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WO1997005216A1 - Ameliorations dans l'utilisation des combustibles houilleux - Google Patents

Ameliorations dans l'utilisation des combustibles houilleux Download PDF

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Publication number
WO1997005216A1
WO1997005216A1 PCT/AU1996/000483 AU9600483W WO9705216A1 WO 1997005216 A1 WO1997005216 A1 WO 1997005216A1 AU 9600483 W AU9600483 W AU 9600483W WO 9705216 A1 WO9705216 A1 WO 9705216A1
Authority
WO
WIPO (PCT)
Prior art keywords
coal
gasifier
slurry
ofthe
turbine
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/AU1996/000483
Other languages
English (en)
Inventor
Donald Ray Cummings
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Isentropic Systems Ltd
Original Assignee
Isentropic Systems Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Isentropic Systems Ltd filed Critical Isentropic Systems Ltd
Priority to AU66064/96A priority Critical patent/AU714670B2/en
Priority to US09/000,316 priority patent/US6141796A/en
Publication of WO1997005216A1 publication Critical patent/WO1997005216A1/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
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
    • F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
    • 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
    • C10J2300/093—Coal
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • 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
    • 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
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the fuel gas leaving the drier integrated with the gasification process is to be further adiabatically cooled by the injection of water and the saturated gas is then washed or treated by known means to remove particulates, and is then further cooled to reduce the water content of the gas such that it is increased in calorific value and can be used in known combustion systems.
  • Gas treatment at water saturation temperature can remove particulates and may also enable the removal of sulphur compounds by known means following that stage.
  • This final cooling has the inherent disadvantage of removing water vapour at combustion pressure which could be heated in the combustion stage and a significant part ofits inherent energy recovered in the expansion stage of the turbine. By condensing the water vapour this inherent energy is wasted and the cooling stage requires extra equipment and cooling media to remove the water vapour and a process plant to handle the resultant condensate.
  • the cooling ofthe gasifier exit gas by simultaneous drying ofthe coal feed puts additional water vapour into the fuel gas, and further adiabatic cooling by water addition and water washing for removal of solid particles and possibly sulphur compounds after the drying stage puts water vapour at combustion stage pressure (which could increase the mass flow to the combustion and final expansion stage thereby increasing the rated power output ofthe turbine system).
  • additional water content added by such cooling has the problem of making the gas unsuitable for combustion and for the achievement of high combustion temperatures such as in excess of 1,100°C and preferably above 1,200 °C.
  • the invention of this application is predicated upon our finding that, surprisingly, against all expectations, coal material with a substantial aqueous (water) content can be utilised as the basic starting material in the gasification of coal fiiel and the generation of power.
  • the invention in its broadest aspect, provides a process for the gasification of carbonaceous fuels, for, inter alia, the production of chemicals and/or the generation of power characterised in that there is employed, as starting material or part thereof, coal in the form of an aqueous slurry, the aqueous (water) content ofthe said slurry being at least 55% by weight.
  • the invention further provides a process a process for the gasification of carbonaceous fuels, for, inter alia, the production of chemicals and/or electrical energy characterised in that
  • coal in the form of an aqueous slurry having a water content of at least 55% by weight, is introduced, with hot gas produced in a coal gasifier stage, to a drying stage, (ii) the resultant slurry mixture is dried in the said drying stage by the adiabatic cooling ofthe hot gas and evaporation ofthe water, the thus dried coal and the cooled humidified gas being separated with return of the dried coal to the hot-gas producing gasifier stage, and
  • the cooled humidified gas is further cooled, cleaned and utilised in the production of chemicals and/or electrical energy.
  • the aqueous content ofthe slurry is at least 65% by weight, and optimally it is in the range 70-80% by weight.
  • the coal slurry may be composed in whole or in part of a slurry further comprising coal washery tailings residue.
  • the aqueous medium, for the coal slurry may be comprised, in whole or in part, of waste water, sewerage and the like.
  • the invention also provides apparatus for carrying out the above-defined process.
  • the apparatus comprises, in interconnected combination, a gasifier into which aquoues coal slurry is introduced, a flow drier/separator wherein materials exiting the gasifier are dried and separated into gaseous component and dried slurry material with feeding ofthe latter back to the gasifier, and a cooling/cleaning device into which the gaseous component from the separator passes and from which, when cleaned, it proceeds to a recuperator turbine/combustion arrangement for power generation.
