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WO2003029389A1 - Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise - Google Patents

Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise Download PDF

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Publication number
WO2003029389A1
WO2003029389A1 PCT/FI2002/000775 FI0200775W WO03029389A1 WO 2003029389 A1 WO2003029389 A1 WO 2003029389A1 FI 0200775 W FI0200775 W FI 0200775W WO 03029389 A1 WO03029389 A1 WO 03029389A1
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Prior art keywords
reactor
bed
particles
fluidised
bubbling
Prior art date
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Ceased
Application number
PCT/FI2002/000775
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English (en)
Inventor
Esa Kurkela
Matti Nieminen
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VTT Technical Research Centre of Finland Ltd
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VTT Technical Research Centre of Finland Ltd
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Application filed by VTT Technical Research Centre of Finland Ltd filed Critical VTT Technical Research Centre of Finland Ltd
Priority to DE60221549T priority Critical patent/DE60221549T2/de
Priority to DK02764902T priority patent/DK1432779T3/da
Priority to JP2003532613A priority patent/JP4445261B2/ja
Priority to EP02764902A priority patent/EP1432779B1/fr
Publication of WO2003029389A1 publication Critical patent/WO2003029389A1/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
    • C10J3/46—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
    • C10J3/46—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
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—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

Definitions

  • Fuels suitable for gasification comprise finely divided biofuels and waste such as saw cuttings, municipal waste, packaging materials and plastic waste.
  • the product gas obtained can be utilised at power plants by substituting it to the plant fuel, such as charcoal, oil or natural gas.
  • the bubbling fluidised bed consisting of relatively coarsely divided fluidised particles remains in position supported by an ascending air flow blown into the reactor space.
  • the speed of the air flow is typi- cally of the order 1 m/s.
  • the solid matter concentration is low in a gas flow above a clearly limited bubbling fluidised bed.
  • the temperature of the reactor space above the fluidised bed in a bubbling fluidised bed reactor can be raised by additional air supply or dropped by injecting cooling water into the gas flow.
  • dust particles present in the gas flow can be separated with a distinct cyclone, in which the particles are returned to the bottom of the reactor space.
  • "Winkler gasifiers" of this type are described in DE patent specifications 195 48 324 and 27 51 911.
  • the second main type of fluidised bed reactors is a circulating fluidised bed, in which solid fluidised particles raise along with the air flow blown into the reactor.
  • the air flow speed which typically is of the order of 5 m/s, is higher and the size of the fluidised particles is smaller than those of a fluidised bed reactor.
  • the fluidised particles are entrained by the product gas into the cyclone, where the particles and the carbonisation residue derived from the fuel are separated and returned to the bottom of the reactor space.
  • circulating fluidised bed reactors have been given a height substantially higher than that of bubbling fluidised bed reactors.
  • Gasification of finely divided biomasses and plastic-containing waste performed with current methods and equipment involves the problem of the formation of tarlike compounds in abundance.
  • the product gas is filtered in order to remove ashes and heavy metals with filters having an operating temperature in the range from 200 to 450 °C.
  • the gas derived from the reactor at a temperature in the range from 800 to 100 °C needs to be cooled with a heat exchanger, and then tars are condensed on the surfaces of the gas ducts, the heat exchanger and the filter, which become clogged.
  • a second source of problems in current gasification processes is the chlorine contained in the fuel, such chlorine being abundantly present especially in plastic waste or similar waste fuels.
  • Chlorine reacts with calcium used as fluidised particles or entrained by the fuel, forming compounds, which also adhere to the gas ducts and heat exchangers and cause clogging of these. This process has been observed to reach a maximum when the cooling product gas is in the temperature range of approx. 720 to 780 °C.
  • the applicant's previous FI Patent Application 981817 describes a gasification method using a circulating fluidised bed reactor, in which the bed material consists of a mixture of hard and coarse material and readily ground and porous material.
  • the objective of this is to achieve a situation, where the tacky alkali metals in the ashes are bound to the finely divided calcium particles and rapidly pass through the circulation cyclone out of the gasifier.
  • the as- cending gas flow has a speed of 5 m/s, which is usual for a circulating fluidised bed gasifier, and the dust separated by the effective circulation cyclone is recirculated into the coarser sand bed at the bed bottom.
  • the purpose of the invention is to provide a solution to the problems explained above, which allows the problems of fouled and clogged gas ducts and heat ex- changers due to tars and/or calcium/chlorine compounds to be prevented or substantially relieved while the consumption of solid fluidised material remains moderate during the process.
