WO2009021471A2 - Procédé et équipement de conversion pyrolytique de matériau combustible - Google Patents

Procédé et équipement de conversion pyrolytique de matériau combustible Download PDF

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Publication number
WO2009021471A2
WO2009021471A2 PCT/CZ2008/000052 CZ2008000052W WO2009021471A2 WO 2009021471 A2 WO2009021471 A2 WO 2009021471A2 CZ 2008000052 W CZ2008000052 W CZ 2008000052W WO 2009021471 A2 WO2009021471 A2 WO 2009021471A2
Authority
WO
WIPO (PCT)
Prior art keywords
reaction zone
combustible material
reactor
equipment
pyrolytic conversion
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/CZ2008/000052
Other languages
English (en)
Other versions
WO2009021471A4 (fr
WO2009021471A3 (fr
Inventor
Václav HOLUSA
Petr Vanicek
Ivan Koutnik
Miroslav Kaloc
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.)
Agro - Eko Spol S Ro
Original Assignee
Agro - Eko Spol S Ro
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 Agro - Eko Spol S Ro filed Critical Agro - Eko Spol S Ro
Priority to EP08757906A priority Critical patent/EP2197982A2/fr
Priority to JP2010520414A priority patent/JP2010536536A/ja
Priority to CN200880103022A priority patent/CN101778926A/zh
Priority to US12/671,696 priority patent/US20100140074A1/en
Publication of WO2009021471A2 publication Critical patent/WO2009021471A2/fr
Publication of WO2009021471A3 publication Critical patent/WO2009021471A3/fr
Publication of WO2009021471A4 publication Critical patent/WO2009021471A4/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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts
    • 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
    • C10J3/20—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/154—Pushing devices, e.g. pistons
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
    • C10J2300/1276—Heating the gasifier by radiating device, e.g. radiant tubes by electricity, e.g. resistor heating
    • 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
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the invention concerns the method and equipment for pyrolytic conversion of combustible material and relates to the problem of production of energetically and technologically flammable gas, which does not contain tar, and at the same time it relates to effective and ecological utilization of solid substances or mixtures with predominant content of solid substances, such as coal, wooden chips or waste organic residues, namely fermentatively hygienized waste from agricultural or food- industry production or other matters containing free or organically bound carbon.
  • Efficiency of the process proceeding within the temperature range from 600 up to 900 0 C on a decomposition bed containing lime, dolomite and, as catalysts, alumina and silicon carbide, is 60 to 90%.
  • Another known possibility is the use of disc filters filled with alumina mixed with powdered nickel and magnesium oxide. The best temperature for this process is 850 0 C.
  • grain bed formed by dolomite modified by nickel is known as well. Even this process takes place at elevated temperature.
  • disadvantages of the processes described above include sensitivity to presence of sulphur compounds, calcium oxide is also added to dolomite usually. It is also known that natural catalysts such as a mixture of limestone, olivine and dolomite or zeolite may also be used for catalytic tar decomposition.
  • Catalytic effect is also featured by substances with increased content of ferric oxide such as siderite or limonite.
  • a joint disadvantage of all catalytic processes is the necessity of grain bed renewal, availability of all components, problems with environment-friendly disposal or with recycling of decomposition bad material used.
  • Another weakness of catalytic processes is that they take place at elevated temperatures, which increases energy consumption of processing.
  • the essence of the invention is that combustible material is supplied to the reaction zone, continuously or in pulses, which the reaction zone is separated from the surrounding atmosphere, after which combustible material is gradually shifted through the reaction zone to the reaction zone outlet, in the same direction as released gases leave the combustible material.
  • the reaction zone is heated to the temperature, the value of which is increasing in the direction to the reaction zone outlet, however, to 1200 0 C as a maximum.
  • the released gases are draught off separately from non- gasified residue.
  • water steam and/or water are brought to combustible material before entry into the reaction zone and/or upon its passage through the reaction zone.
  • combustible material previously charged into the reaction zone moves through the reaction zone by acting of subsequently supplied combustible material.
  • combustible material is compressed in at least one section while moving through the reaction zone.
  • the essence of the equipment comprising at least one filling device, reactor comprising the reaction zone, at least one heater and hopper for non-gasified residue is that the reactor has an elongated shape and its longitudinal axis is deviated from the vertical direction by 45° as a maximum, where the filling device is located in the lowest part of the reactor and non-gasified residue hopper inlet is located in the upper part of the reactor.
  • the reactor comprises the reaction zone which is in contact with at least one heater.
  • the non-gasified residue hopper is connected to the reactor above the reaction zone.
  • the horizontal cross-section of the reaction zone in upwards direction is narrowing in at least one part.
  • at least one supply piping is led into the reaction zone as a steam and/or water supply.
  • At least one column is located inside the reactor, in its elongated directions.
  • heaters are electric heating spirals and/or burners.
