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WO1999037738A1 - Procede de traitement de dechets urbains solides - Google Patents

Procede de traitement de dechets urbains solides Download PDF

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Publication number
WO1999037738A1
WO1999037738A1 PCT/FI1999/000045 FI9900045W WO9937738A1 WO 1999037738 A1 WO1999037738 A1 WO 1999037738A1 FI 9900045 W FI9900045 W FI 9900045W WO 9937738 A1 WO9937738 A1 WO 9937738A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasifying agent
smw
mass fraction
reactor
gas
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/FI1999/000045
Other languages
English (en)
Inventor
Georgi B. Manelis
Victor P. Foursov
Evgueni V. Poliantchik
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.)
Fioter Oy
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 AU21661/99A priority Critical patent/AU2166199A/en
Publication of WO1999037738A1 publication Critical patent/WO1999037738A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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
    • 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 solid municipal wastes (SMW) , primarily highly humid ones, 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.
  • a number of methods for incineration of combustible wastes with energy generation is known. Among those, distinguished by their environmental friendliness are the methods based on two-stage processing, first gasification and then combustion of the product gas.
  • the gasification of organic fuels in counterflow of a gasifying agent can be presented as follows .
  • the gasifying agent containing oxygen and possibly water and/or carbon dioxide enters the com- bustion 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 decreases as the gas filters through the solid 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 for pyrolysis and combustion of combustible part of SMW is described in patent US-A- 4732091.
  • the solid fuel is charged in the upper part of a shaft kiln.
  • the fuel charged is supplied with the rate controlled by moving horizontal grates through a succession of zones wherein the fuel pyrolyzes and burns in a counterflow of air-steam gasifying agent.
  • This method is based on loosening the material with gratings; thus gas- permeability of the fuel is secured.
  • This method also proposes way to control fuel supply to respective zones .
  • a method described in patent RU-2079051 proposes gasification of solid municipal waste in a coun- tercurrent of 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) 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.
  • the product gas is directed for combustion in a boiler.
  • the objective of this invention is to perform pyrolysis and gasification of SMW 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:
  • 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 product gas can be burnt on its own or as a byfuel on natural gas or oil fed boiler.
  • the smoke gases produced in latter case can also be used in this process since they contain carbon dioxide and steam.
  • the oxygen content in smoke gas can vary and at high oxy- gen excess the smoke gas can be directly used as the gasifying agent.
  • 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, hydro- gen, 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 undergo pyrolysis 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. Further the mixture containing coked combustibles enters the gasification (combustion) zone where preheated gasify- ing agent reacts with coke at 800 - 1300°C to yield combustible gas and solid residue of combustion. Finally, the solid residue enters the cooling zone where owing to heat exchange of the solid residue with coun- tercurrently 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.
  • the distinctive feature is that owing to counter- flow 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 solid residue of processing is discharged from the reactor.
  • the product gas withdrawn from the reactor can be di- rectly burnt in gas burner of a boiler; alternatively it can be cleansed or processed according to conventional techniques. So the pyrolysis oils can be condensed and used as a hydrocarbons feedstock and uncon- densed gas used as fuel gas .
  • the smoke gases can be supplied as a component of gasifying agent either directly, or, alternatively, after being used for preliminary drying of the waste .
  • this invention makes possible pyrolysis and gasification of SMW 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.
  • 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 4 through lock 3 at its upper part.
  • reactor 4 the mixture successively passes through heating zone 5, pyrolysis zone 6, combustion zone 7, and cooling zone 8.
  • Solid processing residue “R” is continuously discharged via lock 9 with the rate controlled so as to maintain combustion zone at certain elevation from the reactor bottom.
  • the solid residue is fractionated on sieve 10 and a part of it is recycled as solid material mixed with waste and the rest of solid residue is directed for further processing or disposal.
  • Air “A ⁇ " is supplied by fan 11 to the lower part of the reactor. To the same zone exhaust fan 12 supplies smoke gas "S".
  • the product gas "G” is withdrawn from the upper part of the reactor and directed to gas cleansing unit 13.
  • gas cleansing unit 13 In the condenser liquid products “C” are isolated from the product gas.
  • the product gas is directed for combustion with air “A 2 " in steam boiler 14.
  • 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 oxygen in the gasifying agent is decreased through higher content of smoke gases and correspondingly higher content of steam and carbon dioxide in the gasifying agent. Upon this greater becomes contribution of endo- thermic reactions C + C0 2 ⁇ 2 CO
  • Solid municipal waste of the following 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 .
  • Ash content of dry mass is 27%.
  • the elemental composition of combustible part of SMW corresponds to formula CH 172 O 076 N 0 ⁇ S 0 _ 003 . This composition is typical of Moscow SMW.
  • 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 constitu- ent and secondary air fed to the gas burner) is about 3 t per ton of SMW.
  • the smoke gas produced comprises (vol.
  • SMW is gasified as in 1A but with gasifying agent composed of smoke gas and air in 1:1 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 3220nm 3 per ton of SMW. ⁇ A - 0.082) 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. This water as steam enters the gasifying agent
  • 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.
  • SMW preliminary treated with re- covery of a part of metal, glass, textiles, plastics, and cardboard suited for reprocessing.
  • the material gasified has humidity of 50%, calorific value of 4.3 GJ/t, and ash content of 15% per dry mass.
  • the elemental composition of combustible part of SMW corresponds to formula CH X 8 O 0.75 N 0 -S 0 . 004 .
  • SMW is gasified with addition of 15 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 constitu- ent and secondary air fed to the gas burner) is about 2.5 t per ton of SMW.
  • the smoke gas produced comprises (vol.
  • 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
  • Smoke gas dries ca . 30 kg of water from a ton of SMW. This water as steam enters the gasifying agent
  • the heat loss with smoke gas per ton of waste in 2A is ⁇ 400 MJ higher than that in 2B,C,D.
  • processing of highly humid wastes according to the above described method requires generally lower A than described in RU-2079051, since ratio A characterizes heat exchange in the zone of solid residue cooling, whereas the necessity to evaporate substantial quantity of water with its high latent heat of evaporation makes necessary to shift the heat exchange balance so as let more heat enter the drying zone.
  • Reduction of A below the abovementioned limit is disadvantageous, because it lowers preheating of the gasifying agent prior to it entering the combustion zone .

