WO1987004453A1 - Method and apparatus for gasifying carbonaceous material - Google Patents

Method and apparatus for gasifying carbonaceous material Download PDF

Info

Publication number
WO1987004453A1
WO1987004453A1 PCT/FI1987/000011 FI8700011W WO8704453A1 WO 1987004453 A1 WO1987004453 A1 WO 1987004453A1 FI 8700011 W FI8700011 W FI 8700011W WO 8704453 A1 WO8704453 A1 WO 8704453A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
zone
fluidized bed
gas
gasifying
Prior art date
Application number
PCT/FI1987/000011
Other languages
French (fr)
Inventor
Jorma Nieminen
Original Assignee
A. Ahlstrom Corporation
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 A. Ahlstrom Corporation filed Critical A. Ahlstrom Corporation
Priority to DE8787900821T priority Critical patent/DE3781680T2/en
Priority to AT87900821T priority patent/ATE80412T1/en
Priority to JP62500728A priority patent/JPH0668108B2/en
Publication of WO1987004453A1 publication Critical patent/WO1987004453A1/en
Priority to KR8770859A priority patent/KR900004526B1/en

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M53/00—Fuel-injection apparatus characterised by having heating, cooling or thermally-insulating means
    • F02M53/04—Injectors with heating, cooling, or thermally-insulating means
    • F02M53/06—Injectors with heating, cooling, or thermally-insulating means with fuel-heating means, e.g. for vaporising
    • 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
    • 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
    • C10J3/56—Apparatus; Plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
    • F02M57/00—Fuel-injectors combined or associated with other devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23Q—IGNITION; EXTINGUISHING-DEVICES
    • F23Q7/00—Incandescent ignition; Igniters using electrically-produced heat, e.g. lighters for cigarettes; Electrically-heated glowing plugs
    • F23Q7/001—Glowing plugs for internal-combustion engines
    • 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
    • C10J2300/0953—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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the present invention relates to a method for gasification of carbonaceous material in two phases in a circulating fluidized bed reactor in which solid particles contained in gases exhausted from the reactor are separated and recycled to the reactor.
  • the invention also relates to an apparatus for carrying out the method.
  • HT gasifier Hochtemperatur-Winkler
  • gases hydrogen, carbon monoxide, methane
  • Oxygen then reacts primarily with these gaseous substances although a reaction with the coal would be advantagous for the product of the gasification.
  • Contact of the coal and the supplied aqueous steam also decreases which results in an incomplete coal conversion and low grade gas.
  • British patent specification number 1506729 discloses a method of gasifying carbonaceous material in a circulating fluidized bed reactor which is devided into two parts and in which the carbonaceous material is supplied to the upper part of a gasification reactor.
  • the first stage of the gasification for example pyrolyses of the volatiles, during which pyrolysis for example tarry substances build up, takes place in the upper part of the reactor, the tarry substances remain in the product gas.
  • the amount of these tarry substances depends on the gasified material and the gasification temperature and it may, e.g. in case of coal, be small.
  • the object of this prior method does not primarily seem to be to produce gas of low tar content either but to achieve an as good a coal coversion as possible.
  • the primary object of the present invention is to produce gas containing as little tar as possible.
  • the upper part of the reactor is used for removing tar by raising the temperature.
  • An essential feature is that the temperature is increased by combusting coal and not gaseous components. To achieve this, a spouting type fluidized bed is used.
  • Finnish patent specification number 62554 discloses a two- staged gasification method, in which the beginning of . the gasification process is carried out in the upper part of the reactor, as in the method of GB 1506729 mentioned above, and the tarry substances remain in the product ⁇ as.
  • the present invention is characterized in that gaseous material is supplied to a first zone of a gasifying reactor and is there gasified by a gasifying agent and hot particles separated from the gas, and that the remaining non-gasified material carried by the gas from the first zone is arranged to contact the gasifying agent by supplying the remaining non- gasified material to the solids running down in the spouting type fluidized bed of a second zone, the temperature of which is maintained higher than the temperature of the first zone.
  • a "spouting type" reactor typically has an upward flow in the center and a downward flow of solid material at the periphery.
  • An apparatus for carrying out the method of the present invention is characterized in that the inlet of the particles to be recycled to the reactor and the inlet of the carbonaceous material are located in the lower reactor; that the upper reactor comprises an upward widening portion; and that the inlet/inlets of the gasifying agent of the upper reactor is/are located close to the surface formed by the upward widening portion.