  • the filling device alternatively includes at least one piston which advantageously has annular-shaped base, in the centre of which at least one column or worm is located, advantageously the worm is whipped around the column.
  • An advantageous alternative is achieved if the reactor filling hole is provided with a rib which to advantage comprises conical surface extending in the direction to the reaction zone.
  • Advantage of the method and equipment is that generated gas does not contain tar, which contributes to failure-free operation of associated technologies. Generated gas has high heating value as it is enriched with flammable substances generated by tar decomposition.
  • the method is easy controllable by temperature regulation and by supply of combustible material.
  • Advantage of method is also low energy demand.
  • generated gas can be used in associated technologies.
  • Another advantage is that all organically bounded or free carbon can be converted to gas.
  • process runs continuously generated gas has homogenous composition, quantity of solid residue is minimized and solid residue is also continuously removed from the reaction zone.
  • An advantage of steam blowing or water supply to processes running in the reactor is minimized quantity of free or organically bound carbon in non-gasified residue, as it has been converted to carbon monoxide by reaction with water, with simultaneous generation of hydrogen, which results in improved equipment efficiency.
  • An advantage of the equipment is that it has simple and compact design, as all processes take place in one reaction zone, i.e.
  • Fig.1 shows a scheme of equipment as per example 4, while Fig. 2 shows equipment as per example 5.
  • combustible material is fermentatively hygienized waste from agricultural and food production.
  • Combustible material is continuously supplied to the reaction zone, which is heated by gas burners and separated from surrounding atmosphere.
  • combustible material is exposed to gradually increasing temperature, generating gases which pass through the combustible material, exposed to higher temperature than the combustible material from which gas has generated.
  • gas passes through the combustible material chemical reactions proceed resulting in gasification of additional portions of combustible material and change in gas chemical composition.
  • water evaporates and absorbed gases, such as CO 2 and CH 4 primarily release.
  • Temperature around 250 °C represents the beginning of organic compound splitting accompanied with generation of CO 2 a CO.
  • fission reactions continue, generating CO 2 and CO and starting other decomposition reactions resulting in generation of CH 4 and H 2 .
  • tar substances start releasing and combustible material losses residues of bound hydrogen and oxygen.
  • temperatures above 550 °C the original organic material is virtually decomposed to carbon, released gas and tar substances. If temperature increasing continues, above temperature of 700 °C, decomposition of tar substances, with generation of hydrogen, take place.
  • Example 2 differs from Example 1 in that, the reaction zone is heated electrically, combustible material forming a charge is dosed into the equipment periodically in predetermined volumes and, moreover, steam content in the reaction zone increases by supplying it from an external source. In this case, production of H 2 and CO is much more intensive and amount of non-gasified residue is lower, as there is nearly no free carbon contained therein, nor any other organic carbon compounds.
  • Example 3 differs from Example 1 in that combustible material contains 30% of tires as a minimum.
  • Equipment for pyrolytic conversion of combustible material to pyrolyzed gas and non-gasified residue 8 as per Example 4 consists of the filling device I, reactor 2, comprising reaction zone 5, low-temperature heater 3_ and high-temperature heater 13, and hopper 4 for non-gasified residue 8.
  • Reactor 2 covered by lagging ⁇ 2, has an elongated shape, its longitudinal axis is vertical.
  • Filling device I is located in the lowest part of reactor 2 and inlet of hopper 4 for non-gasified residue S is located in the upper part of the reactor 2.
  • the reactor 2 includes reaction zone 5, which is in contact with both heaters 3, J_3. Gas outlet 16 is led to the reactor 2 in its highest point.
  • the inlet piping 6_ for supplying of steam and/or water is led into the reaction zone 5.
  • the column 9 is also located inside the reactor 2 in its longitudinal axis. Both the low-temperature heater 3 and high-temperature heater !3_represent electric heating spirals.
  • the filling device i comprises a piston K) with annular-shaped base, in the centre of which column 9 is located.
  • the filling hole 14 of reactor 2 is provided with a rib 15.
  • the rib J_5 has a conical frustum shape, its greater base is located on the side of reaction zone 5. Equipment according to this example works in the manner described in Example 2.
  • Equipment for pyrolytic conversion of combustible material as per Example 5 differs from the equipment described in Example 4 in that any inlet piping 6 is led into the reaction zone 5, for supplying stream and/or water and both low-temperature heater 3 and high-temperature heater ]_3 represent gas burners, filling hole 14 of reactor 2 is not provided with rib 15 . and filling device 1 comprises worm 7 which whips around the column 9. Equipment according to per this example works in the manner described in Example 1.
  • the invention can be used for processing of all solid matters or mixtures with the majority of solid matters, containing free or organically bound carbon, either for solid matter gasification or for concentration of substances forming non-combustible residue.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)