  • the method of the invention is characterised by the fact that a bubbling fluidised bed containing coarser fluidised material particles is maintained in the reactor by means of a gas flow, and above this a circulating bed is maintained, which contains finer fluidised material particles, and that circulated particles separated from the product gas are returned to the top of the bubbling fluidised bed or above this in the reactor.
  • the central idea of the invention is to maintain a bubbling fluidised bed and a circulating bed in parallel in the process, with these beds operating substantially separately without intermixing. This achieves an optimal process, which combines the benefits of the two basic solutions: bubbling fluidised bed gasification and circulating fluidised bed gasification.
  • the bubbling fluidised bed at the reactor bottom of the invention requires a rela- tively low flow speed, and then an adequate retention time is achieved in a reactor that is substantially lower than current circulating fluidised bed reactors.
  • Fuel is gasified in the bubbling fluidised bed, from where the gas passes to the upper circulating bed, where circulating finely divided fluidised particles have a catalysing particle surface for tar degradation.
  • a low flow speed of the bubbling bed is sufficient, providing adequate retention time and decreasing disintegration and dust formation caused by particle collision.
  • Waste containing plastic and a number of biofuels are typically rich in evaporating substances and/or the carbonisation residue formed by these is extremely reactive. This is why fluidised bed gasification readily exceeds the required 95% carbon conversion, and hence it is not as crucial to separate cyclone dust with maximum precision and to return it to the fluidised bed as it is in the conventional Winkler gasifiers mentioned above.
  • the bub- bling fluidised bed may have a particle size e.g. in the range from 0.3 to 1.5 mm, and with the separation limit of the separator mentioned above, a fraction can be returned to the fluidised bed whose particle size is in the range from 50 to 300 ⁇ m.
  • Particles of the latter order of magnitude ascend in the gas flow, which has equal or lower speed than that of a bubbling bed, preferably e.g. in the range from 1 to 1.5 m/s.
  • the reactor space top containing the circulating bed can be given a larger width than that of the lower part containing the bubbling bed in such a way that the expansion will compensate the gas flow increase generated by gasification and prevent flow acceleration.
  • the fluidised material supplied to the reactor is a particulate inorganic substance, which may be inert or reactive, yet does not form combustive product gas as does fuel.
  • the reactor may be supplied with two different fluidised particle sizes so that coarser particles form a bubbling fluidised bed in the reactor and more finely divided particles form a circulating bed.
  • the fluidised material particles to be added which may consist of e.g. sand, will then preferably get into the variation range mentioned above between the bubbling bed and the circulating bed.
  • the feed material may consist exclusively of coarsely divided solid particles e.g. of the order of 0.3 to 1.5 mm, whose material is friable, so that the material, after it has been ground in the bubbling bed, joins the ascending air flow and thus forms fluidised material in the circulating bed.
  • a continuing solid matter fraction is further obtained from the finer fraction formed, passing from the separator to the product gas flow, and this fraction serves to prevent clogging of the gas ducts and the heat exchanger caused by tacky ashes.
  • Lime is a particularly suitable powderised fluidised material, however, magnesium oxide and kaolin are also usable.
  • the first one cooling the gas to the temperature range 600 to 720 °C and the second one further to a temperature of 450 °C or less.
  • the first heat exchanger passes the gas by the temperature range 720 to 780 °C, which is critical in terms of clogging, so that ash components containing calcium and chlorine loose their adhesiveness, thus eliminating the risk of clogging in the second heat exchanger operating at a lower temperature and the gas filter.
  • the first heat exchanger is preferably given wide dimensions so that its gas flow rate will be low, and the gas pipes may be disposed vertically, the risk of adhesion being thus minimised.
  • An additional measure for further avoiding clogging is to feed a sorbent, such as a suitable sodium, potassium or calcium compound into the product gas flow in or before the heat exchanger in order to bind ash particles.
  • a sorbent such as a suitable sodium, potassium or calcium compound
  • the gasification apparatus of the invention implementing the method described above comprises as elements known per se a fluidised bed reactor, fluidised material consisting of solid particles, a feed inlet for producing an ascending gas flow in the reactor, a fuel feed inlet, a feed inlet for introducing fluidised material into the reactor, a gas exhaust duct starting from the reactor top, a separator for separating solid matter particles from product gas that has left the reactor, and a return line for returning separated particles to the reactor.
  • the apparatus is characterised by the fact that a bubbling fluidised bed containing coarser fluidised material particles can be provided in the reactor and above this, a circulating bed containing finer fluidised material particles can be provided, so that the return line for particles returning from the separator to the reactor ends at the top level of the bubbling fluidised bed or above this.