  • the lower reactor is primarily used as a pyrolysis reactor for gasification of volatile particles.
  • Gasification of the remaining coal and tar removal are carried out in a spouting type lower portion of the upper reactor in which lower portion the gas, which contains oxygen and is required for a raise of temperature and the gasification process, and aqueous steam are arranged to contact primarily coal by supplying them to the coal and other circulating material running down in the conical part of the zone.
  • the method of the present invention is based on the use of a reactor (1) of the type wherein solids circulate.
  • the reactor is divided in two regions or zones which are herein referred to as a lower reactor 2 and an upper reactor 3. Between the reactor zones (2, 3) there is a throttle 4 in which the flow velocity of the gas increases thus preventing the circulating material from running from the upper reactor 3 to the lower reactor 2.
  • a bottom portion 5 of the upper reactor is desi ⁇ r.ec " to create a fluidized bed of so called spouting type. This is realized by the widening of the cross section area of the reactor which decreases the velocity of the vertical flow.
  • a bottom portion 6 of the widened portion is conical with an inclination of between 20 and 60 relative the horizontal.
  • the cross sectional area in the upper portion of the upper reactor 3 is reduced to be equal to the cross sectional area of the lower reactor 2.
  • the circulating materials carried by the gas (ash, residual coal, etc.) are separated from the gas in a cyclone separator 7 arranged downstream in the process after the upper reactor 3. From the separator 7 the separated material is returned through a return duct 8 and an inlet 9 down to the lower reactor.
  • Carbonaceous material 10 to be gasified is supplied through an inlet 11 to the lower reactor 2 in which it is gasified at a low temperature, preferably 700 to 900 C, by means of the hot particles separated from the gas and by means of gasifying agent 13 supplied to the reactor through orifices 12 in a bottom plate.
  • Oxygen-containing gas such as air, and possibly steam is - used as the gasifying agent.
  • the temperature of the gas is chosen so as to produce a low coal conversion in the gasification and gas of rather a high tar content.
  • the amount of coal in the lower reactor is regulated by supplying, if required, steam with the oxygen-containing gas and by changing the gasifying temperature.
  • the primary function of the lower reactor is to serve as a pyrolysis reactor for the gasifying substances contained in the carbonaceous material supplied to the reactor. Further, partial oxidation of the fuel to be gasified can also be carried out in the lower reactor.
  • a mixture of fuel containing coal and tarry substances flows from the lower reactor through the throttle 4 to the upper reactor.
  • the purpose of using a spouting type fluidized bed is to raise the reaction temperature to 900 to 1100 C by adding oxygen-containing gas and steam so as to cause the oxygen-containing gas and thesteam to react primarily with the coal and not with the gas.
  • a zone is created in the upper reactor in which zone the coal concentration of the gas is remarkably higher than the average.
  • This kind of a fluidized bed typically has an upward flow in the center and a downward flow of solid material at the periphery.
  • a layer of downwardly running solids builds up in the conical portion 6 at the bottom of the upper reactor. This layer is rich in coal.
  • Oxygen-containing gas and steam 14 are supplied through inlets 15 to this layer of solid material running down along surface 16, whereby the gas and the steam react with the coal contained in the layer and thus raise the temperature as desired.
  • the supply of steam causes an endothermic reaction which reduces the temperature and this must be compensated for by supplying the oxygen-containing gas.
  • the use of steam improves the gasification of coal. Removal of tar is based on the rise in temperature, i.e. thermal dis ⁇ integration.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Industrial Gases (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Investigating Or Analysing Biological Materials (AREA)
  • Medicines Containing Material From Animals Or Micro-Organisms (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Method of gasifying carbonaceous material in two phases in a circulating fluidized bed reactor. Carbonaceous material is supplied to the first zone (2) of a gasifying reactor (1) and is gasified there by means of a gasifying agent and hot particles separated from the gas exhausted from the reactor. The non-gasified material carried by the gas from the first zone is arranged to contact the gasifying agent (14) by supplying it to a layer of solids running down in a spouting type fluidized bed in the second zone of the gasifying reactor, in which zone a higher temperature is maintained than in the first zone.

