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WO1999037739A1 - Procede de traitement de combustibles condenses par gazeification - Google Patents

Procede de traitement de combustibles condenses par gazeification Download PDF

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Publication number
WO1999037739A1
WO1999037739A1 PCT/FI1999/000044 FI9900044W WO9937739A1 WO 1999037739 A1 WO1999037739 A1 WO 1999037739A1 FI 9900044 W FI9900044 W FI 9900044W WO 9937739 A1 WO9937739 A1 WO 9937739A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasifying agent
gas
reactor
smoke
smoke gas
Prior art date
Application number
PCT/FI1999/000044
Other languages
English (en)
Inventor
Georgi B. Manelis
Victor P. Foursov
Evgueni V. Poliantchik
Original Assignee
Fioter Oy
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 Fioter Oy filed Critical Fioter Oy
Priority to CA002318971A priority Critical patent/CA2318971A1/fr
Priority to JP2000528647A priority patent/JP2002501112A/ja
Priority to EP99901608A priority patent/EP1049755A1/fr
Priority to AU21660/99A priority patent/AU738097B2/en
Publication of WO1999037739A1 publication Critical patent/WO1999037739A1/fr

Links

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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • 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
    • C10J2300/0983—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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • Y02E20/12—Heat utilisation in combustion or incineration of waste