  • the reactor space preferably comprises a lower part for the bubbling fluidised bed and an upper part wider in cross-section for the fluidised bed.
  • the ratio of the diameter of the upper part to that of the lower part is most appropriately in the range from 1.15 to 1.5.
  • the parts may be spaced by a conically expanding portion, whose conical angle to the vertical axis of the reactor space is obtuse, preferably less than 10 ° and most preferably less than 7 °. This expansion prevents the gas flow rate in a circulating bed from exceeding that of a bubbling bed.
  • the separator for separating solid particles returning to the reactor circulating bed from the finer particles remaining in the gas flow consists of a cyclone.
  • a wide cyclone dimensioned for a low flow speed preferably below 15 m/s can be used, caus- ing low loss of pressure, preferably less than 15 mbar. This facilitates the return of particles from the circulating bed to the reactor, and the product gas will retain solid particles that are able to sweep dust off the gas duct walls and to bind tacky adhesive ash components.
  • the gasification apparatus illustrated in the drawing comprises a fluidised bed reactor 1, which consists of a cylindrical lower part 2, an upper conically expanding part 3 and a cylindrical top part 4, the top part 4 having larger cross-sectional area than the lower part 2.
  • a grill 5 In the reactor 1, in the vicinity of its bottom, there is a grill 5, un- der which gasification air or vapour is fed from the feed inlet 6.
  • a stationary bubbling fluidised bed 7 In said lower reactor part 2, a stationary bubbling fluidised bed 7 is maintained supported by the ascending air flow, the fluidised bed consisting of solid, finely divided fluidised particles having a size above 0.2 mm, preferably in the range from about 0.3 to 1.5 mm.
  • the finely divided fuel to be gasified which may consist of biomass, such as saw cuttings or municipal or industrial waste, such as plastic waste, is fed through the inlet 8 to the reactor bottom part 2, into the fluidised bed 7.
  • the fuel is gasified in the bubbling fluidised bed 7, so that the formed gas passes into the ascending gas flow in the reactor space while ashes 9 are removed from the reactor bottom.
  • a circulating bed is maintained with the gas flow in the conically expanding part 3 of the fluidised bed reactor 1 and in the upper cylindrical part 4, the fluidised solid particles in this circulating bed being smaller than those of the lower bubbling fluidised bed 7, having preferably a size in the range of 50 to 300 ⁇ m.
  • the conical expansion 3 of the reactor space is preferably dimensioned with the increase of the cross-sectional surface of the space corresponding to the increase in gas amount caused by the fuel gasification, so that the speed of the ascending gas flow in the bubbling bed in the narrower lower part 2 of the reactor is the same as in the circulating fluidised bed in the upper part 4 of the reactor, of the order of 1 to 1.5 m/s.
  • the product gas flow is conducted from the top of the reactor space 1 through the duct 10 to the separating cyclone 11, which separates the fluidised particles from the circulating flow to be taken through the duct 12 back to the fluidised bed reactor 1.
  • the return duct 12 joins the reactor space at the level of the upper edge of the bubbling fluidised bed 7 as illustrated in the drawing.
  • the bubbling bed and the circulating bed will thus be separated from each other without intermixing of fluidised particles between the beds.
  • the height of the bubbling bed 7 may vary to some extent, in other words, the upper edge of the bed may momentarily rise slightly above the end of the return duct 12, or accordingly, drop slightly below this.
  • the drawing shows two feed inlets 13, 14 for fluidised particles to be introduced in the process, so that coarser particles of the bubbling bed 7 can be introduced in the fuel supply 8 and finer particles of the circulating bed can be introduced in the return inlet 12 of the circulating flow.
  • the particles to be introduced may be e.g. sand fractions, whose particle size is different in the bubbling bend and the circulating bed.
  • friable fluidised material such as lime can also be used, which, when comminuted in the bubbling bed 7, produces the more finely divided fluidised particles in the circulating bed. In that case, it may be enough if fluidised material is fed only to the bubbling bed 7 through the inlet 13.
  • the circulating bed can optionally be supplied with secondary air raising its temperature through inlet 15 or cooling water or vapour dropping its temperature through inlet 16, in the vicinity of the top part of the reactor space.
  • the cyclone 11 has the task of separating the fluidised particles of the circulating bed returning to the reactor 1 from the product gas flow, which is conducted through ducts 17, 18 to be cooled in two successive heat exchangers 19, 20.
  • the gas flow removed from the cyclone 11 to the duct 17 typically has a temperature of the order of 800 to 1000 °C, and it is cooled to the temperature range 600 to 720 °C with the first heat exchanger 19 in the flow direction.
  • the particle separating limit in the cyclone 11 being about 50 to 70 ⁇ m, solid particles of the size of 10-70 ⁇ m will remain in the product gas flow, and they will have en essential impact in binding ashes and preventing clogging.
  • a sorbent such as calcium, sodium or potassium compounds reacting with chlorine can be fed to the heat exchanger 19 through the inlet 21. If necessary, cooling water or vapour can also be fed in the gas flow of the heat exchanger 19.