Description

METHOD AND APPARATUS FOR GASIFYING CARBONACEOUS MATERIAL
Technical field:
The present invention relates to a method for gasification of carbonaceous material in two phases in a circulating fluidized bed reactor in which solid particles contained in gases exhausted from the reactor are separated and recycled to the reactor. The invention also relates to an apparatus for carrying out the method.
It is an object of the invention to provide a method and an apparatus for producing gas of low tar content by utilizing fluidized bed technology for gasification of a carbonaceous material such as coal, brown coal or peat.
Prior art:
Two-staged gasification is . known technology. The so called HT gasifier (Hochtemperatur-Winkler) could be mentioned as an example. In an apparatus of this kind the gasifying agent of the second phase is, however, supplied "unselected" directly to the gasified mixture which, in addition to coal and tarry substances, contains gases (hydrogen, carbon monoxide, methane) which are the desired end products of the gasification process. Oxygen then reacts primarily with these gaseous substances although a reaction with the coal would be advantagous for the product of the gasification. Contact of the coal and the supplied aqueous steam also decreases which results in an incomplete coal conversion and low grade gas.
British patent specification number 1506729 discloses a method of gasifying carbonaceous material in a circulating fluidized bed reactor which is devided into two parts and in which the carbonaceous material is supplied to the upper part of a gasification reactor. When the first stage of the gasification, for example pyrolyses of the volatiles, during which pyrolysis for example tarry substances build up, takes place in the upper part of the reactor, the tarry substances remain in the product gas. The amount of these tarry substances depends on the gasified material and the gasification temperature and it may, e.g. in case of coal, be small. The object of this prior method does not primarily seem to be to produce gas of low tar content either but to achieve an as good a coal coversion as possible. The primary object of the present invention, on the other hand, is to produce gas containing as little tar as possible. Thus the upper part of the reactor is used for removing tar by raising the temperature. An essential feature is that the temperature is increased by combusting coal and not gaseous components. To achieve this, a spouting type fluidized bed is used.
Finnish patent specification number 62554 discloses a two- staged gasification method, in which the beginning of. the gasification process is carried out in the upper part of the reactor, as in the method of GB 1506729 mentioned above, and the tarry substances remain in the product σas.
Disclosure of invention:
The present invention is characterized in that gaseous material is supplied to a first zone of a gasifying reactor and is there gasified by a gasifying agent and hot particles separated from the gas, and that the remaining non-gasified material carried by the gas from the first zone is arranged to contact the gasifying agent by supplying the remaining non- gasified material to the solids running down in the spouting type fluidized bed of a second zone, the temperature of which is maintained higher than the temperature of the first zone. A "spouting type" reactor typically has an upward flow in the center and a downward flow of solid material at the periphery. An apparatus for carrying out the method of the present invention is characterized in that the inlet of the particles to be recycled to the reactor and the inlet of the carbonaceous material are located in the lower reactor; that the upper reactor comprises an upward widening portion; and that the inlet/inlets of the gasifying agent of the upper reactor is/are located close to the surface formed by the upward widening portion.
In the method of the present invention the lower reactor is primarily used as a pyrolysis reactor for gasification of volatile particles. Gasification of the remaining coal and tar removal are carried out in a spouting type lower portion of the upper reactor in which lower portion the gas, which contains oxygen and is required for a raise of temperature and the gasification process, and aqueous steam are arranged to contact primarily coal by supplying them to the coal and other circulating material running down in the conical part of the zone.