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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 déchets urbains solides (SMW) combustibles, 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 les déchets urbains solides 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 des déchets urbains solides. 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 au moins un des paramètres suivants: la fraction en masse de l'oxygène dans l'agent gazéifiant a, la fraction en masse des non combustibles dans des déchets urbains solides traités b, et la fraction en masse des combustibles dans des déchets urbains solides traités c, tout en maintenant un rapport A = ab/c compris entre 0,022 et 0,1.
PCT/FI1999/000045 1998-01-22 1999-01-22 Procede de traitement de dechets urbains solides Ceased WO1999037738A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU21661/99A AU2166199A (en) 1998-01-22 1999-01-22 A method for processing solid municipal waste

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU98101334/03A RU2150045C1 (ru) 1998-01-22 1998-01-22 Способ переработки горючих твердых бытовых отходов
RU98101334 1998-01-22

Publications (1)

Publication Number Publication Date
WO1999037738A1 true WO1999037738A1 (fr) 1999-07-29

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ID=20201549

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI1999/000045 Ceased WO1999037738A1 (fr) 1998-01-22 1999-01-22 Procede de traitement de dechets urbains solides

Country Status (3)

Country Link
AU (1) AU2166199A (fr)
RU (1) RU2150045C1 (fr)
WO (1) WO1999037738A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003012013A1 (fr) 2001-08-02 2003-02-13 T.G.E. Tech. Ltd. Procede et appareil de traitement des ordures menageres
EP2246411A4 (fr) * 2008-01-08 2012-10-17 Wenzhen Liu Procédé et appareil destinés à produire du gaz combustible à partir de biomasse

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2232347C2 (ru) * 2002-02-27 2004-07-10 Мещанкин Андрей Иванович Газификатор твердого топлива
RU2293108C1 (ru) * 2005-09-30 2007-02-10 ООО "Вихревые системы" Способ получения генераторного газа и устройство для его осуществления
RU2364451C1 (ru) 2008-07-21 2009-08-20 Сергей Юрьевич Вильчек Универсальный способ переработки материалов в секционном аппарате барабанного типа с проходными отверстиями в перегородках между секциями и устройство для его осуществления
RU2478169C1 (ru) * 2011-09-23 2013-03-27 Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Юго-Западный государственный университет" (ЮЗГУ) Плазмохимический способ переработки твердых бытовых и промышленных отходов
RU2545199C1 (ru) * 2014-01-29 2015-03-27 Андрей Иванович Мещанкин Газификатор твердых бытовых отходов и твердого топлива

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4164397A (en) * 1976-10-18 1979-08-14 Hunt Herbert H Fuel gas production
WO1990007085A1 (fr) * 1988-12-16 1990-06-28 Gunn Robert D Procede et appareil de gazeification douce a contre-courant
EP0381254A1 (fr) * 1989-01-31 1990-08-08 ENIRICERCHE S.p.A. Procédé d'obtention de gaz de synthèse à partir de combustibles solides dérivés de déchets solides urbains ou de déchets solides industriels
WO1996000267A1 (fr) * 1994-06-23 1996-01-04 Envirotec Group Limited Procede pour traiter les dechets municipaux combustibles solides ou analogues par gazeification

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0498014B2 (fr) * 1991-02-07 1996-10-30 MARTIN GmbH für Umwelt- und Energietechnik Procédé pour l'admission d'air de combustion et installation de chauffage
FR2704047B1 (fr) * 1993-04-16 1995-07-13 Electricite De France Dispositif de traitement et de vitrification de déchets.
RU2079051C1 (ru) * 1994-06-23 1997-05-10 Институт химической физики в Черноголовке РАН Способ переработки твердых бытовых отходов

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4164397A (en) * 1976-10-18 1979-08-14 Hunt Herbert H Fuel gas production
WO1990007085A1 (fr) * 1988-12-16 1990-06-28 Gunn Robert D Procede et appareil de gazeification douce a contre-courant
EP0381254A1 (fr) * 1989-01-31 1990-08-08 ENIRICERCHE S.p.A. Procédé d'obtention de gaz de synthèse à partir de combustibles solides dérivés de déchets solides urbains ou de déchets solides industriels
WO1996000267A1 (fr) * 1994-06-23 1996-01-04 Envirotec Group Limited Procede pour traiter les dechets municipaux combustibles solides ou analogues par gazeification

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003012013A1 (fr) 2001-08-02 2003-02-13 T.G.E. Tech. Ltd. Procede et appareil de traitement des ordures menageres
US7028624B2 (en) 2001-08-02 2006-04-18 T.G.E. Tech Ltd. Method and apparatus for the treatment of domestic waste
EP2246411A4 (fr) * 2008-01-08 2012-10-17 Wenzhen Liu Procédé et appareil destinés à produire du gaz combustible à partir de biomasse

Also Published As

Publication number Publication date
AU2166199A (en) 1999-08-09
RU2150045C1 (ru) 2000-05-27

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