  • the heat exchanger 19 acts simultaneously as a separator for removing fly ashes to the outlet 22.
  • the gas flow is cooled to a temperature of 450 °C or less.
  • the cooled product gas continues to the filter 23, whose operating temperature is in the range from 200 to 450 °C and from which the final, purified product gas is exhausted to the duct 24 and the separated finest dust fraction is removed to the discharge outlet 25.
  • the operability of the process of the invention was confirmed with an approx. 600 kW pilot equipment, which performed totally 460 hours of gasification tests on recycled fuel prepared from household refuse and on mixtures of recycled fuel and wood.
  • the pilot apparatus comprised all the essential components of the invention.
  • a solid fluidised bed consisting of coarse bed material was maintained at the bottom of the fluidised bed gasifier, and above this a circulating bed consisting of finer sand, lime and ash particles was maintained.
  • the product gas was conducted through a widely dimensioned cyclone, in which the gas in the inlet pipe had a flow rate less than 15 m/s, and the bed material separated by the cyclone returned through the return inlet the pipe located above the fluidised bed of the gasifier.
  • the pressure difference between the cyclone and the circulation line was low, less than 5 mbar, and the circulation acted reliably during the tests runs, and during the gasification tests, there were not even once any problems caused by clogging of the return duct for cyclone ashes, which is typical of conventional bubbling fluidised beds.
  • the product gas and the particles having typically a size of 0 to 70 ⁇ m entrained by the gas through the cyclone passed first through the first heat exchanger.
  • This heat exchanger contained vertical heat exchanger pipes, and the gas flowed from the top towards the bottom.
  • the gas was cooled to a temperature of approx. 550 °C in this heat exchanger, which had been correctly designed in terms of clogging prevention. Owing to the heat exchanger design, the suitable particle load of the product gas and the proper temperature level (below 600 °C), clogging of the gas line was completely avoided, which had caused problems in the tests the applicant had previously performed with conventional bubbling fluidised bed and circulating fluidised bed gasifiers.
  • the gas was cooled to the filter operating temperature in a conventional heat exchanger unit, which comprised horizontal heat exchanger piping.
  • finely divided calcium hydroxide was injected into the product gas before the filter in order to enhance chlorine retention that occurred with the aid of bed lime and alkali metals contained in the fuel.
  • the filter comprised fibre filters reinforced with ceramic, which resisted a temperature of about 500 °C.
  • the filter was used at a temperature of about 400 °C.
  • the recycled fuel of examples 1 to 2 represents recycled fuel substance of poor quality, which is derived exclusively from household refuse.
  • wood and packaging waste from stores and businesses are usually also available at gasification plants, this waste having better composition quality than household waste and being thus suitable for an advanced gasification process.
  • the implementation of the invention is not restricted to the ex- emplified fuels, but instead, the invention may utilise various waste and biofuels, which have the common features of a large amount of evaporating substances and the presence of a substance generating chlorine or other tacky deposits.
  • the pilot equipment was used for gasifying chopped recycled fuel prepared from household refuse, having a humidity of 26% and the following elemental composition of dry matter: C: 50.2%, H: 6.8%, N: 1.1%, S:0.2%, Cl: 0.70%, 0:26.2% and ashes 14.8%.
  • the fuel was disintegrated to a particle size under 20 mm.
  • the bed material in the gasifier consisted of a mixture of sand and limestone. No chlorine removing sorbent was injected into the product gas duct before the filter, the chlorine retention being based on the alkali metals of the fuel proper and bed calcium.
  • the particle size of sand was selected such that part of the sand remained in the lower bed and part was captured into the circulating flow above the bed.
  • Example 2 was conducted in the same way as example 1, except that the average humidity of the recycled fuel made from household refuse was 23% and the elementary composition of dry matters was as follows: C: 49.0%, H: 6.6%, N: 1.1%, S: 0.2%, Cl: 0.61%, O: 26.6% and ashes 15.9%.
  • the bed material in the gasifier consisted of the same mixture as in example 1.
  • chlorine removal sorbent was injected in the product gas duct before the filter. This gasifica- tion was also successfully conducted with good results, which appear from the following table. Carbon conversion exceeded 98%, the chlorine retention degree was 96.9% and the efficiency of separation of heavy metals exceeded 99%.
  • the pressure difference between the heat exchanger and the gas duct remained constant.
  • the gasifier was run over an overall period of about 80 hours.
  • the fuel consisted of a mixture of dry wood and recycled fuel prepared from household refuse, in which the proportion of wood was about 30% by weight and the proportion of recycled fuel was 70% by weight, the average humidity of the mixture was 19% and the elementary composition of dry matter was as follows: C: 49.4%, H: 6.5%, N: 0.8%, S: 0.1%, Cl: 0.57%, O: 31.9% and ashes 10.7%.
  • the bed material in the gasifier consisted of a mixture of sand and lime. No chlorine remov- ing sorbent was injected into the product gas duct.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Abstract

