US20100140074A1 - Method and equipment for pyrolytic conversion of combustible material - Google Patents

Method and equipment for pyrolytic conversion of combustible material Download PDF

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Publication number
US20100140074A1
US20100140074A1 US12/671,696 US67169608A US2010140074A1 US 20100140074 A1 US20100140074 A1 US 20100140074A1 US 67169608 A US67169608 A US 67169608A US 2010140074 A1 US2010140074 A1 US 2010140074A1
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US
United States
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.)
Abandoned
Application number
US12/671,696
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English (en)
Inventor
Václav Holusa
Petr Vanicek
Ivan Koutnik
Miroslav Kaloc
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Individual
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Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of US20100140074A1 publication Critical patent/US20100140074A1/en
Abandoned 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° 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° 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.
  • 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° C. as a maximum.
  • After passage of combustible material through the reaction zone 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.
  • 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. It is also advantageous that 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. heating, gasification, reduction reaction and, alternatively, water gas generation.
  • Other advantages include variability of capacity, variability of physical properties of combustible material, e.g. different granulometry or different content of liquid portion.
  • the equipment may be designed as mobile.
  • Another advantage is that no output analysis of pyrolyzed gas is necessary and that the equipment is not dependant on other technologies, such as gas treatment equipment.
  • 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.
  • incombustible residues having temperature not greater than 1200° C. is thrown off the reaction zone to a shaft, where it is collected and from which is removed periodically.
  • 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 1 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 12 , has an elongated shape, its longitudinal axis is vertical.
  • Filling device 1 is located in the lowest part of reactor 2 and inlet of hopper 4 for non-gasified residue 8 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 , 13 . Gas outlet 16 is led to the reactor 2 in its highest point.
  • Both the low-temperature heater 3 and high-temperature heater 13 represent electric heating spirals.
  • the filling device 1 comprises a piston 10 with annular-shaped base, to in the centre of which column 9 is located.
  • the filling hole 14 of reactor 2 is provided with a rib 15 .
  • the rib 15 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 13 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.

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  • 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)
US12/671,696 2007-08-16 2008-05-12 Method and equipment for pyrolytic conversion of combustible material Abandoned US20100140074A1 (en)

Applications Claiming Priority (3)

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
PCT/CZ2008/000052 WO2009021471A2 (en) 2007-08-16 2008-05-12 Method and equipment for pyrolytic conversion of combustible material

Publications (1)

Publication Number Publication Date
US20100140074A1 true US20100140074A1 (en) 2010-06-10

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ID=39820945

Family Applications (1)

Application Number Title Priority Date Filing Date
US12/671,696 Abandoned US20100140074A1 (en) 2007-08-16 2008-05-12 Method and equipment for pyrolytic conversion of combustible material

Country Status (7)

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

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 (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4004982A (en) * 1976-05-05 1977-01-25 Union Oil Company Of California Superatmospheric pressure shale retorting process

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE487697A (cs) *
JPH0192291A (ja) * 1987-10-02 1989-04-11 Kanagawa Pref Gov 乾留装置
DE19928581C2 (de) * 1999-06-22 2001-06-28 Thermoselect Ag Vaduz Verfahren und Vorrichtung zur Entsorgung und Nutzbarmachung von Abfallgütern
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 (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4004982A (en) * 1976-05-05 1977-01-25 Union Oil Company Of California Superatmospheric pressure shale retorting process

Also Published As

Publication number Publication date
WO2009021471A2 (en) 2009-02-19
CZ2007553A3 (cs) 2009-02-25
EP2197982A2 (en) 2010-06-23
WO2009021471A3 (en) 2009-04-09
WO2009021471A4 (en) 2009-05-28
JP2010536536A (ja) 2010-12-02
CN101778926A (zh) 2010-07-14
RU2010107304A (ru) 2011-09-10

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