EP2391696A2 - Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir - Google Patents

Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir

Info

Publication number
EP2391696A2
EP2391696A2 EP09801945A EP09801945A EP2391696A2 EP 2391696 A2 EP2391696 A2 EP 2391696A2 EP 09801945 A EP09801945 A EP 09801945A EP 09801945 A EP09801945 A EP 09801945A EP 2391696 A2 EP2391696 A2 EP 2391696A2
Authority
EP
European Patent Office
Prior art keywords
gas
fuel
oxygen
lock
container
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Withdrawn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
EP09801945A
Other languages
German (de)
English (en)
Inventor
Johannes Kowoll
Stefan Hamel
Michael Rieger
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
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 Uhde GmbH filed Critical Uhde GmbH
Publication of EP2391696A2 publication Critical patent/EP2391696A2/fr
Withdrawn legal-status Critical Current

Links

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • 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
    • C10J3/466—Entrained flow processes
    • 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
    • C10J3/50—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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T137/00—Fluid handling
    • Y10T137/0318—Processes
    • Y10T137/0324—With control of flow by a condition or characteristic of a fluid
    • Y10T137/0329—Mixing of plural fluids of diverse characteristics or conditions

Definitions

  • the invention is directed to a method for supplying an entrainment gasification reactor with fuel from a storage container with the interposition of at least one lock container and at least one storage container, wherein in the entrained flow gasification reactor CO and H 2 - and fly ash containing gas is generated.
  • the fuel Since the fuel is initially under ambient pressure, it must first be brought via the supply system to a pressure level above the reactor pressure in order to then be metered to the burners of the pressure gasification reactor.
  • An advantageous method provides that the fuel is conveyed from a reservoir in lock container. These are first covered to a pressure level above the reactor pressure, then the fuel over to convey a delivery line by dense phase conveying in a permanently pressurized storage tank for the burner of the gasification reactor. From this storage tank, the burners are continuously supplied in each case with a metered fuel mass flow.
  • the transport gas required for dense phase conveying is supplied in or near the outlet of the lock container or in the delivery line.
  • the emptied lock containers are then relaxed to be able to absorb more fuel charge under approximately atmospheric pressure. The flash gas is dedusted and released into the atmosphere.
  • nitrogen from the air separation plant or carbon dioxide is usually used.
  • Carbon dioxide is used when a low-nitrogen synthesis gas or hydrogen and / or CO should be generated.
  • Carbon dioxide can be recovered in the gas treatment following gasification. Frequently, the gas flowing out of the gasifier is dedusted and cleaned and subjected to CO conversion in order to adjust the H 2 / CO ratio required by the synthesis or to produce pure hydrogen. CO and water vapor are converted into CO 2 and hydrogen. Thereafter, the gas is cooled, the moisture is condensed out and then CO 2 in a wash with circulating solvent, such as MDEa, Genosorb or methanol, washed out. In a desorber, the CO 2 is expelled from the solution by lowering the pressure or raising the temperature.
  • circulating solvent such as MDEa, Genosorb or methanol
  • the gas obtained in this way contains not only CO 2 but also other components, eg H 2 , CO, N 2 , methane, hydrogen sulfide, argon, vapors of the solvent used, eg methanol, etc.
  • the CO content is for example 0.1%.
  • DE 36 90 569 C2 describes a process for removing sulfur-containing compounds from a residual gas.
  • the object of the invention is to provide a method for fuel supply of a pressure gasification plant, which ensures in an economical manner that emission of pollutants from the coal sludge and the transport is minimized or completely avoided.
  • this object is achieved according to the invention in that for smuggling and / or promotion at least 10 ppm VoI.
  • CO preferably 100 ppm to 1000 ppm
  • this gas an oxygen-containing gas is mixed, and that this gas mixture is heated to at least 10% of the oxidizing temperature in the gas-containing pollutants.
  • the oxygen-containing gas used for smuggling the loosening of the fuel in the reservoir and / or loosening and fluidization of the contents of the lock container and / or for further promotion from the lock container and / or loosening and fluidization in the Georgiabhot- ter is used for supplying the fuel between the system components and from the storage tank and / or to Flugstrom- gasification reactor.
  • a particular advantage of the present invention is that all in connection with the lock and the feed of the fuel to the entrained flow gasification reactor gases used may have the claimed criteria.