Breif Description of the Drawing:
The invention is described further, by way of example, with reference to the attached drawing which is a schematic illustration of a fluidized bed reactor.
Best Mode of Carrying out the Invention:
The method of the present invention is based on the use of a reactor (1) of the type wherein solids circulate. The reactor is divided in two regions or zones which are herein referred to as a lower reactor 2 and an upper reactor 3. Between the reactor zones (2, 3) there is a throttle 4 in which the flow velocity of the gas increases thus preventing the circulating material from running from the upper reactor 3 to the lower reactor 2. A bottom portion 5 of the upper reactor is desiσr.ec" to create a fluidized bed of so called spouting type. This is realized by the widening of the cross section area of the reactor which decreases the velocity of the vertical flow. A bottom portion 6 of the widened portion is conical with an inclination of between 20 and 60 relative the horizontal.
The cross sectional area in the upper portion of the upper reactor 3 is reduced to be equal to the cross sectional area of the lower reactor 2. The circulating materials carried by the gas (ash, residual coal, etc.) are separated from the gas in a cyclone separator 7 arranged downstream in the process after the upper reactor 3. From the separator 7 the separated material is returned through a return duct 8 and an inlet 9 down to the lower reactor.
Carbonaceous material 10 to be gasified is supplied through an inlet 11 to the lower reactor 2 in which it is gasified at a low temperature, preferably 700 to 900 C, by means of the hot particles separated from the gas and by means of gasifying agent 13 supplied to the reactor through orifices 12 in a bottom plate. Oxygen-containing gas, such as air, and possibly steam is - used as the gasifying agent. The temperature of the gas is chosen so as to produce a low coal conversion in the gasification and gas of rather a high tar content. The amount of coal in the lower reactor is regulated by supplying, if required, steam with the oxygen-containing gas and by changing the gasifying temperature. The primary function of the lower reactor is to serve as a pyrolysis reactor for the gasifying substances contained in the carbonaceous material supplied to the reactor. Further, partial oxidation of the fuel to be gasified can also be carried out in the lower reactor.
A mixture of fuel containing coal and tarry substances flows from the lower reactor through the throttle 4 to the upper reactor. The purpose of using a spouting type fluidized bed is to raise the reaction temperature to 900 to 1100 C by adding oxygen-containing gas and steam so as to cause the oxygen-containing gas and thesteam to react primarily with the coal and not with the gas. Thus a zone is created in the upper reactor in which zone the coal concentration of the gas is remarkably higher than the average. This kind of a fluidized bed typically has an upward flow in the center and a downward flow of solid material at the periphery. A layer of downwardly running solids builds up in the conical portion 6 at the bottom of the upper reactor. This layer is rich in coal. Oxygen-containing gas and steam 14 are supplied through inlets 15 to this layer of solid material running down along surface 16, whereby the gas and the steam react with the coal contained in the layer and thus raise the temperature as desired. The supply of steam causes an endothermic reaction which reduces the temperature and this must be compensated for by supplying the oxygen-containing gas. The use of steam, on the other hand, improves the gasification of coal. Removal of tar is based on the rise in temperature, i.e. thermal dis¬ integration.
The following conditions are appropriate for the operation of the method and apparatus according to the invention.
Flow velocity range of the gasifier:
- lower reactor 3 to 10 m/s
- throttle between the lower and the upper reactor 10 to 15 m/s
- spouting portion of the upper reactor 1 to 4 m/s
- upper portion of the upper reactor 4 to 12 m/s Pressure in the gasifier (absolute) 1 to 6 bar
The invention is not to be limited to the embodiments described here but it can be modified and applied within the scope of protection defined by the appended claims.