Definitions

  • This invention pertains to methods for processing various condensed fuels, primarily highly humid ones, such as solid municipal waste, biomass wastes, sludges and slurries, coal by means of pyrolysis and gasification of their organic part so as to produce hydrocarbon products of pyrolysis and fuel gas, which are used for energy generation.
  • the method can be used for environmentally friendly and energy efficient processing/disposal of poorly combustible wastes .
  • the gasifying agent containing oxygen and possibly water and/or carbon dioxide enters the combustion zone wherein oxygen reacts at 900—1500°C with the carbon of solid fuel in the form of char.
  • the gasifying agent is fed to the reactor countercurrently to the fuel so that the oxidant gas at least partially is passed through a layer of solid combustion products (ashes) that already do not contain carbon.
  • solid combustion products cool down and the gasifying agent, correspondingly, heats before it enters the combustion zone.
  • the oxygen of the gasifying agent is totally consumed and hot gaseous combustion products, including carbon dioxide and water, enter the next zone of the charge, which is called reduction zone, where carbon dioxide and steam react with the carbon of fuel yielding combustible gases.
  • the sensible heat of the gases heated in the combustion zone is partially consumed in these reduction reactions.
  • the temperature of the gas flow drops as the gas filters through the fuel and lends to the latter its sensible heat.
  • the fuel heated in oxygen-free environment is pyrolyzed yielding char, pyrolysis tars, and combustible gases.
  • the product gas is passed through fresh fuel so as to cool down the gas while fuel is heated and dried. Finally, the product gas (containing steam, hydrocarbon vapors, and tars) is withdrawn for further use.
  • a method described in patent RU-2079051 proposes gasification of solid municipal waste in a countercurrent of a gasifying agent containing oxygen and also water and/or carbon dioxide.
  • the maximum temperature in the combustion zone i.e., maximum temperature in the reactor
  • the maximum temperature in the combustion zone is controlled within 700 to 1400°C (preferably 1000 to 1200°C) while the temperature of the product gas at the reactor outlet is maintained below 400°C (preferably under 250°C) .
  • A is maintained within 0.15 ⁇ A ⁇ 1.0.
  • Analogous countercurrent scheme is also applicable to processing hydrocarbons (e.g., oil slurries) as disclosed in patent application RU- 96/119443 (Manelis et al . ) provided that slurries are charged together with a solid incombustible material.
  • hydrocarbons e.g., oil slurries
  • RU- 96/119443 Manelis et al .
  • introduction of water (carbon dioxide) in the gasifying agent provides means to enhance content of hydrogen (carbon monoxide) in the product gas and to reduce the temperature in the combustion zone.
  • supply of steam necessitates introduction of additional equipment in the installation.
  • a general drawback of the aforementioned methods when applied to gasification of humid fuel is unavoidable addition of steam to the product gas.
  • the latter is diluted with steam, which further increases heat losses with the smoke gas and reduces energy efficiency of the boiler and of the process in general .
  • the objective of this invention is to perform pyrolysis and gasification of condensed fuels without external heat supply, with high energy efficiency and high yield of valuable products, (pyrolysis tars and combustible gases) .
  • This invention provides a method for processing condensed combustibles that includes : charging in the reactor a mixture that possibly contains pieces of solid incombustible material and at least partially consists of combustible components so as to pyrolyze and gasify the latter;
  • the gasifying agent or its constituents can be supplied in one stream or in distributed mode.
  • air and smoke gases can be supplied via their own separate inlets.
  • the mixture charged enters the preheating zone wherein it heats to 300°C owing to heat exchange with the combustible product gas.
  • the product gas is withdrawn from the preheating zone.
  • product gas refers to aerosol comprising pyrolysis tars as vapors and fine droplets and generator gas incorporating carbon monoxide and dioxide, steam, hydrogen, methane, ethylene, propane, and other gases.
  • the charge enters the pyrolysis zone, where it heats to 300 - 500°C due to heat exchange with gas flow and combustible materials pyrolyze emitting volatiles to the gas and forming carbonaceous residue.
  • the mixture containing pyrolyzed waste enters the coking zone where coke is formed from the organic matter of waste at 500 - 800°C.
  • the mixture containing coked combustibles enters the gasification (combustion) zone where preheated gasifying agent reacts with the coke at 800 - 1300°C to yield combustible gas and solid residue of combustion.
  • the solid residue enters the cooling zone where owing to heat exchange of the solid residue with countercurrently supplied gasifying agent the latter is preheated.