  • the pollutant and oxygen-containing gas mixture is passed through at least one catalyst to accelerate the oxidation of the pollutants.
  • the pressure used to increase the pressure in the lock or the container (s) used catalytically oxidized is not catalytically oxidized.
  • a gas with an oxygen content of less than 5% is used as lock gas, wherein in a further embodiment can also be provided that the flash gas from the reservoir of the compression stage of a compressor and / or a compression device or the Lock container (s) is supplied.
  • 1 is an apparatus diagram of the supply of the fuel to a gasification reactor
  • Fig. 2 is a suitably similar system with a plurality of storage containers and in
  • FIG. 3 shows a plant essentially according to FIG. modified guidance of the used and emerging gas flows.
  • 1 shows the fuel supply designated 1 in a storage container 2, wherein the fuel path drawn in a stronger line leads from the reservoir 2 into a lock container 3, from there via a line 4b into a storage container 5 and from there via lines 6a the burners 6 of the gasification reactor. 7
  • the effluent during filling of the lock container gas is fed via a line 3e a filter 10, wherein after filtering the gas is discharged via the line 10e either in the environment or for further use.
  • the filter dust is returned to the reservoir 2.
  • the displaced during filling of the reservoir 2 gas is also supplied to the filter 10 in the line 2e.
  • Slag and solids-containing water are carried out at 7b from the entrained flow gasification reactor, and the gas is passed via line 7a to a gas treatment 8, the synthesis gas being discharged from the gas treatment 8 via line 8a.
  • the recovered carbon dioxide can be divided into two streams, as shown in FIG. 1, a stream 8b supplied to a compression and a pipe 8c supplied to the gas export.
  • the dust-like fuel 1 is temporarily stored in the storage container 2 and transferred from there via a connecting line to the lock container 3.
  • the lock container 3 To be able to absorb fuel from the reservoir 2, the lock container 3 must first be relaxed. The effluent from the lock containers gas 3e is dedusted in the filter 10 and released into the atmosphere. Then the locks are filled with fuel and pressurized with gas 3a and 3b. Thereafter, the outlet line of the lock is rinsed with 3c and the dust-like fuel from the lock container 3 via line 4b conveyed into the storage tank 5. In this case, loosening and fluidizing gas 3b and transport gas 4a are added.
  • the storage tank 5 is permanently at operating pressure and continuously supplies the gasifier 7 via a plurality of lines 6a.
  • the delivery from the storage container is effected by adding loosening and fluidizing gas 5b into the outlet region of the container and of further transport gas 5c into the burner line 6a.
  • the Brennstoffström 6a is continuously and regulated transported by dense phase conveying in the gasification 7 via the burner 6.
  • the flash gas 5e from the feed tank is returned to an appropriate pressure stage of the compressor 18 to reduce the required gas amount 8b and the compression power.
  • the gasification 7 comprises a gasification reaction tor, a gas cooling and dedusting and a cooling and discharge of the slag 7b and the solids-containing water.
  • the gas treatment 8 part of the carbon monoxide and water vapor is converted into carbon dioxide and hydrogen.
  • the gas is purified with a solvent (eg MDEa or methanol) and carbon dioxide is separated from the synthesis gas 8a (predominantly H 2 and CO).
  • a solvent eg MDEa or methanol
  • carbon dioxide is separated from the synthesis gas 8a (predominantly H 2 and CO).
  • the carbon dioxide-containing gas obtained in the gas purification has a low pressure and usually contains small amounts of pollutants, such as carbon monoxide ⁇ 1%, hydrogen sulfide ⁇ 10 ppmv, traces of hydrocarbons, etc.
  • the recovered carbon dioxide may have one or more qualities.
  • Fig. 1 shows two CO 2 streams, 8b for densification and 8c for export.
  • the exported stream may often contain CO, H 2 S and methanol, eg if the gas is used to displace underground crude oil. If the pollutant content should also be reduced in this stream, this can also be done by oxidation, as shown in FIG.
  • An oxygen-containing gas 16c preferably air
  • the stream 8b is compressed in the compressor 18 and used for the transfer, fluidization and pneumatic transport of the fuel into the gasifier. Part of this gas is released to the environment, in the exemplary embodiment of FIG. 1 that is the flow 10e.
  • an oxygen-containing gas 16 is added to the pollutant-containing gas 8b and the mixture is compressed adiabatically or polytropically with only slight intercooling.
  • the oxygen addition, stream 16a may occur after compression 18.
  • the compressed hot gas can optionally be further heated with heat exchangers (not shown) and dwell for a certain time at the temperature so that the pollutants, in particular CO and methanol, can react with the oxygen in the gas mixture.