  • the invention also provides apparatus, for use in carrying out the above defined process which comprises, in interconnected combination, a gasifier into which aqueous coal slurry is introduced, a flow drier/separator wherein materials exiting the gasifier are dried and separated into gaseous component and dried slurry material with feeding ofthe latter back to the gasifier, a cooling/cleaning device into which the gaseous component from the separator passes and from which, when cleaned, it proceeds for further processing, a gas turbine generation unit in turn comprised of a compressor, expansion stage, and generator, and, a combustor mechanism, the arrangement being such that combustion and process air passes from the turbine compressor in one stream to the gasifier and in another stream to the combustor, where the latter is combined with the gaseous component from the cooling/cleaning device, the combined gasses then being passed to the expansion stage ofthe gas turbine generation unit, and converted therein into electrical energy.
  • a gasifier into which aqueous coal slurry is introduced
  • the lignite/brown coal/high water content semi bituminous coal being fed to the drying stage ofthe process is fed by pumping, or other known means, as a slurry or paste of size reduced, but otherwise untreated "as mined" lignite or coal.
  • This feed material has a water content in the range 70-80% by weight of water.
  • Combustor system for the turbine comprises two combustion stages, the first stage being a combustor in which sufficient fuel gas is intimately mixed with the combustion air prior to the first stage of combustion to give a temperature in excess of 800°C and below 1,000°C at which temperature the mixture leaves the first stage.
  • the remaining part of the fuel (as required) is added under conditions which ensure maximum mixing and turbulence such that free radical induced rather than flame induced combustion is favoured.
  • An example of such a combustor is described in the specification of application PCT/AU95/00719 which is incorporated herein by reference.
  • the fiiel gas passing to the second stage of combustion is catalytically reacted (e.g. per medium of known sulphur tolerant shift catalysts) to convert at least part ofthe carbon monoxide and water vapour in the gas stream to hydrogen and carbon dioxide before passing to the said second combustion stage.
  • This further increases its temperature and hydrogen content to ease its combustion in lean phase mix with combustion gases by means of free radicle-induced combustion.
  • the gases leaving the coal gasification stage are used to dry the coal (lignite) water slurry and the gases are then further cooled by evaporative cooling by further water addition, water washing being thereby used to remove solid particles from the gas (by known means such as venturi scrubbers, water sprays, coalescers, demisters, electrostatic precipitators). Thereafter the gases can be preheated by heat exchange with exhaust gases leaving the expansion stage of the gas turbine before being used as fuel gas in the turbine's combustion system.
  • Salts may be removed by solution in the wash water and fuel and ash components may be separated by known means. Unused fiiel may be recovered as a water / fuel slurry and recycled with the incoming fiiel / water slurry feed.
  • the water content in the coal may be due in whole or in part to the addition of wastes such as sewerage waste or other suitable wastes requiring disposal which may be added together with the coal or lignite fuel.
  • the process of this invention is also suitable for the use of lignite / water slurries where the lignite has been pre-treated by the Hydro Thermal Dewatering process (known as the HTD process).
  • HTD process Hydro Thermal Dewatering process
  • an integrated drying and gasification process producing power in accordance with this invention can dry a feed coal and water slurry in excess of that required for power generation and can produce a side-stream of dried coal for oxygen-based gasifiers producing synthesis gas for coal processing plant such as hydrogenation to produce liquid fuels or other uses such as a low moisture high quality briquette fuel.
  • the pressure ofthe air passing to the gasifier may be no more than 4.0 bar and possibly less than 2 bar above the pressure ofthe air passing to the combustor.
  • figure 1 depicts, schematically, a preferred embodiment ofthe invention.
  • the apparatus ofthe invention which is used in the performance ofthe process ofthe invention is illustrated.
  • the aqueous coal slurry is an aqueous slurry of lignite, lignite being a well-known brown coal with a carbon content within the range 25-45%.
  • lignite being a well-known brown coal with a carbon content within the range 25-45%.
  • the lignite slurry is discussed further below. It is re-emphasised that the figure is a schematic illustration and is to be understood as such.
  • item 2 is an air blown pressurised lignite gasifier (such as a Winkler gasification device) and item 4 is an outlet duct of the gasifier to which additional air or oxygen may be optionally added via pipeline 132.
  • Items 6, 8 and 10 are components of an entrained flow drier of known construction in which 6 is an entrainment mixing vessel in which fluidisation and conveying of lignite is initiated, 8 is an entrainment flow drying tube or tubes, and 10 is a separator or separators such as a cyclone separator or separators.