Claims

Claims :
1. A method of gasifying carbonaceous material in two stages in a fluidized bed reactor, in which particles contained in gases exhausted from the reactor are separated and recycled to the reactor, characterized in that the carbonaceous material is supplied to a first zone of the gasifying fluidized bed reactor and is gasified there by means of a gasifying agent and hot particles previously separated from the exhausted gases; and that the remaining non-gasified material carried by gas from the first zone is caused to contact a gasifying agent by supplying it to the downwardly-running solids in a spouting type fluidized bed of a second zone in the gasifying reactor, in which zone a higher temperature is maintained than in the first zone.
2. A method as claimed .in claim 1, characterized in that the temperature in the first zone is 700 to 900 C.
3. A method as claimed in claim 1 or 2, characterized in that the temperature in the second zone is 900 to 1100 C.
4. A method as claimed in claim 1, 2 or 3, characterized in that the gasifying agent comprises oxygenous gas and aqueous steam.
5. A method as claimed in any of claims 1 to 4, characterized in that the velocity of the gas flowing from the first zone to the second zone is maintained high enough to prevent the solid material from running from the second zone to the first zone.
6. A method as claimed in any of claims 1 to 5, characterized in that the velocity of the gas in the first zone is 3 to 10 m/s.
7. A method as claimed in any of claims 1 to 6 , characterized in that the velocity of the gas in the spouting portion of the second zone is 1 to 4 m/s.
8. A method as claimed in claim 7, characterized in that the velocity of the gas in the inlet of the second zone is 10 to 15 m/s.
9. A fluidized bed reactor for gasifying carbonaceous material, comprising means (7) for separating particles entrained by the gas exhausted from the reactor; means (8) for recycling the separated particles to the reactor; a lower reactor (2) and an upper reactor (3) and means (inlets 11, 15) for inlet of gasifying agent into said reactors (2, 3) , characterized in that the inlets (9, 11) for the particles to be recycled to the reactor and for the carbonaceous material are located in the lower reactor (2) ; and in that the upper reactor (3) comprises a portion (6) which widens or increases in cross-section in an upward direction; and that the inlet/ inlets (15) for the gasifying agent in the upper reactor are located close to the surface (16) provided by the upwardly widening portion.
10. A fluidized bed reactor as claimed in claim 9, characterized in that the bottom (6) of the upper reactor (3) is conical.
11. A fluidized bed reactor as claimed in claim 10, characterized in that the inclination of the bottom (6) in relation to a horizontal level is between 20 and 60 .
12. A fluidized bed reactor as claimed in claim 9, characterized in that the inlet/inlets (15) for the gasifying agent in the upper reactor (3) are arranged to supply oxidizing gas downwards in the direction of the surface (16) of the upwards widening portion.
13. A fluidized bed reactor as claimed in any of claims 8 to
12, characterized in that the cross sectional area of the portion (4) connecting the upper reactor (3) to the lower reactor (2) is smaller than the cross sectional area of the lower reactor (2) .
14. A fluidized bed reactor as claimed in any of claims 1 to
13, characterized in in that the cross sectional area of the widened portion (5) of the. upper reactor (3) is larger than the cross sectional area of the lower reactor (2) .
PCT/FI1987/000011 1986-01-22 1987-01-21 Method and apparatus for gasifying carbonaceous material WO1987004453A1 (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
DE8787900821T DE3781680T2 (en) 1986-01-22 1987-01-21 METHOD AND DEVICE FOR VOLATIFYING CARBONATED MATERIALS.
AT87900821T ATE80412T1 (en) 1986-01-22 1987-01-21 METHOD AND APPARATUS FOR THE VOLATILATION OF CARBON CONTAINING MATERIALS.
JP62500728A JPH0668108B2 (en) 1986-01-22 1987-01-21 Gasification method and equipment for carbonaceous material
KR8770859A KR900004526B1 (en) 1986-01-22 1987-09-22 Method and apparatus for gasifying cabonaceous material

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FI860299A FI80066C (en) 1986-01-22 1986-01-22 Process and apparatus for gasification of carbonaceous material
FI860299 1986-01-22

Publications (1)

Publication Number Publication Date
WO1987004453A1 true WO1987004453A1 (en) 1987-07-30

Family

ID=8522009

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI1987/000011 WO1987004453A1 (en) 1986-01-22 1987-01-21 Method and apparatus for gasifying carbonaceous material

Country Status (9)

Country Link
US (1) US4799937A (en)
EP (1) EP0290450B1 (en)
JP (1) JPH0668108B2 (en)
KR (1) KR900004526B1 (en)
AT (1) ATE80412T1 (en)
CA (1) CA1268338A (en)
DE (1) DE3781680T2 (en)
FI (1) FI80066C (en)
WO (1) WO1987004453A1 (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4987115A (en) * 1987-09-25 1991-01-22 Michel Kim Herwig Method for producing generator gas and activated carbon from solid fuels
WO1992000801A1 (en) * 1990-07-13 1992-01-23 A. Ahlstrom Corporation Method and apparatus for treating gases and/or solid material in a circulating fluidized bed reactor
EP0534243A1 (en) * 1991-09-25 1993-03-31 Hismelt Corporation Pty. Limited A method and apparatus for treating gases and particulate solids in a fluid bed
US8398729B2 (en) 2005-12-15 2013-03-19 General Electric Company Gasification systems for partial moderator bypass
CN103952186A (en) * 2014-04-30 2014-07-30 浙江大学 Downdraft gasifier with tar degrading function

