EP0101005A2 - Procédé et appareil pour décharger des restes de combustibles contenant des cendres - Google Patents

Procédé et appareil pour décharger des restes de combustibles contenant des cendres Download PDF

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Publication number
EP0101005A2
EP0101005A2 EP83107632A EP83107632A EP0101005A2 EP 0101005 A2 EP0101005 A2 EP 0101005A2 EP 83107632 A EP83107632 A EP 83107632A EP 83107632 A EP83107632 A EP 83107632A EP 0101005 A2 EP0101005 A2 EP 0101005A2
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EP
European Patent Office
Prior art keywords
water
separation chamber
slag
container
water bath
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.)
Granted
Application number
EP83107632A
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German (de)
English (en)
Other versions
EP0101005B1 (fr
EP0101005A3 (en
Inventor
Josef Dipl.-Ing. Hibbel
Ulrich Dipl.-Ing. Gerhardus
Volkmar Dipl.-Ing. Schmidt
Bernhard Lieder
Heinrich Dipl.-Ing. Scheve
Erwin Zerres
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.)
Hoechst AG
Original Assignee
Ruhrchemie AG
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 Ruhrchemie AG filed Critical Ruhrchemie AG
Publication of EP0101005A2 publication Critical patent/EP0101005A2/fr
Publication of EP0101005A3 publication Critical patent/EP0101005A3/de
Application granted granted Critical
Publication of EP0101005B1 publication Critical patent/EP0101005B1/fr
Expired legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • 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
    • C10J3/52—Ash-removing 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
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10J3/78—High-pressure apparatus
    • 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
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/18—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
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
    • 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
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/02—Slagging producer