  • Item 12 denotes a dried lignite feeding device which may be a screw conveyor, lock hopper mechamsm, injector or any combination of such known devices, which can inject dried lignite into the gasifier which is at a higher pressure than the lignite recovered from separator 10.
  • a dried lignite feeding device which may be a screw conveyor, lock hopper mechamsm, injector or any combination of such known devices, which can inject dried lignite into the gasifier which is at a higher pressure than the lignite recovered from separator 10.
  • Item 14 is an adiabatic cooling device such as a venturi scrubber, which is capable of cooling hot and dust laden gases to their dew point, coagulating mist particles and wetting dust particles in the gas stream.
  • Item 16 is a separator, such as a cyclone separator and mist elimination system or electrostatic precipitator or the like, which may incorporate water spraying or partial condensation to provide a clean water wash capable of removing substantially all of the dust particles and soluble salts as a solution or slurry which is separated from the gas stream within separator 16 and removed via pipeline 146.
  • the apparatus also comprises a recuperated turbine and combustion system which will now be described.
  • Items 18, 20, 22, 24 and 26 depict a gas turbine power generation unit in which 18 is the air compression stage, 22 is the expansion stage, 26 is the generator and 20 and 24 are respective connecting shafts between 18 and 22 and 22 and 26.
  • the expansion stage, 22 may be a split or single shaft unit.
  • Items 28 and 32 are sets of recuperators.
  • item 34 is a first stage combustion vessel (combustor), which may be of the type described in the copending application referred to above.
  • Item 36 is an interconnecting duct and item 38 is a second stage combustion vessel (combustor) in which combustion is achieved as described hereafter.
  • the gas turbine may have a compression ratio less than 35/1, for example below 17/1, and may be as low a 4/1.
  • Item 40 is a catalytic system incorporating known (e.g. sulphur tolerant) shift catalysts mounted in a vessel such that part ofthe carbon monoxide in the gas stream entering the vessel reacts with the water vapour in the gas stream to form additional hydrogen and carbon dioxide.
  • known e.g. sulphur tolerant
  • Hot gases typically at between 900°C and 1,000°C pass from the gasifier 2 to duct 4. As indicated above, additional air and or oxygen may be added to raise the exit gas temperature via pipeline 132.
  • the hot gases leaving the gasifier in duct 4 enter mixing vessel 6 and slurried lignite is added via pipeline 102.
  • the lignite slurry in this case is "as mined" lignite reduced in size to particles of dimensions less than 10 mm and suspended in water as a dense slurry or paste having a dry lignite content of about 25% by weight on an "as fed wet" slurry basis.
  • the drying lignite and mixed hot gases and water vapour enter 10 in which the greater part of the dried lignite is removed and pass to feeding device 12 in which the lignite is conveyed at a controlled rate and increased in pressure such that lignite passes to the gasifier, 2.
  • Part of the steam shown as entering the gasifier may be used to assist in the conveyance and dispersion ofthe lignite from device 12 to gasifier 2.
  • Gas from the combined gasification and drying stages leave separator 10 via pipeline or duct 104 and enter cooling device 14 in which water is added via pipeline 106 to cool and saturate the gases to or slightly below their adiabatic dew point.
  • the excess water plus dissolved and suspended salts and ash from the lignite plus unburnt or partially burnt lignite are removed via pipeline 146.
  • the material leaving via the pipeline may be treated by known means to extract ash and to remove and recycle the unburnt and partially burnt lignite. All or part ofthe lignite may be utilised in the production ofthe aqueous slurry introduced via pipeline 102. Remaining salts and water may be treated in orthodox fashion.
  • the cleaned fuel gases which also contain a substantial amount of water vapour and inert gases such as nitrogen and carbon dioxide, leave cooling device 14 via pipeline 108 and pass to the recuperator 32 in which the gas is preheated for passage to and use as fuel in the above ⁇ mentioned gas turbine combustor system (34, 36 and 38, 18, 20, 22, 24,26).
  • Combustion and process air for the gas turbine system enters the system via duct 118 and is compressed in compressor 18 such that compressed combustion air is withdrawn via pipeline 120 and preheated in recuperators 28 and 32 and then passes via duct 122 to the first stage combustor 34.
  • Some air at a higher pressure than in pipeline 120 is withdrawn via pipeline 124 and passes via this pipeline to the gasifier in which the air is injected into the gasifier via pipelines 128, 130 and (abovementioned) 132.
