EP0050863A1 - Procédé et appareil pour gazéifier des charbons - Google Patents

Procédé et appareil pour gazéifier des charbons Download PDF

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Publication number
EP0050863A1
EP0050863A1 EP81108825A EP81108825A EP0050863A1 EP 0050863 A1 EP0050863 A1 EP 0050863A1 EP 81108825 A EP81108825 A EP 81108825A EP 81108825 A EP81108825 A EP 81108825A EP 0050863 A1 EP0050863 A1 EP 0050863A1
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EP
European Patent Office
Prior art keywords
gasifying
combustion
section
reaction
coals
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.)
Withdrawn
Application number
EP81108825A
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German (de)
English (en)
Inventor
Hiroshi Miyadera
Shuntaro Koyama
Tomohiko Miyamoto
Junichi Tomuro
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Hitachi Ltd
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Hitachi Ltd
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Filing date
Publication date
Priority claimed from JP15116280U external-priority patent/JPS5774949U/ja
Priority claimed from JP56024315A external-priority patent/JPS57139184A/ja
Application filed by Hitachi Ltd filed Critical Hitachi Ltd
Publication of EP0050863A1 publication Critical patent/EP0050863A1/fr
Withdrawn legal-status Critical Current

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    • 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
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • 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
    • 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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C10J3/845—Quench rings
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • C10J2300/093—Coal
    • 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
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0976—Water as steam

Definitions

  • This invention relates to a process of and an apparatus for gasifying coals, wherein coals are converted and separated into combustible gas, e.g. hydrogen or carbon oxide, and molten ashes (slags).
  • combustible gas e.g. hydrogen or carbon oxide
  • slags molten ashes
  • Coals are one of fossil fuel resources with the maximum estimated amount of deposits and increasing public attention as an alternative energy in place of petrol.
  • coals are inconvenient in their treatment because they are solid fuels and require counter measures to prevent environment contamination because they contain ashes, sulphur and nitrogen.
  • Gasification of coals is one prospective method for converting coals into clear fuels, so that coal gas for consumption, fuel gas for industries, raw gas for technical chemistry and hydrogen gas for oil refining or coals gasifying and also the conversion into fuel gas for the power generation by gas turbines may be produced.
  • Reactions caused in the process of such coal gasiri- cation are mainly divided into three reactions; i.e. a combustion reaction between coals and oxidizing agents (air, oxygen), a dry distillation reaction of coals by heat produced during the combustion, and a gasifying reaction between chars (solid substances containing carbon and ashes) as a residual component of the dry distillation and steam or carbon dioxide.
  • the gasifying reaction among those reactions is represented by the following Equations (1) and (2), and combustible gas such as hydrogen or carbon oxide is produced in larger amounts as the temperature is increased up to a higher degree.
  • Methods of gasifying coals are basically grouped into a fixed bed system, a fluidized bed system, a jet stream bed system and a molten bath bed system. This grouping is based on the state of the coal particles within furnaces, but also closely related to a diameter of the particles and temperature in the furnaces.
  • the fixed bed systems has the disadvantage that the reaction velocity is low because of massive coals with a diameter of several tens mm and this leads to limitations in the processing capacity, whereby the system is not suitable for a large scale plant.
  • positive achievements have been accumulated for this system up to now, so that gasification furnaces of the fixed bed type are adopted in most plants in the present condition.
  • coal particles with a diameter equal to or less than several mm are gasified while being fluidized by the action of gas. Therefore, the furnace temperature becomes uniform in its distribution due to the fact that the coal particles agitate air bubbles, whereby the generation of tars often experienced in the fixed bed system is restricted to a low level, so that a high efficiency of the gasifying reaction can be obtained.
  • the generation of clinkers due to the solidification of molten ashes has to be restricted, it is difficult to raise the furnace temperature above 950°C and the gasifying reaction is limited in its velocity.
  • coal particles are atomized to a still smaller diameter and gasified by a gasifying agent and ashes are molten at a high temperature above 1300°C, so that discharged ashes include a lower content of parts not yet burnt and the gasification velocity becomes extremely high with little amount of tar byproducts.