L'invention concerne un procédé et un appareil permettant de gazéifier du combustible dans un réacteur à lit fluidisé (1) contenant des particules de matériau solide fluidisées. Le combustible (8) est introduit dans la partie de fond du réacteur, et un gaz produit (10) formé par gazéification est amené du sommet du réacteur à un séparateur, tel qu'un cyclone (11), qui sépare les particules solides du gaz pour recirculation vers le réacteur. Selon cette invention, un lit fluidisé bouillonnant (2) contenant des particules grossières, et au-dessus de ce dernier, un lit circulant contenant des particules plus fines, sont maintenus dans le réacteur par recirculation des particules séparées du gaz produit vers le réacteur, vers le sommet du lit fluidisé bouillonnant ou au-dessus de celui-ci. Le réacteur peut comprendre une partie inférieure (2) pour le lit fluidisé bouillonnant, et une partie supérieure (4) dont la section transversale est plus grande pour le lit fluidisé circulant, la vitesse de l'écoulement gazeux ascendant dans le lit circulant étant égale ou inférieure à celle du lit bouillonnant. La limite de séparation dans le cyclone peut être ajustée de manière que l'écoulement de gaz produit libéré entraîne des particules solides, ce qui a un effet de liaison sur des particules de cendres collantes. Le gaz produit est refroidi dans deux échangeurs de chaleur successifs (19, 20) avant filtration du gaz. Ce procédé est adapté à la gazéification de biomasses et de combustibles recyclés formant des goudrons et/ou contenant du chlore, et constitue une solution aux problèmes des conduits de gaz encrassés ou colmatés.
PCT/FI2002/000775 2001-10-02 2002-10-01 Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise Ceased WO2003029389A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
DE60221549T DE60221549T2 (de) 2001-10-02 2002-10-01 Verfahren und vorrichtung zur vergasung von brennstoff in einem wirbelschichtreaktor
DK02764902T DK1432779T3 (da) 2001-10-02 2002-10-01 Fremgangsmåde og apparat til forgasning af brændstof i en fluid-bed-reaktor
JP2003532613A JP4445261B2 (ja) 2001-10-02 2002-10-01 流動床リアクターにおける燃料のガス化のための方法および装置
EP02764902A EP1432779B1 (fr) 2001-10-02 2002-10-01 Procede et appareil pour la gazification des combustibles dans un reacteur a lit fluidise