  • heat exchangers not shown
  • the gas in the heat exchanger 19, e.g. an evaporator to be cooled to the desired temperature.
  • the admixture of the oxygen 16 in front of the compressor 18 brings a further advantage in the carburetor.
  • the gasification media fuel 6a and oxygen are fed into the gasifier through separate, concentric passages of the burners 6 and initially form separate strands in the gasifier which are gradually mixed together.
  • the rate of reaction of the oxygen with the hot gas in the gasifier is several orders of magnitude higher than that with the first relatively cold fuel, so that the majority of the oxygen reacts with the gas, forming an extremely hot gas flame and a relatively long cold fuel strand. Only by mixing and radiation, the fuel temperature is raised, so that the gasification of the fuel can take place. If, on the other hand, part of the oxygen is fed together with the fuel, the exothermic oxygen reactions take place in the immediate vicinity of the fuel particles, which shortens the cold fuel strand and thus also the flame. The practical consequences are a higher fuel consumption and a higher carburetor output, since the maximum fuel throughput of a gasification burner is usually limited by the flame length.
  • FIG. 2 shows in more detail an alternative embodiment of the emission-reduced fuel discharge and delivery, wherein, as already mentioned above, functionally identical plant components have the same reference symbols of FIG. 1.
  • the dust-like fuel 1 is temporarily stored in the storage container 2 and from there via connecting lines to e.g. passed three lock container 3.
  • the lines are flushed with 2c before opening the lock valves.
  • fluidizing gas 2b is fed into the discharge cones of the reservoir.
  • the lock containers are used offset in time to promote the fuel, so that there is a quasi-continuous supply of the storage container 5.
  • the fuel-filled lock containers are pressed with 3a and 3b. Then, the fuel is transported into the receiver tank 5, whereby fluidizing gas 3b are fed into the outlet cones and transport gas 3c and 4a. Thereafter, the emptied containers are relaxed over 3e.
  • the expansion gases 3e are heated, for example, in the heat exchanger 11, in order to avoid icing and condensation during the expansion and in the filter 10.
  • Some of the gases can be collected in the buffer 9 and used further, for example in the storage tank, streams 2a, 2b, 2c and for inerting the grinding plant. At least some of the gases will be in the Filter 10 dedusted and released into the atmosphere.
  • the buffer 9 is additionally supplied with the gas 9a, for example during the start-up phase. Part of the transport gas introduced into the feed tank 5 with the fuel is also discharged via 5e.
  • the pressure of the expansion gases 5e is reduced by means of a compression device, e.g. an injector, which is driven by propellant gas 18d raised, so that the gases can be returned to the lock or used as a transport gas.
  • a compression device e.g. an injector, which is driven by propellant gas 18d raised, so that the gases can be returned to the lock or used as a transport gas.
  • the predominantly CO 2 -containing cold gas 8b separated in the gas treatment 8 is compressed using a compressor with interstage cooling to reduce the compression capacity.
  • a portion of the compressed gas, for example, with the parameters 60 bar and 100 0 C, is fed into the buffer 17, in which a constant pressure with PC (pressure control) is regulated and then in the fuel delivery between the outlet cones of the locks and the carburetor used.
  • PC pressure control
  • the mixture can be heated, for example, in a gas / gas heat exchanger 15 and heated with external heat Q heater 14 further heated and contacted with a catalyst 13.
  • the gas is heated by the egzotherme oxidation, so that the heat exchanger 14 at sufficiently high Concentration of the oxidizable substances H 2 , CO, H 2 S, etc., eg> 1%, can be omitted.
  • the gas is heated for example in the heat exchanger 15 to 190 0 C and in the heater 14 to 220 0 C.
  • CO, methanol and others are converted into significantly less toxic gases.
  • the effluent from the reactor 13 gas is cooled in the heat exchanger 15 to about 130 0 C and passed into the buffer 12.
  • FC flow control
  • the recirculated and compressed gas 20a may alternatively be e.g. be used as transport gas 4a and 5c or as Fluidisiergas.
  • the optimum parameters of oxidation of CO, methanol and the like, the temperature, the oxygen concentration, the amount of catalyst or the residence time in the high temperature range, if no catalyst is used, must be determined by economic analysis. Since the required residence time and the amount of catalyst are reduced with increasing oxygen concentration, an optimum in the case of excess oxygen is to be expected. High levels of oxygen in the lock gas, however, could result in ignition and explosion of the mixture with dusty fuel, particularly when using reactive fuels such as lignite or biofuels. The oxygen concentration should therefore not be higher than 5%.