  • the former system (1) has an advantage in that slags can be prevented from adhering to the inner wall of the furnace, but disadvantage in that the recovery of the released gas heat is difficult because the generated gas and slags are introduced into warm water for cooling.
  • the latter system (2) has an advantage in that the released heat of the generated gas can be recovered with ease, but drawbacks in that the dropping ratio of the slags becomes low because of a tendency to flow upward together with the generated gas, and ashes can be hardly molten due to limitations on the furnace structure when gasifying coals containing ashes with high melting temperature.
  • Reactions caused in the process of coal gasification are mainly divided into three reactions; i.e. dry distillation, gasifying and combustion reactions.
  • dry distillation reaction volatile components are formed and combustible gas such as methane, hydrogen, carbon oxide, or others is generated.
  • gasifying reaction chars as a residual component of the dry distillation react with steam or carbon dioxide to generate hydrogen or carbon oxide. These reactions go on in the form of an endothermic reaction and the required heat source is obtained through combustion of the chars.
  • these three reactions are performed, and effective coal gasification can be obtained only when the three reactions proceed at the optimum ratio therebetween.
  • the invention aims at controlling the amount of the combustion reaction determining the temperature and at adjusting the amount of raw coals supplied to the combustion reaction section with the coal gasification apparatus for that control.
  • a gasification method comprising a process for gasifying fine coal particles by supplying coals pulverized to particles into a high temperature atmosphere together with a gasifying agent, a process for separating combustible gas and chars generated in the gasifying process, and a process for burning the chars separated in the separating process, wherein- the fine coal particles and the gasifying agent are supplied while burning the chars.
  • the fine coal particles are preferably controlled in their amount in response to the reaction temperature when burning the chars.
  • a gasificr for realizing the gasification method of the present invention comprises a gasification means including a dry distillation gasifying reaction section at the upper side and a combustion gasifying section, a separation means for separating combustible gas and chars generated in the gasification means a means for supplying the chars separated in the separation means to the combustion gasifying section in the gasification means, and a means for supplying fine coal particles and gasifying agents to both the dry distillation gasifying reaction section and the combustion gasifying section in the gasification means.
  • an advantage has been achieved in that the chars are burned at a temperature not below the dropping point of the molten ashes contained in the chars irrespective of varieties - of coals and thus all varieties of coals can be gasified effectively and stably.
  • a gasifier 1 includes a dry distillation (thermal decomposition) gasifying reaction section 2 at the upper side, a combustion gasifying section 3 at the lower side and a molten ash pot section 4 at the bottom, respectively. Throttled portions 17, 1 8 are formed between these three sectiones 2 to 4 to increase the combustion efficiency in the combustion gasifying section 3.
  • ports 5A and 5B for supplying raw coals and a gasifying agent (an oxidizing agent, steam or a gas mixture thereof), to the combustion gasifying section 3 connected are ports 6A and 6B for supplying raw coals and a gasifying agent and ports 7 for resupplying by-producted chars, respectively.
  • Each port 6A formed in the combustion gasifying section 3 for supplying raw coals is opened in the tangential direction of the combustion gasifying section 3 as described hereinafter and radially faces the port 7 for resupplying chars with an angular interval of 180°.
  • a cooling water supply port 8 and a cooling water exhaust port 9 are connected to the molten ash pot section 4.
  • a cooler 11 and a cyclone 12 are connected to a . outlet tube 10 for leading out the generated gas and chars, the latter tube 10 being connected to the top of the gasifier 1.
  • the leg portion of the cyclone 12 is connected.to the port 7 for resupplying the byproducted chars via a transport system comprising a char recycling tube 13 and a char pot 14.
  • An outlet of the cyclone 12 is coupled with a refining system 16 via a gas transport tube 15, so that gas discharged from the cyclone 12 is refined.
  • the refined gas serves directly as a fuel for a gas turbine, while the heat thereof is recovered to increase the efficiency of power generation with the aid of a steam turbine.
  • fine coal particles are supplied to the dry distillation gasifying reaction section 2 through the supply ports 5A with a gasifying agent by a predetermined amount successively.
  • coals are dry-distilled to generate methane, hydrogen, carbon oxide and other components.
  • Byproducted chars move upward in the gasifier 1 by the action of high temperature gas while being under the gasifying action, whereby the content of carbon contained in the chars is reduced.