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI20011925A FI120770B (fi) 2001-10-02 2001-10-02 Menetelmä ja laitteisto polttoaineen kaasuttamiseksi leijukerrosreaktorissa
FI20011925 2001-10-02

Publications (1)

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WO2003029389A1 true WO2003029389A1 (fr) 2003-04-10

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PCT/FI2002/000775 Ceased WO2003029389A1 (fr) 2001-10-02 2002-10-01 Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise

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EP (1) EP1432779B1 (fr)
JP (1) JP4445261B2 (fr)
AT (1) ATE368719T1 (fr)
DE (1) DE60221549T2 (fr)
DK (1) DK1432779T3 (fr)
ES (1) ES2292803T3 (fr)
FI (1) FI120770B (fr)
PT (1) PT1432779E (fr)
WO (1) WO2003029389A1 (fr)

Cited By (12)

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GB2465055A (en) * 2008-11-07 2010-05-12 John William Carson Manufacturing cement by burning wood and grit aggregate
CN101245264B (zh) * 2008-03-25 2011-02-16 东南大学 单床自热式热解气化燃烧反应器及热解气化燃烧方法
ITMI20101244A1 (it) * 2010-07-06 2012-01-07 Eni Spa Procedimento per la produzione di gas di sintesi tramite un reattore di gassificazione a letto fluido alimentato con materiale carbonioso e dispositivo adatto allo scopo
WO2012059016A1 (fr) * 2010-11-01 2012-05-10 广州迪森热能技术股份有限公司 Procédé de gazéification de biomasse
WO2012150097A1 (fr) * 2011-05-04 2012-11-08 Outotec Oyj Procédé et plante pour la production et le traitement ultérieur d'un gaz combustible
WO2013041372A1 (fr) * 2011-09-19 2013-03-28 Thyssenkrupp Uhde Gmbh Procédé de fabrication de gaz de synthèse par gazéification d'une biomasse dans un lit fluidisé
EP2569078A4 (fr) * 2010-05-14 2015-02-11 Frontline Bioenergy Llc Appareil et procédé pour le contrôle optimisé des gaz acides et des métaux toxiques dans des gaz produits par un gazogène
EP2884170A1 (fr) * 2013-12-16 2015-06-17 Doosan Lentjes GmbH Appareil à lit fluidisé
WO2020012221A1 (fr) * 2018-07-11 2020-01-16 Arcelormittal Procédé de transfert de chaleur et dispositif associé
ES2915695A1 (es) * 2020-12-24 2022-06-24 Waste To Energy Advanced Solutions S L Instalacion y procedimiento de conversion termoquimica de un combustible solido en un gas de sintesis
SE2150187A1 (en) * 2021-02-23 2022-08-24 Phoenix Biopower Ip Services Ab An apparatus and a method for gasification of a solid fuel in a fluidized bed gasifier
WO2025168667A1 (fr) * 2024-02-06 2025-08-14 Borealis Gmbh Système de réacteur intégré et procédé de production simultanée d'un mélange d'hydrocarbures provenant d'une charge d'alimentation carbonée et d'une récupération de chaleur

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CN101294092B (zh) * 2007-04-25 2012-07-25 中国科学院过程工程研究所 固体燃料联合热转化方法及转化装置
DE102010006192A1 (de) 2010-01-29 2011-08-04 Uhde GmbH, 44141 Verfahren zur Biomasse-Vergasung in einer Wirbelschicht
CN102002399A (zh) * 2010-11-15 2011-04-06 国电长源电力股份有限公司 一种采用打包燃料的流化床气化反应方法及反应器
CN102784792B (zh) * 2012-07-28 2014-08-20 北京化工大学 多层鼓泡式城市生活垃圾分选装置及方法
ES2436844B1 (es) 2013-09-23 2014-07-07 Eqtec Iberia, S.L. Procedimiento para la gasificaci�n de materiales sólidos orgánicos y reactor empleado
CN104593088B (zh) * 2015-01-23 2018-05-25 新奥科技发展有限公司 一种煤气化反应装置及方法
JP6388555B2 (ja) * 2015-03-13 2018-09-12 三菱日立パワーシステムズ株式会社 バイオマスガス化システム及びこれを用いるボイラ設備
EP4209710A1 (fr) 2022-01-10 2023-07-12 ICMEA Srl leader of temporary association of companies ICMEA Srl - Tecnomec Engineering Srl - CNR IRSA Unité de lit fluidisé

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WO1999032583A1 (fr) * 1997-12-09 1999-07-01 Danish Fluid Bed Technology Aps Procede et appareil de gazeification de matieres carbonees solides