Families Citing this family (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL8902738A (en) * 1989-11-06 1991-06-03 Kema Nv METHOD AND APPARATUS FOR PERFORMING CHEMICAL AND / OR PHYSICAL REACTIONS
US5145490A (en) * 1990-08-09 1992-09-08 Crs Sirrine Engineers, Inc. Process for fixed bed coal gasification
US5133780A (en) * 1990-08-09 1992-07-28 Crs Sirrine Engineers, Inc. Apparatus for fixed bed coal gasification
FI89944C (en) * 1990-12-21 1993-12-10 Ahlstroem Oy Method and apparatus for controlling the temperature of a reactor with circulating fluidized bed
US5622677A (en) * 1991-10-28 1997-04-22 Shell Oil Company Venturi riser reactor and process for catalytic cracking
CA2132689C (en) * 1993-09-28 1998-02-03 David A. Stats Two stage carbonizer
US5641327A (en) * 1994-12-02 1997-06-24 Leas; Arnold M. Catalytic gasification process and system for producing medium grade BTU gas
DE19836428C2 (en) * 1998-08-12 2000-07-13 Siempelkamp Guss Und Anlagente Processes and devices for gasifying biomass, in particular wood materials
NL1016411C2 (en) * 2000-10-16 2002-04-18 Stichting Energie Method and device for gasifying biomass.
DE102007006981B4 (en) * 2007-02-07 2009-01-29 Technische Universität Bergakademie Freiberg Process, gasification reactor and plant for entrained flow gasification of solid fuels under pressure
NL2000520C2 (en) * 2007-03-05 2008-09-08 Stichting Energie Device for manufacturing a product gas from a fuel, such as biomass.
DE102008014799A1 (en) * 2008-03-18 2009-09-24 Karl-Heinz Tetzlaff Process and apparatus for producing synthesis gas from biomass
DE102008032166A1 (en) * 2008-07-08 2010-01-14 Karl-Heinz Tetzlaff Process and device for the production of tar-free synthesis gas from biomass
US20140209447A1 (en) * 2011-09-01 2014-07-31 Guradoor, S.L. Gasification-pyrolysis dual reactor device
US10738249B2 (en) 2012-01-30 2020-08-11 Aries Gasification, Llc Universal feeder for gasification reactors
US20180094199A1 (en) * 2012-01-30 2018-04-05 Aries Gasification, Llc Burner nozzle with backflow prevention for a fluidized bed biogasifier
US20150315498A1 (en) * 2012-12-18 2015-11-05 Long Wu Improved coal gasification
FI125951B (en) * 2012-12-20 2016-04-29 Amec Foster Wheeler En Oy Method for controlling a gasifier with circulating fluidized bed
KR101480503B1 (en) * 2012-12-26 2015-01-12 주식회사 포스코 Coal gasification device and method for coal gasification

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2312283A1 (en) * 1972-03-23 1973-10-11 Bituminous Coal Research TWO-STAGE GASIFICATION OF COAL WITH FORCED MIXING OF THE REACTION PARTIES
GB1506729A (en) 1974-07-03 1978-04-12 Mitsubishi Heavy Ind Ltd Apparatus for gasifying carbonaceous matter
GB2065162A (en) * 1979-11-23 1981-06-24 Carbon Gas Tech Gmbh Apparatus and process for the gasification of carboniferous material
GB2086411A (en) * 1980-10-27 1982-05-12 British Gas Corp Efg process

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1913968A (en) * 1928-02-09 1933-06-13 Ig Farbenindustrie Ag Fuel gas
US2786280A (en) * 1954-03-12 1957-03-26 Ca Nat Research Council Method of contacting solid particles with fluids
DE2640180B2 (en) * 1976-09-07 1980-10-23 Projektierung Chemische Verfahrenstechnik Gmbh, 4030 Ratingen Method and device for gasifying solid fuels
DE2742222C2 (en) * 1977-09-20 1987-08-20 Carbon Gas Technologie GmbH, 4030 Ratingen Method and device for generating gas from solid fuels in a fluidized bed
JPS5842233B2 (en) * 1980-02-19 1983-09-17 通商産業大臣 Two-stage fluidized coal gasification method
US4704138A (en) * 1982-12-06 1987-11-03 Atlantic Richfield Company Spouted bed heating of solids for coal gasification