Abstract

Selon la présente invention, un matériau combustible est fourni à la zone de réaction, de façon continue ou par impulsions, la zone de réaction étant séparée de l'atmosphère environnante, et le matériau combustible se déplace progressivement à travers la zone de réaction vers la sortie de la zone de réaction, dans la même direction que les gaz libérés s'échappant du matériau combustible. La zone de réaction est chauffée à une température dont la valeur augmente en direction de la sortie de la zone de réaction, jusqu'à un maximum de 12 000 °C. Puis, les gaz libérés sont extraits séparément des résidus non gazéifiés. Un effet avantageux de l'invention est que la vapeur et/ou l'eau est/sont fournie(s) au matériau combustible et que le matériau combustible précédemment chargé dans la zone de réaction se déplace sous l'action du matériau combustible fourni par la suite, le matériau combustible étant ainsi compressé. L'équipement de conversion pyrolytique comprend un dispositif de remplissage (1), un réacteur (2) comprenant la zone de réaction (5), au moins un réchauffeur (3, 13), et une trémie (4) pour les résidus non gazéifiés (8). Le réacteur (2) a une forme allongée et son axe longitudinal est incliné par rapport à la direction verticale de 45° au maximum. Le dispositif de remplissage (1) se trouve dans la partie la plus basse du réacteur (2) et l'entrée de la trémie (4) pour les résidus non gazéifiés (8) se trouve dans la partie supérieure du réacteur (2). Le réacteur (2) comprend une zone de réaction (5), qui est en contact avec au moins un réchauffeur (3, 13). La trémie (4) pour les résidus non gazéifiés (8) est reliée au réacteur (2) au-dessus de la zone de réaction (5). La coupe transversale horizontale de la zone de réaction (5) en direction du haut se rétrécit dans au moins une partie, et de façon avantageuse, au moins un conduit d'entrée (6) mène dans la zone de réaction (5) pour l'alimentation en vapeur et/ou en eau. De façon également avantageuse, au moins une colonne (9) se trouve à l'intérieur du réacteur (2), dans le sens de sa longueur. Les réchauffeurs (3,13) sont des spirales de chauffage électrique et/ou des brûleurs. Le dispositif de remplissage (1) comprend au moins un piston (10) ayant, de façon avantageuse, une base de forme annulaire (10), au centre de laquelle se trouve au moins une colonne (9) ou une vis sans fin. Il est avantageux que la vis sans fin soit formée autour de la colonne (9) et que l'orifice de remplissage (14) du réacteur (2) comporte une nervure (15).
PCT/CZ2008/000052 2007-08-16 2008-05-12 Procédé et équipement de conversion pyrolytique de matériau combustible Ceased WO2009021471A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP08757906A EP2197982A2 (fr) 2007-08-16 2008-05-12 Procédé et équipement de conversion pyrolytique de matériau combustible
JP2010520414A JP2010536536A (ja) 2007-08-16 2008-05-12 可燃性物質の熱分解転化のための方法及び装置
CN200880103022A CN101778926A (zh) 2007-08-16 2008-05-12 用于可燃材料的高温转化的方法和设备
US12/671,696 US20100140074A1 (en) 2007-08-16 2008-05-12 Method and equipment for pyrolytic conversion of combustible material