  • gas generated from the dry distillation and gas and chars generated from the gasifying reaction are led out through the outlet tube 10 to the cooler 11, where they are cooled and the heat thereof is recovered.
  • the chars are separated from the gas in the cyclone 12. Separated chars pass down through the char recycling tube 13 and are stored in the char pot 14. The chars stored in the char pot 14 are supplied to the combustion gasifying section 3 with a gasifying agent by a predetermined amount succsssively.
  • the chars are burnt up so as to produce heat.
  • raw coals and a gasifying agent are supplied to the combustion gasifying section 3 through the supply ports 6A, 6B, so that the temperature within the combustion gasifying section 3 becomes above the melting temperature of ashes due to the combustion reaction of coals.
  • ashes contained in the chars are molten, flow down along the inner wall surface of the combustion gasifying section 3 and then drip into the molten ash pot section 4, where the ashes are cooled by cooling water to be solidified.
  • the solidified ahe.s are discharged out . of the system.
  • the raw coals to the combustion gasifying section 3 For supplying the raw coals to the combustion gasifying section 3, they may be continuously supplied. to the section 3, when the used raw coals generate such chars as contain a smaller amount of combustible components. It is pereferable, however, to detect the temperature within the combustion gasifying section 3 and then adjust the amount of the raw coals supplied to the section 3 by a control unit 19 in response to the temperature condition within the combustion gasifying section 3. According to this system, the process of gasification can be effectively operated even when the raw coals are changed in their varieties during the course of coal gasification.
  • the gasifier comprises a pressure-resistant vessel and is lined with fire-resistant material and heat insulating material at the inner surface.
  • the dry distillation (heat decomposition) gasifying reaction section has an inner diameter of 105 mm and a height of 4.2 m
  • the combustion gasifying section has an inner diameter of 200 mml and a height of 0.4m
  • the both sections are coupled with each other via a throttle tube with an inner.diameter of 50mm.
  • the molten ash pot section having an inner diameter of 300mm and a height of 0.6 m is connected at the upper end thereof to the combustion gasifying section via an another throttle tube with a diameter of 70mm.
  • a heater of fire-resident material at its periphery is provided within the pressure-resistant vessel to accelerate the radiation of heat.
  • Each supply port connected to the dry distillation gasifying reaction section has an inner diameter of 12.7mm and is opened in the tangential direction of that section.
  • the port for supplying raw coals, connected to the combustion gasifying section has an inner diameter of 12.7mm and is opened in the downward tangential direction.
  • the port for resupplying chars to the combustion gasifying section has the same diameter as the port supplying raw coals thereto and is opened in the tangential direction at a position radially facing the latter port with an angular interval of 180°.
  • coals were gasified by supplying Taiheiyo Coal of 14.3 kg/h pulverized to fine particles with diameter not greater than 74 ⁇ m, steam of 6.0 kg/h and air of 37 kg/h to the dry distillation gasifying reaction section, and the same coals of 0.7kg/h and air of 9,5kg/h to the combustion gasifying section.
  • Recycled chars of 5.4 kg/h and air of 21.2 kg/h from the char pot are also supplied to the combustion gasifying section.
  • gas obtained at an outlet of the cyclone was composed of hydrogen 12 vol %, and carbon oxide 20.5 vol %, methane 1.5 vol % and carbon dioxide 8.1vol% and had a calorific power of 4533 kJ/Nm 3 .
  • the temperature within the combustion gasifying section was 1470°C. Ashes were molten in the combustion gasifying section, adhered to the inner wall surface thereof and also dripped into the molten ash pot section.
  • coals of 13kg/h, steam of 6.0kg/h and air of19.2 kg/h were supplied to the dry distillation gasifying reaction section, and the same coals of 2.0kg/h, air. of 27.1kg/h, recycled chars of 5.1 kg/h and air of 21 kg/h were supplied to the combustion gasifying section.
  • Coals were gasified in such conditions.
  • the temperature within the combustion gasifying section raised up to 1630°C, and ashes within the combustion gasifying section dropped down in the molten state and could be collected in the molten ash pot section.