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2312283A1 (en) * 1972-03-23 1973-10-11 Bituminous Coal Research TWO-STAGE GASIFICATION OF COAL WITH FORCED MIXING OF THE REACTION PARTIES
GB1506729A (en) 1974-07-03 1978-04-12 Mitsubishi Heavy Ind Ltd Apparatus for gasifying carbonaceous matter
GB2065162A (en) * 1979-11-23 1981-06-24 Carbon Gas Tech Gmbh Apparatus and process for the gasification of carboniferous material
GB2086411A (en) * 1980-10-27 1982-05-12 British Gas Corp Efg process

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4987115A (en) * 1987-09-25 1991-01-22 Michel Kim Herwig Method for producing generator gas and activated carbon from solid fuels
US5089030A (en) * 1987-09-25 1992-02-18 Michel Kim Herwig Apparatus for producing generator gas and activated carbon from solid fuels
WO1992000801A1 (en) * 1990-07-13 1992-01-23 A. Ahlstrom Corporation Method and apparatus for treating gases and/or solid material in a circulating fluidized bed reactor
AU655930B2 (en) * 1990-07-13 1995-01-19 A. Ahlstrom Corporation Method and apparatus for treating gases and/or solid material in a circulating fluidized bed reactor
EP0534243A1 (en) * 1991-09-25 1993-03-31 Hismelt Corporation Pty. Limited A method and apparatus for treating gases and particulate solids in a fluid bed
US8398729B2 (en) 2005-12-15 2013-03-19 General Electric Company Gasification systems for partial moderator bypass
CN103952186A (en) * 2014-04-30 2014-07-30 浙江大学 Downdraft gasifier with tar degrading function
CN103952186B (en) * 2014-04-30 2015-07-29 浙江大学 There is the down-draft type gasifying furnace of tar degradation function

Also Published As

Publication number Publication date
FI80066B (en) 1989-12-29
FI860299A0 (en) 1986-01-22
EP0290450A1 (en) 1988-11-17
EP0290450B1 (en) 1992-09-09
US4799937A (en) 1989-01-24
KR900004526B1 (en) 1990-06-29
ATE80412T1 (en) 1992-09-15
JPH01501395A (en) 1989-05-18
FI80066C (en) 1991-07-29
DE3781680T2 (en) 1993-03-25
DE3781680D1 (en) 1992-10-15
FI860299A (en) 1987-07-23
KR880700850A (en) 1988-04-12
CA1268338A (en) 1990-05-01
JPH0668108B2 (en) 1994-08-31

Similar Documents

Publication Publication Date Title
US4799937A (en) Method and apparatus for gasifying carbonaceous material
US4400181A (en) Method for using fast fluidized bed dry bottom coal gasification
EP0007807B1 (en) A method of gasifying an ash-containing fuel in a fluidized bed
US4166786A (en) Pyrolysis and hydrogenation process
EP1606370B1 (en) Method for producing synthesis gas
US4162959A (en) Production of hydrogenated hydrocarbons
EP1348011B1 (en) Multi-faceted gasifier and related methods
EP0027280A1 (en) Process and apparatus for the conversion of agglomerating hydrocarbonaceous solid material to a more valuable gaseous product
US4696678A (en) Method and equipment for gasification of coal
US4243489A (en) Pyrolysis reactor and fluidized bed combustion chamber
US4312638A (en) Coal gasification process
US5213587A (en) Refining of raw gas
JP2011522084A (en) Two-stage high-temperature preheating steam gasifier
US5895508A (en) Down-flow moving-bed gasifier with catalyst recycle
US4578175A (en) Combined process for coal pyrolysis and char gasification
US3876392A (en) Transfer line burner using gas of low oxygen content
US3847566A (en) Fluidized bed gasification process with reduction of fines entrainment by utilizing a separate transfer line burner stage
US4118201A (en) Production of low sulfur fuels from coal
GB1529849A (en) Integrated coal hydrocarbonization gasification and combustion process
US3993583A (en) Gasification of ash containing carbonaceous solids
JP2003171675A (en) Liquid fuel synthesis system
CA1194696A (en) Ash removal and synthesis gas generation from coal
KR100208654B1 (en) Reactor for gasification
JPS5832196B2 (en) Coal gasification method
CA1086672A (en) Pyrolysis of carbonaceous material

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): JP KR US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE FR GB IT LU NL SE

WWE Wipo information: entry into national phase

Ref document number: 1987900821

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 1987900821

Country of ref document: EP

WWG Wipo information: grant in national office

Ref document number: 1987900821

Country of ref document: EP