  • the above classification of the zones is in part arbitrary, they might be defined alternatively, say according to gas temperature or composition and state of the reactants. However, for any notation chosen the distinctive feature that owing to counterflow of the gas and the charge, the gasifying agent (oxidant gas) preheats due to heat exchange with the solid residue and further hot gaseous products lend their heat to fresh mixture charged into reactor.
  • the gasifying agent oxidant gas
  • solid residue of processing is discharged from the reactor.
  • This residue can be processed, e.g., on a sieve and pieces of solid incombustible material isolated from the residue can be used for preparation of processing mixture. In particular, this applies to recycling of solid material intentionally introduced in the mixture.
  • the product gas withdrawn from the reactor can be burnt directly in a gas burner of power- generating utility. It also can be cleansed or processed according to known technologies.
  • pyrolysis oils can be condensed and used as a hydrocarbon feedstock and uncondensed gas as a fuel gas .
  • the smoke gas can be supplied as a component of gasifying agent either directly, or, alternatively, after being used for preliminary drying of the waste. In the latter case one can achieve both lower humidity of the waste charged into reactor and reduce overall volume of recycled smoke gas; correspondingly higher becomes combustion temperature of the product gas.
  • this invention makes possible pyrolysis and gasification of low-grade condensed fuels without additional heat supply and with high energy efficiency.
  • the energy necessary to support the process is supplied by combustion of a fraction of combustible part of the waste.
  • Introduction of steam and carbon dioxide from the smoke gas provides a possibility to enhance content of combustible components (hydrogen and carbon monoxide) in the product gas, while use of the smoke gas allows one to avoid additional energy expenditure to produce steam, only water contained in the waste is used in the process.
  • the figure schematically presents a possible materialization of the process.
  • Waste "W” is prepared in crasher 1, further in mixer 2 it is mixed with solid incombustible material "I” and then charged into shaft kiln reactor
  • a fraction of smoke gas "S" is directed to drier 15, where waste "W” is dried with the heat of smoke gas.
  • the temperatures in respective zones are measured continuously and when the temperatures deviate from prescribed optimal values, the control parameters are adjusted. In case the temperature in the combustion zone exceeds the prescribed limits the fraction of smoke gases in the gasifying agent is increased, correspondingly higher becomes content of steam and carbon dioxide in the gasifying agent and greater contribution of endothermic reactions
  • the fraction of smoke gases in the gasifying agent is reduced.
  • the concentration of oxygen in the gasifying agent is maintained within 2 to 18% by volume; when the oxygen concentration falls below said limit, this results in excessive dilution of the product gas with nitrogen of the smoke gas and this hampers combustion of the fuel gas, whereas at higher oxygen concentration there is insufficient yield of hydrogen and carbon monoxide according to aforementioned reactions.
  • composition wt.%: paper and cardboard 38.2, food residues 28.6, wood and leaves 1.8, textiles 4.9, leather and rubber 0.6, polymers 7.0, bones 1.0, metals 4.0, glass and stones 5.1, fines 9.1, having humidity 47% and calorific value of 5.87 GJ/t.
  • the composition of dry mass is : C - 32.25%, H - 4.46%, O - 25.78%, N - 0.93%, S - 0.32%, ash - 33.26%.
  • This composition is typical of solid municipal waste (SMW) of Moscow. 1A.
  • SMW is gasified with addition of 10 wt.% of solid inert material in the processing mixture and supply of the gasifying agent comprising 200 g steam per 1 kg of air.
  • the product gas is burnt with supply of secondary air so as to maintain volume concentration of oxygen in the smoke gas at 2% (on dry gas basis; i.e. overall stoichiometric ratio of oxygen is 1.1) .
  • Total air consumption (sum of that fed as gasifying agent constituent and secondary air fed to the gas burner) is 2.8 t per ton of SMW.
  • 170 kg of steam is consumed for gasification of 1 t SMW.
  • the smoke gas produced comprises (vol. %) : N 2 - 53.9, C0 2 - 11.0, 0 2 -1.3, Ar - 0.6, H 2 0 - 33.2%; yield of smoke gas is 3190 nm 3 per ton of SMW. IB.
  • SMW is gasified as in 1A but with gasifying agent composed of smoke gas and air in 11:10 volume ratio.
  • the smoke gas produced comprises (vol. %) : N 2 - 57.8, C0 2 - 11.8, 0 2 -1.3, Ar - 0.7, H 2 0 - 21.3; yield of smoke gas is 2980 nm 3 per ton of SMW. 1C.
  • SMW is gasified as in IB but with gasifying agent composed of smoke gas and air in 7:10 volume ratio, the smoke gas withdrawn from boiler at 250°C, being directed for drying of SMW. Smoke gas dries ca. 50 kg of water from a ton of SMW.
  • the composition of the smoke gas and yield of the smoke gas are the same as in IB.
  • the heat loss with smoke gas (primarily as the condensation heat of the steam in the smoke gas in 1A is ⁇ 500 MJ/ton of SMW higher than that in 1B,C.
  • Processed is biomass waste having humidity of 35% and ash content of 10% per total mass; the calorific value of the waste is 9.6 GJ/t.