  • Air stream 124 may be recuperated prior to passage to the gasifier via a recuperator in parallel with recuperators 28/32 so as to increase gasification temperature.
  • total gasifier temperature may be raised, or alternatively, part of the air is pre-heated and used to partially fuse and agglomerate coal in a fluid bed gasifier.
  • the combustor 34 is operated so as to use all or the greater part of the air preheated in recuperators 28 and 32 and entering the combustor via pipeline 122, and part ofthe preheated fuel gas from recuperators 28 and 32 entering the combustor via pipeline 110 and 112.
  • the combustion products are then transported to combustor 38 via duct 36 at typically between 850°C and 1,000°C.
  • the remainder of the fuel passes from pipeline 110 to pipeline 114 and enters catalytic system 40 in which part of the carbon monoxide in the gas is converted by reaction with water vapour in the gas by known catalysts into additional hydrogen with an increase in temperature due to the exothermic nature ofthe reaction.
  • the hydrogen enriched gas then passes via pipeline 116 to the second stage combustor 38.
  • the resultant combustion gases leaving combustor 38 are at a temperature in excess of 1,000°C and preferably above 1,200°C before entering the expansion stage 22 ofthe turbine via 136. Net surplus power produced in the expansion turbine 22 passes via shaft 24 to generator 26 in which it is converted predominantly into electrical energy.
  • the first combustor may be fired with fuel oil (diesel) for start up purposes.
  • the aqueous lignite slurry is fed into the outlet duct ofthe gasifier and steam, air, enriched air or oxygen are fed into the gasifier.
  • hot gases typically at a temperature in the range 900 to 1,000°C, leave the gasifier, then traverse the duct through which the slurried lignite enters.
  • the mixture of gases, slurried lignite and drying lignite proceed via the entrained flow dryer sequentially comprised ofthe entrainment mixing vessel, the flow drying tube and the cyclone separator.
  • the components enter the separator wherein the greater part ofthe dried lignite is recovered and passes to the screw conveyor or other feeding device for feeding into the gasifier.
  • Gas leaving the cyclone separator passes via a pipeline to the adiabatic cooling device (venturi scrubber) to which water is added via a pipeline to cool and saturate the gases to or slightly below their adiabatic dew point.
  • the adiabatic cooling device venturi scrubber
  • excess water, plus dissolved and suspended salts and ash from the lignite, plus any unburnt or partially burnt lignite are removed via the exit pipeline.
  • the fuel gases which have been cleaned by the water from the pipeline entering the venturi scrubber, and which also contain water vapour plus nitrogen and carbon dioxide, leave the scrubber via a pipeline and pass to the recuperators.
  • the gas is preheated for use as fuel in the associated gas turbine system which is comprised ofthe air compressor, expansion stage, generator and respective connecting shafts.
  • first stage combustion vessel Further associated with the gas turbine system and the recuperators are a first stage combustion vessel and a second stage combustion vessel.
  • the vessels are interconnected by a duct.
  • combustion is achieved by the rapid and intimate mixing ofthe remaining fuel gas with the hot gases from the recuperators such that predominantly free radical rather than flame initiated combustion takes place.
  • Combustion and process air for the gas turbine system, enters the air compressor via an entrance duct and compressed air exits via two pipelines.
  • the exiting air in one pipeline at a lower pressure than the air in the other pipeline, travels to the recuperators and thence to the first combustor.
  • the higher pressure air passes to the gasifier via the appropriate pipelines.
  • the first combustion vessel is also fed with portion of the abovementioned cleaned preheated fuel gas which has travelled from the venturi scrubber.
  • the combined combustion products from the first combustion vessel are transported to the second vessel via the connecting duct at a temperature typically within the range 850 to 1,100°C.
  • the remainder of the cleaned fuel gas from the scrubber enters a sulphur tolerant catalytic system wherein there is a reaction between the incipient carbon monoxide and water vapour to form additional hydrogen and some carbon dioxide.
  • the thus hydrogen-enhanced gas then passes, via pipeline, to the second combustor vessel.
  • This second vessel thus contains air and gas from the first combustion vessel and further fuel gas from the gasifier and flow drier (via the scrubber).
  • the combustion gases leaving the second combustion vessel are at a temperature in excess of 1, 100°C whereupon they enter the expansion stage of the turbine system. Power produced therein passes to the generator wherein it is converted into electrical energy.
  • the streams of air exiting the compressor are respectively at 8 and 10 atmospheres .