  • FIG. 3 shows a further variant of the inventive emission reduction with three C0 2 fractions with different pressures.
  • the oxygen flow 16 is here the fraction 8b mixed with the lowest, for example, approximately atmospheric pressure, the mixture is adiabatically compressed until the pressure of the second fraction 8c, eg 5 bar in 18 LP, whereby the gas is heated to about 200 0 C and mixed with 8c.
  • the mixture in Figs. 22 and 23 may be further heated. Then the oxidation of the pollutants in 24 and the recovery of the heat in 22.
  • the most of the pollutants liberated low pressure gas is used in the low pressure part of the coal treatment 22a, by other consumers 22b, in the smuggling and promotion 22c after prior compression in the high pressure compressor 18HP, however the rest is relaxed in expander 25, recovering mechanical or electrical energy.
  • the expanded gas 25a can be used, for example, for the inertization of the coal grinding plant or released into the atmosphere. Further heat exchangers, eg for heating the streams 8c, 22d, 25a or cooling the streams 18a, 18b, 22a to 22c, should be considered in consideration of the technical and economic aspects.
  • Part of the gas 8 produced in the gas treatment 8, consisting mainly of CO 2 gas 8d no oxygen-containing gas is added. This gas, if necessary after compression, is exported and / or used downstream of the carburetor, for example in the gas dedusting, fly ash treatment and as flushing or sealing gas, to avoid Nutzgasppee by oxidation of H 2 and CO.
  • the gas Upon release of the lock 3, the gas is significantly cooled due to the isenotropic or polytropic relaxation, whereby ice formation from the water vapor, which originates from the residual moisture of the coal, and condensation of CO 2 could disturb the process.
  • the lock container is cyclically cally confronted with low temperatures, whereby the container wall is subjected to mechanical stress, resulting in a cyclic process fatigue of the material.
  • the lock container is heated from the outside electrically or with a medium.
  • Other apparatus of fuel extraction 2, 4, 5, 9, 10 and the connecting pipelines should also be heated in order to avoid a dew point.
  • exemplary advantageous embodiments of the invention are shown to illustrate the path of pollutants into the atmosphere and the method of reducing emissions.
  • the emission control according to the invention is also applicable to alternative designs of fuel injection and delivery, gasification and gas treatment, e.g.
  • the oxygen-containing gas 16 may have the same composition as the oxygen flow for the gasifier.
  • Common to gasification is a cryogenically recovered gas containing from 85 to 99.8% O 2 to 3% Ar and nitrogen.
  • air, oxygen-enriched air or nitrogen with an oxygen content of, for example, 2% can also be used.
  • gas 8b which consists predominantly of carbon dioxide
  • gas 8b is generally obtained in gasification plants from the downstream gas scrubber
  • an imported gas is required for the start-up operation of the entire plant, for example CO 2 or nitrogen.
  • nitrogen is preferred, which can be stored for this purpose, for example in the liquid phase.
  • the flow 18c shows that the compressed and low-pollutant gas 18 can also be used for other purposes, eg as lock and purge gas in the fly ash treatment.
  • An export gas at medium pressure can be withdrawn from the buffer 9 and the current 1Oe is available under a slight overpressure.
  • the illustrated in Fig. 2 embodiment of the reservoir 2, the lock container 3 and the Nachré effet 4b is an example that is used here to illustrate the basic processes. It is envisaged that the number of lock containers can be larger. It is also provided that the lock containers supply the feed tank 5 via a plurality of feed lines.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention vise à mettre au point un procédé pour alimenter une installation de gazéification sous pression en combustible, de sorte à garantir de manière économique une réduction ou une élimination totale d'émissions polluantes dues au sassement du charbon et au transport. A cet effet, il est prévu d'utiliser pour le sassement ou le transport un gaz contenant au moins 10 ppm vol. de CO, un gaz contenant de l'oxygène étant mélangé avec ledit gaz et le mélange gazeux obtenu étant porté à une température entraînant l'oxydation d'au moins 10% des polluants contenus dans les gaz.
EP09801945A 2009-01-28 2009-12-23 Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir Withdrawn EP2391696A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE200910006384 DE102009006384A1 (de) 2009-01-28 2009-01-28 Verfahren zur Versorgung eines Flugstromvergasungsreaktors mit Brennstoff aus einem Vorratsbehälter
PCT/EP2009/009240 WO2010086008A2 (fr) 2009-01-28 2009-12-23 Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir

Publications (1)

Publication Number Publication Date
EP2391696A2 true EP2391696A2 (fr) 2011-12-07

Family

ID=42338484

Family Applications (1)

Application Number Title Priority Date Filing Date
EP09801945A Withdrawn EP2391696A2 (fr) 2009-01-28 2009-12-23 Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir

Country Status (14)

Country Link
US (1) US8900334B2 (fr)
EP (1) EP2391696A2 (fr)
KR (1) KR101626185B1 (fr)
CN (1) CN102300963A (fr)
AP (1) AP3458A (fr)
AU (1) AU2009338632B2 (fr)
BR (1) BRPI0924226A2 (fr)
CA (1) CA2750927A1 (fr)
DE (1) DE102009006384A1 (fr)
RU (1) RU2513404C2 (fr)
TW (1) TWI464254B (fr)
UA (1) UA108984C2 (fr)
WO (1) WO2010086008A2 (fr)
ZA (1) ZA201106284B (fr)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102009036973A1 (de) 2009-08-12 2011-02-17 Uhde Gmbh Verfahren zur Versorgung eines Flugstromvergasungsreaktors mit kohlenstoffhaltigen Brennstoffen
WO2013153791A1 (fr) * 2012-04-09 2013-10-17 Ｊｆｅスチール株式会社 Procédé pour réduire le point de rosée de gaz ambiant dans un four de recuit, dispositif associé, et procédé de production de tôle d'acier recuit laminée à froid
DE102012104868B4 (de) 2012-06-05 2022-07-28 Thilo Kraemer Pneumatischer Förderer für Schüttgüter
DE102012104866B4 (de) * 2012-06-05 2014-10-30 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren zum Betrieb einer Schüttgutschleuseneinrichtung
DE102013018332A1 (de) * 2013-10-31 2015-04-30 Linde Aktiengesellschaft Vorrichtung zur Einbringung von festem organischen Einsatzmaterial in eine Vergasungsanlage
HUE043074T2 (hu) * 2014-10-01 2019-08-28 Shell Int Research Rendszerek és eljárások anyag túlnyomásos rendszerben történõ beadagolására
CN108650888B (zh) * 2015-12-14 2020-11-06 气体产品与化学公司 气化工艺和馈送系统
JP6700773B2 (ja) * 2015-12-18 2020-05-27 三菱日立パワーシステムズ株式会社 チャー排出装置、これを有するチャー回収装置及びチャー排出方法、ガス化複合発電設備
JP7331512B2 (ja) * 2019-07-18 2023-08-23 Ｕｂｅマシナリー株式会社 貯蔵設備
CN110760327B (zh) * 2019-10-28 2020-11-13 安徽理工大学 煤炭液化装置及工艺
CN110669551B (zh) * 2019-10-28 2020-11-13 安徽理工大学 煤炭气化系统及方法