  • the waste is gasified with addition of 20 wt.% of solid inert material in the processing mixture and supply of the gasifying agent comprising 200 g steam per 1 kg of air.
  • the product gas is burnt with supply of secondary air at 1.1 overall stoichiometric ratio of oxygen.
  • the smoke gas produced comprises (vol. %) : N 2 - 57.8, C0 2 - 12.8, 0 2 -1.5, Ar - 0.7, H 2 0 - 27.8%; yield of smoke gas is 3620 nm 3 per ton of fuel .
  • the waste is gasified as in 1A but with gasifying agent composed of smoke gas and air in 8:10 volume ratio.
  • the smoke gas produced comprises (vol.
  • yield of smoke gas is 3485 nm 3 per ton of SMW.
  • the waste is gasified as in 2B but with gasifying agent composed of smoke gas and air in 5:10 volume ratio, the smoke gas withdrawn from boiler at 250°C, being directed for drying of SMW.
  • Smoke gas dries ca. 30 kg of water from a ton of SMW. This water as steam enters the gasifying agent
  • the composition of the smoke gas and yield of the smoke gas are the same as in 2B.
  • the heat loss with smoke gas per ton of waste in 2A is ⁇ 350 MJ higher than that in 2B,C.
  • Example (3) Processed is oil slurry having humidity of
  • the slurry is gasified in mixture comprising 30 wt.% of slurry and 70% of solid inert material in the processing mixture and supply of the gasifying agent comprising 100 g steam per 1 kg of air.
  • the gasifying agent comprising 100 g steam per 1 kg of air.
  • 200 kg of oil is condensed from the product gas and uncondensed gas is burnt with supply of secondary air at 1.1 overall stoichiometric ratio of oxygen.
  • the smoke gas produced comprises (vol. %) : N 2 - 69.8, C0 2 - 13.8, 0 2 -1.7, Ar - 0.8, H 2 0 - 13; yield of smoke gas is 5560 nm 3 per ton of fuel .
  • the waste is gasified as in 3A but with gasifying agent composed of smoke gas and air in 1:1 volume ratio.
  • the smoke gas produced comprises (vol.
  • the heat loss with smoke gas per ton of waste in 3A is ⁇ 270 MJ higher than that in 3B.
  • brown coal having humidity of 29%, 41% content of combustibles, and ash content of 30% per total mass. 4A.
  • the coal is gasified with supply of the gasifying agent comprising 300 g steam per 1 kg of air.
  • the product gas is burnt with supply of secondary air at 1.1 overall stoichiometric ratio of oxygen.
  • the smoke gas produced comprises (vol. %) : N 2 - 60.2, CO- - 10.9, 0 2 -1.5, Ar - 0.7, H 2 0 - 26.2, S0 2 - 0.5; yield of smoke gas is 4500 nm 3 per ton of fuel.
  • the coal is gasified as in 4A but with gasifying agent composed of smoke gas and air in 1:1 volume ratio.
  • the smoke gas withdrawn from boiler at 250°C, being directed for drying of coal.
  • Smoke gas dries ca. 65 kg of water from a ton of coal.
  • the smoke gas produced comprises (vol. %) : N 2 - 65.7, C0 2 - 11.9, 11
  • the heat loss with smoke gas per ton of coal in 4A is ⁇ 800 MJ higher than that in 4B .
  • a comparison of the above examples shows that use of smoke gases as a component of the gasifying agent in gasification of combustible wastes provides a possibility to enhance energy efficiency of the process, as compared with the use of steam from external source, since heat loss with smoke gases becomes less. Additionally to that this allows one to exclude special apparatus for steam production.
  • Use of the smoke gas for preliminary partial drying of the fuel provides possibility to reduce volume of the smoke gas recycled and enhances the temperature of combustion of the product gas in burner.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention concerne des procédés de traitement de combustibles condensés à faible pouvoir calorifique, en particulier ceux qui sont très humides. Ce traitement se fait par pyrolyse et gazéification de leur partie organique, de façon à produire des produits hydrocarbonés liquides de pyrolyse et du gaz combustible, utilisés pour produire de l'énergie. Ce procédé peut être utilisé pour un traitement ou une élimination écologique de déchets faiblement combustibles. On introduit le combustible dans un four à cuve de type réacteur de gazéification, éventuellement avec un matériau solide non combustible, à contre-courant par rapport à un agent gazéifiant renfermant de l'oxygène, et on gazéifie les composants combustibles de la charge. On introduit dans l'agent gazéifiant des gaz de fumées. On régule la température maximale dans le réacteur pour qu'elle soit comprise entre 800 et 1300 °C, en modifiant la fraction des gaz de fumées dans l'agent gazéifiant, la teneur en oxygène dans l'agent gazéifiant étant régulée pour qu'elle soit comprise entre 2 et 18 % en volume.
PCT/FI1999/000044 1998-01-22 1999-01-22 Procede de traitement de combustibles condenses par gazeification WO1999037739A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
CA002318971A CA2318971A1 (fr) 1998-01-22 1999-01-22 Procede de traitement de combustibles condenses par gazeification
JP2000528647A JP2002501112A (ja) 1998-01-22 1999-01-22 ガス化によって凝縮燃料を処理する方法
EP99901608A EP1049755A1 (fr) 1998-01-22 1999-01-22 Procede de traitement de combustibles condenses par gazeification
AU21660/99A AU738097B2 (en) 1998-01-22 1999-01-22 A method for processing condensed fuel by means of gasification