  • the combustion gasifying section was supplided with only recycled char at 5.4 kg/h and air at 2 1.2kg/h without coals, and the dry distillation (thermal decomposition) gasifying section was supplied with the same coals as above at 15 kg/h, steam at 6 kg/h and air at 46.3 kg/h.
  • the temperature within the combustion gasifying section was 1280°C, and ashes were hardly adhered to the inner wall surface of the combustion gasification section and not dipped into the molten ash pot section.
  • the combustion gasifying section 3 is shaped into an invert-conical form with a throttled bottom.
  • Raw coals in the pulverized particle form are blown into the combustion gasifying section 3 together with a gasifying agent (oxygen or air and steam) through the nozzles 6A.
  • a gasifying agent oxygen or air and steam
  • the nozzles 6A are disposed in such a manner that the fine coal particles are jetted from the nozzles in the tangential direction of a phantom circle 20 at the furnace wall and the number of nozzles j at each stage i is proportional to the circumferential length of the phantom circle at the same stage.
  • each nozzle 6A is so oriented that the fine coal particles from the nozzle 6A travel downward obliquely and the fine coal particles reflected at the furnace wall travel downward with respect to the horizontal plane.
  • the angle ⁇ of the nozzle 6A against the horizontal plane is set to be not smaller than the vertical angle ⁇ of the invert-conical-shaped furnace, as illustrated in Fig.2(a).
  • thejet stream of the gasifying agent and fine coal particles from the nozzles 6A, 6'A becomes a whirling stream 21, 21' towarding the bottom of the furnace so that the coal particles collide hard with gas and their staying time at high temperature is prolonged, whereby not only the gasification factor can be increased, but also the generated molten ashes 22, 23 collide with the furnace wall 18 and then drip into water 24 within the molten ash pot section 4.
  • an invert-conical-shaped gasification furnace constituting the combustion gasifying section 3 has a vertical angle of 20°, an inner diameter of 900mm at the upper end and an inner diameter of 300mm at the lower end.
  • a plurality of nozzles at three stages, the upper stage being located at a level A-A' in the upper portion of the conical-shaped furnace, the middle stage being located at a level B-B' lower 600mm than the level A-A', and the lower stage being located at a level C-C' lower 600mm than the level B-B' .
  • Respective nozzles are directed downward at an angle of 30° with respect to the horizontal plane and disposed in such a manner depending cn each stage that the nozzles on the level A-A' are oriented in the tangential direction of a-phantom circle sectioned at the level B-B', the nozzles on the level B-B' in the tangential direction of a phantom circle sectioned at the level C-C', and the nozzles on the level C-C' in the tangential direction of a phantom circle sectioned at a level D-D' lower 600 mm than the level C-C', respectively.
  • the velocity of the gas jet from each nozzle is set not less than 50m/s, preferably not less than 150m/s, and the aperture diameter of and the injection angle from the nozzles are so selected that the running speed at the phantom circles mentioned above becomes not less than 5m/s, preferably not less than 20m/s, thereby producing a satisfactory whirling stream.
  • the nozzles at the A and B stages are used for supplying coals and the nozzles at the C stage are used for resupplying the chars recovered from the cyclone.
  • the generated gas had a temperature of 960 C at the outlet of the gasification furnace and was composed of H 2 13.8 vol%, CO 24.2 vol%, C0 2 5.5 vol%, H 2 S 0.2 vol% and N 2 56.3 vol%.
  • the calorific power, carbon gasified rate and energy yield (cooling gas efficiency) of the generated gas were 4856 kJ/Nm 3 , 992% and 75%, respectively.
  • the total amount of supplied coals was lowered to 60% of the above rated value by interrupting the supply of coals from the nozzles at the B stage while maintaining the supply from the nozzles at the A stage at the rated value (100%, 49 kN/h).
  • a stable stream of slags was formed, because the whirling stream from the nozzles at the A stage was kept at nearly the same one as generated under the rated state.
  • the supply amount from those nozzles reduced to 60% of the rated value has also resulted in the phenomenon that a stable formation of a slag stream is 'prevented. Therefore, it becomes possible to maintain the stable operation in a range from 60 to 36% of the total processing amount corresponding to the rated state by using the nozzles at the A stage only.