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DD147188A3 (de) * 1977-09-19 1981-03-25 Lutz Barchmann Verfahren und vorrichtung zur druckvergasung staubfoermiger brennstoffe
DD145180A3 (de) * 1978-10-16 1980-11-26 Herbert Richter Verfahren zur druckent-und-vergasung von rohbraunkohle
GB2156843A (en) * 1984-02-10 1985-10-16 Hitachi Ltd Method and apparatus for feeding coal in an integrated power and coal gasification plant
JPH0635589B2 (ja) * 1985-04-17 1994-05-11 三菱重工業株式会社 加圧型ガス化炉
FR2589141B1 (fr) * 1985-10-25 1987-12-11 Elf Aquitaine Procede d'elimination des composes soufres contenus dans un gaz residuaire, notamment issu d'une usine a soufre claus, avec recuperation desdits composes sous la forme de soufre
DE3809851A1 (de) * 1988-03-24 1989-10-05 Krupp Koppers Gmbh Verfahren zum foerdern eines feinkoernigen bis staubfoermigen brennstoffes in einen unter erhoehtem druck stehenden vergasungsreaktor
DE3810404A1 (de) * 1988-03-26 1989-10-12 Krupp Koppers Gmbh Verfahren und vorrichtung zum pneumatischen foerdern eines feinkoernigen bis staubfoermigen brennstoffes in einen unter erhoehtem druck stehenden vergasungsreaktor
US20030181314A1 (en) * 2001-08-31 2003-09-25 Texaco Inc. Using shifted syngas to regenerate SCR type catalyst
GB0218815D0 (en) * 2002-08-13 2002-09-18 Air Prod & Chem Process and apparatus for the production of hydrocarbon compounds from methane
CN100450901C (zh) * 2005-07-11 2009-01-14 西安热工研究院有限公司 一种多支路出料的干煤粉加压密相输送装置
US20070225382A1 (en) * 2005-10-14 2007-09-27 Van Den Berg Robert E Method for producing synthesis gas or a hydrocarbon product
DE102007008690A1 (de) 2007-02-20 2008-08-21 Linde Ag Erzeugung von Gasprodukten aus Syntheserohgas
DE102007020333A1 (de) 2007-04-30 2008-11-06 Siemens Ag Einsatz von reinem Kohlendioxid als Inertisierungs- und Fördermedium in Staubeintragsystemen für die Kohlenstaubdruckvergasung
DE102007020332A1 (de) 2007-04-30 2008-11-06 Siemens Ag Einsatz einer Mischung von Kohlendoxid und Stickstoff als Inertisierungs- und Fördermedium in Staubeintragsystemen für die Kohlenstaubdruckvergasung
US20090121191A1 (en) * 2007-11-14 2009-05-14 Texyn Hydrocarbon, Llc System and method for high pressure synthesis gas processing
US20110071229A1 (en) * 2009-09-21 2011-03-24 Synthesis Energy Systems, Inc. Synthetic Gas Recycle Apparatus and Methods