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US4852994A (en) * 1986-05-27 1989-08-01 Rheinische Braunkohlenwerke Ag Process for the production of gas containing hydrogen and carbon monoxide from solid fuel
US5562744A (en) * 1993-06-11 1996-10-08 Enviropower Oy Method for treating process gas
WO1999032583A1 (fr) * 1997-12-09 1999-07-01 Danish Fluid Bed Technology Aps Procede et appareil de gazeification de matieres carbonees solides

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101245264B (zh) * 2008-03-25 2011-02-16 东南大学 单床自热式热解气化燃烧反应器及热解气化燃烧方法
GB2465055A (en) * 2008-11-07 2010-05-12 John William Carson Manufacturing cement by burning wood and grit aggregate
GB2465055B (en) * 2008-11-07 2011-08-03 John William Carson Manufacturing cement using a wood burning fluid-bed furnace
EP2569078A4 (fr) * 2010-05-14 2015-02-11 Frontline Bioenergy Llc Appareil et procédé pour le contrôle optimisé des gaz acides et des métaux toxiques dans des gaz produits par un gazogène
WO2012004001A3 (fr) * 2010-07-06 2012-03-08 Eni S.P.A. Procédé pour la production de gaz de synthèse au moyen d'un réacteur de gazéification à lit fluidisé alimenté en matière carbonée et dispositif approprié à cette fin
ITMI20101244A1 (it) * 2010-07-06 2012-01-07 Eni Spa Procedimento per la produzione di gas di sintesi tramite un reattore di gassificazione a letto fluido alimentato con materiale carbonioso e dispositivo adatto allo scopo
WO2012059016A1 (fr) * 2010-11-01 2012-05-10 广州迪森热能技术股份有限公司 Procédé de gazéification de biomasse
WO2012150097A1 (fr) * 2011-05-04 2012-11-08 Outotec Oyj Procédé et plante pour la production et le traitement ultérieur d'un gaz combustible
WO2013041372A1 (fr) * 2011-09-19 2013-03-28 Thyssenkrupp Uhde Gmbh Procédé de fabrication de gaz de synthèse par gazéification d'une biomasse dans un lit fluidisé
RU2639911C2 (ru) * 2011-09-19 2017-12-25 Тюссенкрупп Индастриал Солюшнс Аг Способ и установка для производства синтез-газа посредством газификации биомассы в псевдоожиженном слое
EP2884170A1 (fr) * 2013-12-16 2015-06-17 Doosan Lentjes GmbH Appareil à lit fluidisé
WO2020012221A1 (fr) * 2018-07-11 2020-01-16 Arcelormittal Procédé de transfert de chaleur et dispositif associé
WO2020012378A3 (fr) * 2018-07-11 2020-03-19 Arcelormittal Procédé de transfert de chaleur et dispositif associé
ES2915695A1 (es) * 2020-12-24 2022-06-24 Waste To Energy Advanced Solutions S L Instalacion y procedimiento de conversion termoquimica de un combustible solido en un gas de sintesis
SE2150187A1 (en) * 2021-02-23 2022-08-24 Phoenix Biopower Ip Services Ab An apparatus and a method for gasification of a solid fuel in a fluidized bed gasifier
SE545010C2 (en) * 2021-02-23 2023-02-28 Phoenix Biopower Ip Services Ab An apparatus and a method for gasification of a solid fuel in a fluidized bed gasifier comprising means for re-introducing solid particles into a fluidized bed
WO2025168667A1 (fr) * 2024-02-06 2025-08-14 Borealis Gmbh Système de réacteur intégré et procédé de production simultanée d'un mélange d'hydrocarbures provenant d'une charge d'alimentation carbonée et d'une récupération de chaleur

Also Published As

Publication number Publication date
DK1432779T3 (da) 2007-12-10
ATE368719T1 (de) 2007-08-15
PT1432779E (pt) 2007-11-09
EP1432779A1 (fr) 2004-06-30
DE60221549D1 (de) 2007-09-13
JP2005504167A (ja) 2005-02-10
FI20011925L (fi) 2003-04-03
JP4445261B2 (ja) 2010-04-07
FI120770B (fi) 2010-02-26
ES2292803T3 (es) 2008-03-16
EP1432779B1 (fr) 2007-08-01
DE60221549T2 (de) 2008-04-24
FI20011925A0 (fi) 2001-10-02

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