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CZ20070553A CZ2007553A3 (cs) 2007-08-16 2007-08-16 Zpusob a zarízení pro pyrolytickou premenu spalitelného materiálu
CZPV2007-553 2007-08-16

Publications (3)

Publication Number Publication Date
WO2009021471A2 true WO2009021471A2 (fr) 2009-02-19
WO2009021471A3 WO2009021471A3 (fr) 2009-04-09
WO2009021471A4 WO2009021471A4 (fr) 2009-05-28

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PCT/CZ2008/000052 Ceased WO2009021471A2 (fr) 2007-08-16 2008-05-12 Procédé et équipement de conversion pyrolytique de matériau combustible

Country Status (7)

Country Link
US (1) US20100140074A1 (fr)
EP (1) EP2197982A2 (fr)
JP (1) JP2010536536A (fr)
CN (1) CN101778926A (fr)
CZ (1) CZ2007553A3 (fr)
RU (1) RU2010107304A (fr)
WO (1) WO2009021471A2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CZ306173B6 (cs) * 2012-06-28 2016-09-07 Polycomp, A.S. Linka na zpracování odpadu, obsahujícího převážně plasty a celulózu, a způsob zpracování odpadu na této lince
CN105012267A (zh) * 2015-08-19 2015-11-04 海南科进生物制药有限公司 一种瑞巴派特片及其制备方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE487697A (fr)
US4004982A (en) 1976-05-05 1977-01-25 Union Oil Company Of California Superatmospheric pressure shale retorting process
DE19928581A1 (de) 1999-06-22 2001-01-11 Thermoselect Ag Vaduz Verfahren und Vorrichtung zur Entsorgung und Nutzbarmachung von Abfallgütern

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0192291A (ja) * 1987-10-02 1989-04-11 Kanagawa Pref Gov 乾留装置
JP4938920B2 (ja) * 2000-02-29 2012-05-23 三菱重工業株式会社 バイオマスガス化炉及びバイオマスのガス化システム
JP2003221111A (ja) * 2002-01-31 2003-08-05 Oriental Kiden Kk ダイオキシン揮発分離装置
JP2005179509A (ja) * 2003-12-19 2005-07-07 Matsushita Electric Ind Co Ltd 加熱方法
JP2006143983A (ja) * 2004-10-20 2006-06-08 Mitsui Eng & Shipbuild Co Ltd ガス化装置の運転方法及びガス化装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE487697A (fr)
US4004982A (en) 1976-05-05 1977-01-25 Union Oil Company Of California Superatmospheric pressure shale retorting process
DE19928581A1 (de) 1999-06-22 2001-01-11 Thermoselect Ag Vaduz Verfahren und Vorrichtung zur Entsorgung und Nutzbarmachung von Abfallgütern

Also Published As

Publication number Publication date
JP2010536536A (ja) 2010-12-02
US20100140074A1 (en) 2010-06-10
CZ2007553A3 (cs) 2009-02-25
WO2009021471A4 (fr) 2009-05-28
WO2009021471A3 (fr) 2009-04-09
CN101778926A (zh) 2010-07-14
EP2197982A2 (fr) 2010-06-23
RU2010107304A (ru) 2011-09-10

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