  • a slagging gasifier using oxygen instead of air for the partial oxidation/ gasification ofthe coal is used, in this case air compressed by the turbines air compression stage is withdrawn at the compressor exit with part ofthe air being used as feed to the combustor and the remainder being feed an air separation unit.
  • the turbine At sea level and at 15oC the turbine is capable of producing 27.2 MW when integrated with coal gasification, coal slurry feed, drying and fuel gas treatment system having the following characteristics.
  • the pre-heated fuel gas and air are mixed in parallel venturi mixers immediately beneath the lower tube sheet of two combustors each containing 3,000 2 metre long 25 mm outside diameter silicon carbide tubes arranged generally in accordance with co-pending patent PCT AU95/07719. In this case no secondary combustion stage is used.
  • the net production of power from the integrated slurry drying and gasification gas turbine system is 27.2 MW

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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)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention concerne un procédé de gazéification des combustibles houilleux, pour, entre autres, la fabrication de produits chimiques et/ou la production d'électricité, caractérisé par le fait que le matériau de départ est partiellement ou totalement du charbon sous forme de schlamm, la teneur en eau dudit schlamm étant au moins de 55 à 80 % en poids. L'invention concerne également un dispositif destiné au brûlage de combustibles carbonés pour la production d'énergie électrique. Ce dispositif comprend, assemblés et reliés, un gazéificateur dans lequel est introduit le schlamm; un sécheur/séparateur de flux où les matériaux sortant du gazéificateur sont séchés et séparés en composant gazeux et schlamm séché, lequel est renvoyé dans le gazéificateur; un dispositif de refroidissement/nettoyage dans lequel passe le composant gazeux venant du séparateur et d'où, une fois nettoyé, il continue en vue d'un traitement ultérieur; une unité génératrice de turbine à gaz qui comprend un compresseur, un étage de détente et un générateur; et un mécanisme de combustion. La disposition est telle que l'air de combustion et de traitement venant du compresseur de la turbine se dirige en un premier flux vers le gazéificateur et en un second flux vers le brûleur, au niveau duquel le second flux est combiné au composant gazeux venant du dispositif de refroidissement/nettoyage. Les gaz combinés passent ensuite à l'étage de détente de l'unité génératrice de turbine à gaz, où ils sont convertis en énergie électrique.
PCT/AU1996/000483 1995-08-01 1996-08-01 Ameliorations dans l'utilisation des combustibles houilleux Ceased WO1997005216A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU66064/96A AU714670B2 (en) 1995-08-01 1996-08-01 Improvements in the use of carbonaceous fuels
US09/000,316 US6141796A (en) 1996-08-01 1996-08-01 Use of carbonaceous fuels

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPN4517A AUPN451795A0 (en) 1995-08-01 1995-08-01 Improvements in the use of carbonaceous fuels
AUPN4517 1995-08-01

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US6361682B1 (en) 2000-03-16 2002-03-26 Kellogg Brown & Root, Inc. Pelletization of petroleum resids
WO2001083644A3 (fr) * 2000-04-28 2002-05-30 Texaco Development Corp Utilisation des eaux usees de fischer-tropsch
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CN102373096A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373099A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373090A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373098A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373092A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373091A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN112780411A (zh) * 2019-11-06 2021-05-11 中国航发商用航空发动机有限责任公司 燃气轮机水汽混合动力系统、水汽发生组件、航空器及动力提供方法

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6499979B2 (en) 1999-11-23 2002-12-31 Kellogg Brown & Root, Inc. Prilling head assembly for pelletizer vessel
US6361682B1 (en) 2000-03-16 2002-03-26 Kellogg Brown & Root, Inc. Pelletization of petroleum resids
WO2001083644A3 (fr) * 2000-04-28 2002-05-30 Texaco Development Corp Utilisation des eaux usees de fischer-tropsch
US6533945B2 (en) 2000-04-28 2003-03-18 Texaco Inc. Fischer-Tropsch wastewater utilization
CN102373090A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373099A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373096A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373098A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373092A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373091A (zh) * 2010-08-20 2012-03-14 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373092B (zh) * 2010-08-20 2013-10-16 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN102373090B (zh) * 2010-08-20 2013-10-16 新奥科技发展有限公司 煤气化工艺与蒸汽透平发电工艺的耦合方法
CN112780411A (zh) * 2019-11-06 2021-05-11 中国航发商用航空发动机有限责任公司 燃气轮机水汽混合动力系统、水汽发生组件、航空器及动力提供方法

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