  • the amount of supplied coals was lowered to 40% of the rated value by interrupting the supply of coals from the nozzles at the A stage while keepting the supply amount from the nozzles at the B stage at its raged value (49 kN/h for each nozzle). In this case, operation was performed at the sufficiently stable state.
  • the processing amount by the nozzles at the B stage is reduced to below 60% of the rated value, the slag stream may be also brought into an unstable state. But practical processing can be continued in a range up to 50% of the rated value.
  • each nozzle has a lower limitation at about 60% of the rated value in its allowable fluctuation.
  • the load factor it became possible to change the load factor from 20% to 100% through the combined using of the nozzles at the A and B stages.
  • the gas composition and gas conversion rate which are variable due to the load fluctuation could be maintained at nearly constant level.
  • the lowered load factor leads to a reduction in the flowing speed of the gas within the furnace and the amount of chars recovered from the cyclone is reducted, so that the char supply amount from the nozzle at the C stage is also significantly lowered, whereby the formation of slags may become not easy.
  • solidification of the slag stream is relatively hard to occur, because gasification of the char jet from the nozzles at the C stage is accelerated by slag streams from the nozzles at the A and B stages.
  • multi-stage nozzles are provided at the gasifying section in the form of an inverted cone, the number of nozzles at each stage is made proportional to the circum- ferencial length of a circle sectioned at the level of each stage, and each nozzle is so directed and oriented downward obliquely that the angle of the nozzles with respect to the horizontal plane becomes greater than the vertical angle of the conical-shaped gasifying section, and the nozzles are directed in the tangential direction of a phantom circle in the furnace sectioned horizontally, thereby permitting to maintain dripping of molten ashes, increase the gasification efficiency and achieve stable gas composition, even when thesupply amount of materials is remarkably changed.
  • Fig.4 The foregoing arrangement as shown in Fig.4 is one embodiment and the present invention is not limited to this embodiment. It is a matter of course that the vertical angle of the conical-shaped gasifying section can be changed, and the number'of nozzles and orientation thereof can be also varied. Furthermore, raw coals can be supplied not only dry but also in the form of water slurry, and oxgen or steam can be used as a gasifying agent in place of air.
EP81108825A 1980-10-24 1981-10-23 Procédé et appareil pour gazéifier des charbons Withdrawn EP0050863A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP15116280U JPS5774949U (fr) 1980-10-24 1980-10-24
JP151162/80 1980-10-24
JP24315/81 1981-02-23
JP56024315A JPS57139184A (en) 1981-02-23 1981-02-23 Coal gasification

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EP0050863A1 true EP0050863A1 (fr) 1982-05-05

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EP81108825A Withdrawn EP0050863A1 (fr) 1980-10-24 1981-10-23 Procédé et appareil pour gazéifier des charbons

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2138841A (en) * 1983-03-28 1984-10-31 Hitachi Ltd Coal gasifier and process for gasifying coal
FR2578263A1 (fr) * 1985-03-01 1986-09-05 Skf Steel Eng Ab Procede et dispositif pour la gazeification de combustibles fossiles et le reformage d'un combustible gazeux.
EP0241866A2 (fr) * 1986-04-09 1987-10-21 Hitachi, Ltd. Procédé de gazéification pour un four de gazéification de charbon et appareillage à cet effet
EP0400740A1 (fr) * 1989-05-30 1990-12-05 Shell Internationale Researchmaatschappij B.V. Réacteur de gazéification de charbon
EP0423401A1 (fr) * 1985-11-29 1991-04-24 The Dow Chemical Company Procédé de gazéification de charbon à deux étages
DE3936732A1 (de) * 1989-11-04 1991-05-08 Krupp Koppers Gmbh Verfahren und vorrichtung zur vergasung von feinkoernigen bis staubfoermigen brennstoffen
EP0451265A1 (fr) * 1989-11-02 1991-10-16 United States Department Of Energy Procede d'enrichissement et d'utilisation du charbon
EP0487157A1 (fr) * 1990-11-19 1992-05-27 Shell Internationale Researchmaatschappij B.V. Procédé et dispositif de préparation de gaz de synthèse par oxydation partielle de combustible contenant des particules de carbone finement divisées
EP1489046A1 (fr) * 2001-08-21 2004-12-22 Mitsubishi Materials Corporation Procede et appareil de recyclage de ressources d'hydrocarbures
WO2010096278A3 (fr) * 2009-02-20 2010-12-29 Conocophillips Company Effluent gazeux riche en dioxyde de carbone issu d'un procédé de gazéification en deux étapes
WO2011085088A3 (fr) * 2010-01-07 2011-12-29 General Electric Company Système et procédé de gazéification utilisant des injecteurs de carburant
US8690973B2 (en) 2006-12-14 2014-04-08 Siemens Aktiengesellschaft Entrained flow reactor for gasifying solid and liquid energy sources
US9102882B2 (en) 2012-09-04 2015-08-11 General Electric Company Gasification system and method

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FR2400550A1 (fr) * 1977-08-18 1979-03-16 Combustion Eng Procede d'exploitation d'un appareil a gazeifier le charbon
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GB2138841A (en) * 1983-03-28 1984-10-31 Hitachi Ltd Coal gasifier and process for gasifying coal
FR2578263A1 (fr) * 1985-03-01 1986-09-05 Skf Steel Eng Ab Procede et dispositif pour la gazeification de combustibles fossiles et le reformage d'un combustible gazeux.
