM-Kymmene Oyj Procédé et appareil de production d'un produit hydrocarboné liquide à partir d'une biomasse solide
US9434615B2 (en) 2007-07-20 2016-09-06 Upm-Kymmene Oyj Method and apparatus for producing liquid biofuel from solid biomass
US20110065815A1 (en) * 2007-08-17 2011-03-17 Masayasu Sakai Method and apparatus for production of hydrocarbon from biomass
DE102007050566A1 (de) 2007-10-23 2009-05-07 Stevanović, Dragan, Dr. Verfahren und Vorrichtung zur Vergasung von kohlenstoffhaltigen Rohstoffen
DE102008014297A1 (de) 2007-11-16 2009-05-20 Krones Ag Verfahren und Vorrichtung zur Umwandlung kohlenstoffhaltiger Rohstoffe
AU2009218694B2 (en) * 2008-02-28 2014-02-13 Krones Ag Method and device for converting carbonaceous raw materials
CN101970617A (zh) * 2008-02-28 2011-02-09 克朗斯公司 用于转化碳质原材料的方法和设备
EA020334B1 (ru) * 2008-02-28 2014-10-30 Кронэс Аг Способ и устройство для конверсии углеродсодержащего сырья
WO2009106357A3 (fr) * 2008-02-28 2010-03-25 Krones Ag Procédé et dispositif de transformation de matières brutes carbonées
WO2009106357A2 (fr) * 2008-02-28 2009-09-03 Krones Ag Procédé et dispositif de transformation de matières brutes carbonées
CN102227487A (zh) * 2008-10-31 2011-10-26 芬欧汇川公司 由固体生物质生产液体生物燃料的方法和设备
RU2495908C2 (ru) * 2008-10-31 2013-10-20 Упм-Кюммене Корпорейшн Способ и устройство для производства жидкого биотоплива из твердой биомассы
WO2010049592A1 (fr) * 2008-10-31 2010-05-06 Upm-Kymmene Corporation Procédé et appareil pour la fabrication de biocarburant liquide à partir de biomasse solide
CN102261267A (zh) * 2010-05-25 2011-11-30 阳碁动力节能科技股份有限公司 电力供应系统和集合式住宅发电系统
WO2012095556A1 (fr) * 2011-01-14 2012-07-19 Vapo Oy Procédé d'utilisation de l'énergie thermique des gaz en produit dans une usine appartenant à la filière btl
US20130291808A1 (en) * 2011-01-14 2013-11-07 Vapo Oy Method for utilizing thermal energy of product gases in a btl plant
GR1010414B (el) * 2021-08-02 2023-02-24 ΑΝΩΝΥΜΗ ΕΤΑΙΡΕΙΑ ΠΕΡΙΒΑΛΛΟΝΤΙΚΩΝ ΚΑΙ ΕΝΕΡΓΕΙΑΚΩΝ ΜΕΛΕΤΩΝ ΚΑΙ ΑΝΑΠΤΥΞΗΣ ΛΟΓΙΣΜΙΚΟΥ με δ.τ. ΕΜΙΣΙΑ Α.Ε., Συστημα παραγωγης καθαρου καυσιμου αεριου μικρης κλιμακας με χρηση αεριοποιησης ευελικτου καυσιμου

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