EP3290493B1 - Procédé de la gazéification en lit fixe sous pression - Google Patents

Procédé de la gazéification en lit fixe sous pression Download PDF

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Publication number
EP3290493B1
EP3290493B1 EP16400040.8A EP16400040A EP3290493B1 EP 3290493 B1 EP3290493 B1 EP 3290493B1 EP 16400040 A EP16400040 A EP 16400040A EP 3290493 B1 EP3290493 B1 EP 3290493B1
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EP
European Patent Office
Prior art keywords
ash
reactor
particles
fuel
bed
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.)
Active
Application number
EP16400040.8A
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German (de)
English (en)
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EP3290493A1 (fr
Inventor
Ganesh Arumugam
Nicolas Spiegel
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.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Filing date
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to EP16400040.8A priority Critical patent/EP3290493B1/fr
Priority to PCT/EP2017/025235 priority patent/WO2018041411A1/fr
Priority to CN201721120405.4U priority patent/CN207567181U/zh
Priority to CN201710779718.9A priority patent/CN107794090A/zh
Publication of EP3290493A1 publication Critical patent/EP3290493A1/fr
Application granted granted Critical
Publication of EP3290493B1 publication Critical patent/EP3290493B1/fr
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—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
    • C10J3/02—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
    • C10J3/04—Cyclic processes, e.g. alternate blast and run
    • 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
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1631—Ash recycling
    • 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
    • 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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates

Definitions

  • the invention relates to a process for converting a solid, carbonaceous fuel, such as coal or coke, to a raw synthesis gas mainly comprising hydrogen and carbon monoxide and to ash, using a shaft reactor in which the fuel is arranged as a fixed bed and flows through it continuously, the A gaseous gasifying agent comprising oxygen and steam flows through the fixed bed at elevated pressure and at elevated temperature, and the shaft reactor is filled with fuel via a pressure lock and the ash is discharged from it.
  • the invention also relates to a system for carrying out the method.
  • solid fuel such as coal, coke or other carbonaceous fuel is gasified with steam and oxygen as gasifying agents at elevated temperature and, in most cases, under excess pressure to form a synthesis gas containing carbon monoxide and hydrogen, with solid ash being obtained which over an ash discharge grate, which in many cases is designed as a rotating grate is discharged from the reactor.
  • a particle size distribution has proven to be favorable in which at least 90% by weight of the particles are in a size range from 10 to 50 mm and the remainder is divided equally between the size range above and below.
  • the particle size is determined in accordance with ASTM D4749.
  • the object of the invention is therefore to provide a method which is able to carry out the gasification of carbonaceous fuel in the fixed bed more effectively and to improve the gas flow through the fuel bed.
  • AU 469 916 B2 and GB 1 435 088 A describe processes for the gasification of coal with the return of inert mass to improve the flow behavior of the shaft reactors.
  • a process for converting a solid, carbonaceous fuel, such as coal or coke, to a raw synthesis gas comprising mainly hydrogen and carbon monoxide and to ash using a shaft reactor in which the fuel is arranged as a fixed bed and flows through it continuously, the fixed bed at increased Pressure and at elevated temperature, is flowed through by a gaseous gasifying agent comprising oxygen and steam, and the shaft reactor is filled with the fuel via a pressure lock each and the ash is discharged from it, with part of the discharged ash being returned to the reactor and with the Fuel passes through the fixed bed, characterized in that the ash is sieved off before being returned to the reactor to separate fine and coarse particles, the sieving comprising at least two sieve stages and with decreasing or increasing mesh size and the sieve fr action with medium particle size is at least partially returned to the reactor and the separated particles are fed to a further treatment or use outside of the process .
  • Eleated pressure and “elevated temperature” are understood to mean pressure and temperature values above ambient pressure or room temperature. The person skilled in the art can find suitable pressure and temperature values from the abovementioned literature.
  • the presence of ash particles leads to loosening, ie to gaps that exist uniformly between the particles of the fixed fuel bed and thus enables gasification agent to flow through it more evenly.
  • the pressure drop of the gasification agent is reduced, whereby a larger amount of gasification agent can flow through the fixed bed. Due to the more even distribution and the larger amount of the gasification agent used in the fixed bed, the production capacity of the fixed bed gasification reactor can be increased.
  • the loosening achieved by the ash particles also improves the flowability of the bed of the fixed bed.
  • the tendency of the bed to form bridges at bottlenecks is thus reduced.
  • the outflow of the ash through the annular gap between the rotating grate and the inner wall of the reactor is less disturbed by the formation of bridges in the ash bed.
  • a particular advantage of using the ash particles produced in the gasification process itself is that these particles have already been exposed to the process conditions, in particular the high temperatures, so that they have only a slight tendency to disintegrate when they pass through the fixed bed.
  • the particle size distribution of the returned ash is adjusted to the area that is most suitable for a uniform flow through the bed of solids. This is especially the range of mean grain sizes of the ash particles. Too high a proportion of small particles can block the flow; too high a proportion of large particles can lead to channel formation, i.e. H. to places with particularly low flow resistance. Which size range is most suitable for a specific application must be determined through tests. It depends on the apparatus conditions of the reactor, the adjustable process parameters and, in particular, on the quality of the fuel.
  • a preferred embodiment of the invention is characterized in that the ash discharged from the reactor via the pressure lock is rinsed with water for screening and is separated from the water again when the fine and coarse particles are screened. With this method of transport, the ashes are cooled at the same time.
  • the method does not require any complicated apparatus and is therefore reliable and inexpensive.
  • This method can also be used particularly advantageously when water is scarce, by circulating the water used, passing it through a device for separating fine ash particles, which are discharged for further treatment outside the process.
  • Another preferred embodiment of the invention is characterized in that the water used is circulated, being passed through a device for separating fine ash particles which are discharged for further treatment outside the process. Since the recycled water has already been saturated or partially saturated with water-soluble ash constituents in this way, such dissolution effects are reduced when the water that has already been used is used again. This increases the stability of the ash particles.
  • the fine particles are particles with a size of less than 10 mm, less than 20 mm, less than 30 mm or less than 40 mm and / or as the coarse particles, particles with a size of more than 20 mm, more than 30 mm , over 40 mm or over 50 mm. These sizes are a good starting point for testing to determine which particle size distribution is the most suitable.
  • Another preferred embodiment of the invention is characterized in that the ash is fed to the solid bed up to a proportion of 30% of the mass of the solid bed.
  • the ash in the solid bed improves and evens out the Permeability of the solid bed, on the other hand, it also represents a dead mass for the gasification process, which does not contribute directly to the production of synthesis gas. It therefore makes sense to limit the ash content in the solid bed.
  • Another preferred embodiment of the invention is characterized in that the ash intended for recycling into the reactor is dried.
  • the ash is emptied from the ash lock of the fixed bed reactor into a channel, from which it is rinsed with water for further treatment.
  • the one recorded Moisture is largely separated from the ash when the coarse and fine particles are sieved.
  • it can be useful to dry the ash before returning it to the reactor.
  • a further preferred embodiment of the invention is characterized in that the ash and the fuel provided for return are each conveyed by means of conveying means that generate a material flow and that the two material flows are brought together and the mixed material flow thus formed is filled into the pressure lock or an upstream feed container will.
  • conveying means that generate a material flow
  • the two material flows are brought together and the mixed material flow thus formed is filled into the pressure lock or an upstream feed container will.
  • a suitable alternative to a mixing apparatus is, in each case by suitable means of conveyance, such as. B. conveyor belts, vibrating troughs or pneumatic conveying systems to generate a continuous flow of material, and to merge the fuel and ash flows and combine them into a single, mixed flow; and to introduce this stream into the fuel lock or into a storage container for the fuel lock.
  • suitable means of conveyance such as. B. conveyor belts, vibrating troughs or pneumatic conveying systems to generate a continuous flow of material, and to merge the fuel and ash flows and combine them into a single, mixed flow; and to introduce this stream into the fuel lock or into a storage container for the fuel lock.
  • Fig. 1 comprises the plant 1 comprises a fixed-bed pressure gasification reactor 2 with the pressure lock 3 for charging the reactor with fuel 4, e.g. B. coal, and the pressure lock 5 for discharging the ash 6 produced.
  • the locks can be closed with the closures 7.
  • the fixed fuel bed 8, which rests on the grate 9, is located in the reactor 2.
  • the gasification agents 10 are introduced through the grate 9 into the fixed bed 8 and convert the fuel 4 into raw synthesis gas 11 and ash 6.
  • the raw synthesis gas 11 is discharged from the reactor 2 above the fixed bed 8 for further treatment outside the process.
  • the ash 6 is drained from the lock 5 into the lock channel 12 and fed with water 13 as a water / ash mixture 14 to the two-stage screening device 15.
  • This is equipped with a first sieve 16 for sieving off the ash fine particles and for separating the water from the ash.
  • a size of 10 mm is most suitable, but the sieve 16 should be adjustable in such a way that sizes up to 40 mm can also be sieved off as fine particles.
  • the mixture 17 of fine ash particles and water is discharged from the system 1 for further treatment. It is also possible for the mixture 17 to be passed through a device (not shown) for separating the fine particles from the water, so that the water can be circulated and used again to flush the lock channel.
  • the ash 18 is then passed to a second sieve 20 to screen the coarse ash particles 19.
  • the size of the coarse ash particles screened off can be changed. In many cases a size of 50 mm is most suitable, but the sieve 20 should be adjustable in such a way that sizes down to 20 mm are screened off as coarse particles.
  • the ash 18 can optionally be washed free of ash dust with water 25. The water 25 can be performed in a cycle, not shown, in which it is of the Ash dust is freed.
  • the coarse particles 19 are discharged from the system 1 for further treatment.
  • This device meters and mixes the flows of the fuel 4 and the ash 21 in the desired ratio and fills them as a mixture 24 into the pressure lock 3.
  • the invention provides a method with which the gas flow behavior of a fixed-bed pressure gasification reactor is improved and it can thus be operated with a greater throughput and thus with increased economic efficiency.
  • the invention is therefore advantageously industrially applicable.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Claims (7)