EP0423401A1 (fr) * 1985-11-29 1991-04-24 The Dow Chemical Company Procédé de gazéification de charbon à deux étages
EP0241866A2 (fr) * 1986-04-09 1987-10-21 Hitachi, Ltd. Procédé de gazéification pour un four de gazéification de charbon et appareillage à cet effet
EP0241866A3 (en) * 1986-04-09 1988-05-04 Hitachi, Ltd. Gasification process for coal gasification furnace and apparatus therefor
US4806131A (en) * 1986-04-09 1989-02-21 Hitachi, Ltd. Gasification process for coal gasification furnace and apparatus therefor
EP0400740A1 (fr) * 1989-05-30 1990-12-05 Shell Internationale Researchmaatschappij B.V. Réacteur de gazéification de charbon
EP0451265A4 (en) * 1989-11-02 1992-05-06 United States Department Of Energy Coal beneficiation and utilization process
EP0451265A1 (fr) * 1989-11-02 1991-10-16 United States Department Of Energy Procede d'enrichissement et d'utilisation du charbon
EP0431266A1 (fr) * 1989-11-04 1991-06-12 Krupp Koppers GmbH Procédé et appareil pour la gaséification de combustibles finement divisés à poudreux
DE3936732A1 (de) * 1989-11-04 1991-05-08 Krupp Koppers Gmbh Verfahren und vorrichtung zur vergasung von feinkoernigen bis staubfoermigen brennstoffen
EP0487157A1 (fr) * 1990-11-19 1992-05-27 Shell Internationale Researchmaatschappij B.V. Procédé et dispositif de préparation de gaz de synthèse par oxydation partielle de combustible contenant des particules de carbone finement divisées
EP1489046A1 (fr) * 2001-08-21 2004-12-22 Mitsubishi Materials Corporation Procede et appareil de recyclage de ressources d'hydrocarbures
EP1489046A4 (fr) * 2001-08-21 2010-02-24 Mitsubishi Materials Corp Procede et appareil de recyclage de ressources d'hydrocarbures
US8690973B2 (en) 2006-12-14 2014-04-08 Siemens Aktiengesellschaft Entrained flow reactor for gasifying solid and liquid energy sources
US7883682B2 (en) 2009-02-20 2011-02-08 Conocophillips Company Carbon dioxide rich off-gas from a two stage gasification process
WO2010096278A3 (fr) * 2009-02-20 2010-12-29 Conocophillips Company Effluent gazeux riche en dioxyde de carbone issu d'un procédé de gazéification en deux étapes
WO2011085088A3 (fr) * 2010-01-07 2011-12-29 General Electric Company Système et procédé de gazéification utilisant des injecteurs de carburant
US8696774B2 (en) 2010-01-07 2014-04-15 General Electric Company Gasification system and method using fuel injectors
AU2011203614B2 (en) * 2010-01-07 2016-06-09 Air Products And Chemicals, Inc. Gasification system and method using fuel injectors
US9102882B2 (en) 2012-09-04 2015-08-11 General Electric Company Gasification system and method

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