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2010086008A2 *

Also Published As

Publication number Publication date
BRPI0924226A2 (pt) 2016-01-26
CN102300963A (zh) 2011-12-28
ZA201106284B (en) 2012-10-31
WO2010086008A3 (fr) 2010-11-11
AP3458A (en) 2015-11-30
RU2011135415A (ru) 2013-03-10
AP2011005832A0 (en) 2011-08-31
WO2010086008A2 (fr) 2010-08-05
DE102009006384A1 (de) 2010-08-19
RU2513404C2 (ru) 2014-04-20
US20120111416A1 (en) 2012-05-10
KR20110118143A (ko) 2011-10-28
AU2009338632B2 (en) 2014-12-18
AU2009338632A1 (en) 2011-08-18
UA108984C2 (uk) 2015-07-10
TW201037071A (en) 2010-10-16
KR101626185B1 (ko) 2016-05-31
TWI464254B (zh) 2014-12-11
CA2750927A1 (fr) 2010-08-05
US8900334B2 (en) 2014-12-02

Similar Documents

Publication Publication Date Title
EP2391696A2 (fr) Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustible prélevé dans un réservoir
EP2102453B1 (fr) Procédé et installation de production d'énergie électrique dans une centrale à cycle combiné
EP1749872A2 (fr) Méthode de gazéification endothermique de charbon
WO2010057767A9 (fr) Procédé et dispositif de production d'un gaz brut de synthèse
WO2011018198A2 (fr) Procédé pour alimenter un réacteur de gazéification à lit entraîné en combustibles carbonés
EP3465041A1 (fr) Système d'installations interconnectées de fabrication de matériaux de construction minéraux et procédé de fonctionnement du système d'installations interconnectées
DE2659752C3 (de) Verfahren zum Entschwefeln von auf unter 0,1 mm zerkleinerter Kohle
DE102008060893A1 (de) Verfahren und Vorrichtung zur Versorgung eines Reaktors zur Erzeugung von Rohsynthesegas
WO2017202659A1 (fr) Système d'installations interconnectées destiné à la fabrication de matériaux de construction minéraux et procédé de fonctionnement du système d'installations interconnectées
DE19536383A1 (de) Verfahren und Vorrichtung zur Vergasung von heizwertarmen Brennstoffen
WO2017202661A1 (fr) Ensemble d'installations pour la production de matériaux de construction minéraux et procédé permettant de faire fonctionner un ensemble d'installations
DE102014000471A1 (de) Verfahren zur thermischen Spaltung von organischen Abfallstoffen
EP3465040A1 (fr) Système d'installations interconnectées de fabrication de matériaux de construction minéraux et procédé de fonctionnement du système d'installations interconnectées
WO2017202660A1 (fr) Système d'installations interconnectées destiné à la fabrication de matériaux de construction minéraux et procédé de fonctionnement de ce système
WO2015035969A2 (fr) Procédé et installation de vecteurs carbone et traitement ultérieur du gaz produit
DE102012104866B4 (de) Verfahren zum Betrieb einer Schüttgutschleuseneinrichtung
DE2631185A1 (de) Verfahren zum erzeugen von synthesegas aus kohlenstoffhaltigen ausgangsfeststoffen
DE1471587C (de) Verfahren zur Erzeugung von Staubkoks
DE102009007879A1 (de) Verfahren und Vorrichtung zur Gaserzeugung aus chlorhaltigen Brenn- und Abfallstoffen
DE2721677A1 (de) Verfahren zum verstromen schwefelreicher kohle
DE2457362A1 (de) Verfahren zum entschwefeln von kohle
DE2843976A1 (de) Verfahren und anlage zur autothermen druckvergasung, insbesondere fuer die verstromung von fossilen brennstoffen, z.b. von steinkohle
DE2715929A1 (de) Verfahren zur schnellentgasung von zu staub gemahlener kohle
DE3144171A1 (de) Herstellung von heizgas
DD252387A1 (de) Verfahren zur stofflichen verwertung von staubdickteer

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20110812

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO SE SI SK SM TR

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: THYSSENKRUPP UHDE GMBH

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: THYSSENKRUPP INDUSTRIAL SOLUTIONS AG

17Q First examination report despatched

Effective date: 20160331

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20170701