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU98101335 1998-01-22
RU98101335/03A RU2152561C1 (ru) 1998-01-22 1998-01-22 Способ переработки конденсированных горючих

Publications (1)

Publication Number Publication Date
WO1999037739A1 true WO1999037739A1 (fr) 1999-07-29

Family

ID=20201550

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI1999/000044 WO1999037739A1 (fr) 1998-01-22 1999-01-22 Procede de traitement de combustibles condenses par gazeification

Country Status (6)

Country Link
EP (1) EP1049755A1 (fr)
JP (1) JP2002501112A (fr)
AU (1) AU738097B2 (fr)
CA (1) CA2318971A1 (fr)
RU (1) RU2152561C1 (fr)
WO (1) WO1999037739A1 (fr)

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WO2000043468A1 (fr) * 1999-01-25 2000-07-27 Valtion Teknillinen Tutkimuskeskus Procede de gazeification de combustible carbone dans un gazeifieur a lit fluidise
WO2009080336A2 (fr) 2007-12-20 2009-07-02 Ecoloop Gmbh Procédé autothermique pour la gazéification continue de substances riches en carbone
CN101412915B (zh) * 2008-11-21 2011-12-14 中国林业科学研究院林产化学工业研究所 内热式连续制备生物质热解气化煤气的方法及热解气化炉
US8246700B1 (en) * 2007-12-06 2012-08-21 Leonid Kutsin Method and system for recycling flue gas
WO2013087172A1 (fr) * 2011-12-16 2013-06-20 Ecoloop Gmbh Gazéification à contre-courant avec un gaz de synthèse comme fluide de travail
RU2611870C2 (ru) * 2015-06-15 2017-03-01 Федеральное государственное бюджетное образовательное учреждение высшего образования "Уфимский государственный нефтяной технический университет" Способ переработки нефтесодержащих отходов (шламов)
CN107841344A (zh) * 2017-11-14 2018-03-27 华电电力科学研究院 一种电厂烟气与碳基固体燃料反应制取燃气的系统及方法
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RU2495076C1 (ru) 2012-07-25 2013-10-10 Закрытое Акционерное Общество Научно-Производственная Компания "Интергаз" Способ переработки горючих углерод- и/или углеводородсодержащих продуктов, реактор для его осуществления (варианты) и установка для переработки горючих углерод- и/или углеводородсодержащих продуктов
RU2520450C2 (ru) * 2012-10-09 2014-06-27 Общество с ограниченной ответственностью "Альтернативные Тепловые Технологии" (ООО АТТ) Способ получения свободного от пиролизных смол горючего газа при газификации конденсированного топлива и газогенераторы для его осуществления
CN109251753A (zh) * 2018-05-25 2019-01-22 华北科技学院 一种可再生能源协同互补的热电冷气联供系统及工艺
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WO2000043468A1 (fr) * 1999-01-25 2000-07-27 Valtion Teknillinen Tutkimuskeskus Procede de gazeification de combustible carbone dans un gazeifieur a lit fluidise
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CN110319452A (zh) * 2019-07-05 2019-10-11 中节能(盘锦)清洁技术发展有限公司 锅炉烟气温度调节装置以及方法
RU2756622C1 (ru) * 2020-08-04 2021-10-04 Федеральное государственное автономное образовательное учреждение высшего образования "Сибирский федеральный университет" Способ переработки грунтов, загрязненных нефтепродуктами

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AU738097B2 (en) 2001-09-06
RU2152561C1 (ru) 2000-07-10
AU2166099A (en) 1999-08-09

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