  1. Procédé de transformation d'un combustible solide, contenant du carbone, tel que charbon ou du coke, en un gaz de synthèse brut comprenant principalement de l'hydrogène et du monoxyde de carbone et en cendre, en utilisant un réacteur à puits (2), dans lequel le combustible (4) est agencé sous la forme d'un lit fixe (8) et traverse celui-ci en continu, le lit fixe (8) étant traversé, à pression élevée et à température élevée, par un moyen de gazéification gazeux comprenant de l'oxygène et de la vapeur, et le réacteur à puits (2) étant rempli avec le combustible (4) et la cendre (6) étant déchargée de celui-ci, à chaque fois par l'intermédiaire d'un sas sous pression (3, 5), une partie de la cendre déchargée (6) étant réintroduite dans le réacteur (2) et traversant le lit fixe (8) avec le combustible (4), caractérisé en ce que la cendre (6) est tamisée avant sa réintroduction dans le réacteur (2) pour la séparation de particules fines et. grossières, le tamisage comprenant au moins deux étages de tamis (16, 20) et pouvant avoir lieu à largeur de mailles décroissante ou croissante, et la fraction de tamisage ayant une taille de particule intermédiaire (21) étant au moins partiellement réintroduite dans le réacteur (2), et les particules séparées (17, 19) étant acheminées vers un traitement supplémentaire ou une utilisation en dehors du procédé.
  2. Procédé selon la revendication 1, caractérisé en ce que la cendre (6) déchargée du réacteur par l'intermédiaire du sas sous pression (5) est rincée avec de l'eau pour le tamisage et est séparée de l'eau pendant ou après le tamisage des particules fines et grossières.
  3. Procédé selon la revendication 2, caractérisé en ce que l'eau utilisée est mise en circulation, celle-ci passant par un dispositif pour la séparation de particules fines de cendre, qui sont déchargées pour le traitement supplémentaire en dehors du procédé.
  4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que des particules ayant une taille inférieure à 10 mm, inférieure à 20 mm, inférieure à 30 mm ou inférieure à 40 mm sont tamisées en tant que particules fines et/ou des particules ayant une taille supérieure à 20 mm, supérieure à 30 mm, supérieure à 40 mm ou supérieure à 50 mm sont tamisées en tant que particules grossières.
  5. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la fraction de cendre (21) réintroduite dans le réacteur est acheminée vers le lit de solides (8) jusqu'à une proportion de 30 % de la masse du lit de solides (8).
  6. Procédé selon la revendication 5, caractérisé en ce que la cendre destinée à être réintroduite dans le réacteur (2) est séchée avant l'acheminement vers le lit de solides (8).
  7. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que la cendre prévue pour être réintroduite et le combustible sont chacun transportés au moyen de moyens de transport, qui génèrent un flux de matière, et en ce que les deux flux de matière sont réunis et le flux de matière mélangé ainsi formé est versé dans le sas sous pression ou dans un contenant de chargement en amont.
EP16400040.8A 2016-09-02 2016-09-02 Procédé de la gazéification en lit fixe sous pression Active EP3290493B1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP16400040.8A EP3290493B1 (fr) 2016-09-02 2016-09-02 Procédé de la gazéification en lit fixe sous pression
PCT/EP2017/025235 WO2018041411A1 (fr) 2016-09-02 2017-08-21 Procédé et installation pour la gazéification sous pression à lit fixe
CN201721120405.4U CN207567181U (zh) 2016-09-02 2017-09-01 用于固定床加压气化的设备
CN201710779718.9A CN107794090A (zh) 2016-09-02 2017-09-01 用于固定床加压气化的方法和设备

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP16400040.8A EP3290493B1 (fr) 2016-09-02 2016-09-02 Procédé de la gazéification en lit fixe sous pression

Publications (2)

Publication Number Publication Date
EP3290493A1 EP3290493A1 (fr) 2018-03-07
EP3290493B1 true EP3290493B1 (fr) 2021-11-10

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EP16400040.8A Active EP3290493B1 (fr) 2016-09-02 2016-09-02 Procédé de la gazéification en lit fixe sous pression

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EP (1) EP3290493B1 (fr)
CN (2) CN207567181U (fr)
WO (1) WO2018041411A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114259962B (zh) * 2021-11-15 2023-08-01 山东绿满神州环境科技有限公司 一种微波作用下二氧化碳转化装置和方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1435088A (en) * 1972-11-09 1976-05-12 Gen Electric Fixed bed coal gasification
AU469916B2 (en) * 1972-11-15 1976-02-26 General Electric Company Fixed bed compositions for coal gasification
AUPQ314399A0 (en) * 1999-09-29 1999-10-21 World Oasis Australia Pty Ltd Process for recovering energy from carbon-containing materials

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* Cited by examiner, † Cited by third party
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Publication number Publication date
WO2018041411A1 (fr) 2018-03-08
CN107794090A (zh) 2018-03-13
CN207567181U (zh) 2018-07-03
EP3290493A1 (fr) 2018-03-07

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