Definitions

  • the invention relates to a method and an apparatus for discharging residues which arise in the gasification of ash-containing, in particular solid, fuels such as hard coal, lignite and other carbon-containing substances with oxygen or oxygen-containing compounds such as water and / or carbon dioxide.
  • the feedstock is converted at a pressure of 10 to 200 bar.
  • the gasification residues leave the gasification chamber in liquid or plastic form and are converted into solid granules, which can also be fine-grained, in a water bath connected to the gasification chamber. With the help of a water-filled lock container arranged under the water bath, the granular residues are periodically discharged from the pressure system of the pressure gasification system.
  • the method and device for discharging the ashes must meet a number of requirements. Apart from the fact that their operation should be possible with economically justifiable effort, it is certain make sure that the residues are discharged safely and without harming the environment.
  • the escape of product gas from the gasification chamber, which is under high pressure, into the atmosphere because of the risk of poisoning and explosion must be avoided.
  • care must be taken to ensure that dangerous or odor-causing gases, which are dissolved under pressure in process water, for example, and are released when the pressure is released, do not get into the environment, as does the waste water derived with the slag.
  • the outflow of the granulated slag from the gasification chamber into the discharge system should only be briefly interrupted by the discharge process in order to prevent the slag from backing up in the gasification chamber and thus blocking the outlet.
  • DE-OS 28 29 629 describes a method for periodically discharging residues resulting from the gasification of ash-containing fuels.
  • the resulting combustion residues granulate in a water bath.
  • a lock tank which sees a separate water supply, is located below the water bath. It is connected to the water bath via a line in which an injector is installed. The injector draws water from the lock tank and conveys it back into the water bath. To compensate, water and slag from the water bath enter the lock. The slag sediments in the lock. Before the sludge collected in the lock container is discharged, it is under the same pressure as the water Bad lock container relaxed in the separate, unpressurized or slightly overpressure water supply.
  • a predetermined amount of water is flushed into the lock container from the water supply, whereby water and slag from the lock container enter a downstream, unpressurized or slightly overpressure collection container in which slag and water are separated.
  • the lock tank which is always completely filled with water, is brought to the pressure prevailing in the water bath by opening a connecting line leading to the water bath.
  • the sluice tank is filled with slag using the previously described water circuit, which is maintained with the help of the injector.
  • the invention consists in a process for the periodic removal of residues which occur when gasifying ash-containing, in particular solid, fuels with oxygen or oxygen-containing gasifying agents under a pressure of 10 to 200 bar, which are granulated in a water bath and which are connected to a separate water supply standing, constantly filled with water lock container, from which they are discharged after relaxing from the gasification pressure to 0, o5 to 4 bar or atmospheric pressure through the water supply, into a downstream container.
  • a separating chamber is arranged between the water bath and the lock container, when the lock container is filled with slag a water flow directed from the water bath into the separating chamber is generated, which is returned from the separating chamber to the water bath, water and slag being separated from one another separate, slag gets into the lock tank located below the separation chamber, the Separation chamber is connected to the separate water supply and the hot water in the separation chamber is cooled after filling the sluice container with slag and before discharging the water-slag mixture or replaced by cold water.
  • the water-slag mixture reaches a separating chamber completely filled with water by means of a circuit flow via shut-off devices through a central channel and is returned to the water bath as a hot water phase cleaned of solids from the separating chamber using a conveying unit.
  • the central part of the central channel consists of a pipe socket, adjoined by guide surfaces arranged parallel to one another, which have an opening forming the channel in their center.
  • the guide surfaces are expediently self-contained and have the shape of a truncated cone or an oblique plate, the opening of which is determined by the overall diameter and points upwards.
  • Their diameter is from 70% to 99% of the diameter of the separation chamber. They are suspended from load-bearing axles that have spacers to ensure that the individual guide surfaces are arranged in parallel. It has proven to be advantageous to use a conical shape with an opening angle of 30 to 160 °, preferably 60 to 120 °. However, it is also possible to design the guide surfaces as inclined plates.
  • the untexn part of the central channel is formed by a further tubular connecting piece, the end of which protrudes only a short distance into a lock container immediately downstream of the separation chamber.
  • the central channel has the task of guiding falling solid particles into the lock tank and discharging hot water from the separation chamber along its guide surfaces.
  • the separation chamber On the one hand, the separation of finely divided slag, which settles on the guide surfaces built into the separation chamber, and water is brought about, on the other hand, the hot water is - immediately returned from the separation chamber back into the water bath.
  • the hot water enters the separation chamber through the central channel, flows between the baffles, resulting in a considerable slowdown in flow as a result of an enlarged overall cross-section and, thanks to the short sedimentation paths between the plates, also effectively separating fine particles.
  • the hot water is drawn off at the top of the separation chamber and returned to the water bath with the aid of the delivery unit.
  • the coarse, compact slag sinks due to its high weight directly through the central channel into the lock tank located below the separation chamber and settles there. Since the central channel leads through the separation chamber, but only slightly dips into the lock container, it is ensured that the hot and correspondingly lighter water which is circulated does not get into the lock container. Rather, the hot water flows even before the end of the central channel between the individual, parallel guide surfaces and is returned to the water bath with the help of the conveyor unit.
  • the fine-particle ash or fine-grained slag particles settle on the guide surfaces, agglomerate over time into a more compact layer, which due to its own weight finally slides into the central channel following the inclination of the guide surfaces and also reaches the lock tank via this.
  • a possible warming due to mixing of the hot water from the water bath and the cold water of the lock container is thus prevented and at the same time sufficient separation of fine-particle slag or ash is achieved.
  • the hot water in the separation chamber After filling the sluice container with slag and ash, the hot water in the separation chamber, after opening the corresponding shut-off devices, is passed through a heat exchanger with the aid of the delivery unit and cooled until the filling of the separation chamber has temperatures below 100 ° C.
  • This measure ensures that spontaneous evaporation processes are prevented during the subsequent expansion of the separation chamber and the lock container from a gasification pressure of 10 to 200 bar to a pressure of 0.05 to 4 bar or atmospheric pressure due to the high water temperature.
  • the relaxation occurs very quickly and without whirling up or partial discharge of the lock contents via the relaxation line.
  • An alternative is to introduce cold, pressurized water directly into the separation chamber instead of cooling by means of a heat exchanger, to displace the hot water present in the separation chamber into the water bath via the connecting line between the separation chamber and the water bath, in order to then relax of the so exchanged. also carry out cold contents of the separation chamber and the lock container.
  • the slag which has accumulated in the lock container, is discharged by means of a predetermined amount of water from a storage container arranged above the separation chamber, which is connected to the head of the separation chamber via a line.
  • the water flows inside the separation chamber from the outside between the guide surfaces into the central channel of the separation chamber and passes through this into the lock container and from there via a line through a previously opened shut-off device into a collecting container downstream of the lock container.
  • the slag accumulated in the lower part of the lock container is washed out and reaches the collecting container located below the lock container as a water-slag mixture, in which the slag sediments and also the final separation of water and slag, e.g. by means of a mechanical separation device, such as a slag scraper or mud dredger.
  • the discharge takes place within a short time and is usually completed within 15 to 25 seconds, for the entire process of relaxation, outfeed and pressure equalization are estimated between 20 and 30 seconds.
  • the opening and closing of the corresponding shut-off devices takes place automatically, thus preventing human error.
  • the separation chamber and the lock container always remain completely filled with water even during the discharge process. This is achieved in that the storage container arranged above the separation chamber is not completely emptied, but rather only a predetermined amount of water is removed from it.
  • the connection between the separation chamber and the storage container as well as between the lock container and the collecting container is interrupted and the spontaneously occurring pressure equalization is brought about by opening a valve in a connection between the water bath and the separation chamber. After pressure equalization, this valve is closed and the line between the water bath and the separation chamber, which is intended for the passage of slag, is opened. At the same time, the path from the separation chamber via the conveyor unit to the water bath is cleared, the circuit is thus restored, and the sluice container can absorb slag again.
  • FIG. 1 A possible embodiment of the device on which the inventive idea is based can be seen in FIG. 1.
  • the separation chamber 43 is equipped with a fill level measuring device 14.
  • the lock container 6 has two level measuring devices 23 and 25 and a pressure measuring device 20 and has jacket cooling 48.
  • the water bath 2 has a high temperature, for example 200 ° C., which is dependent on the water vapor partial pressure in the synthesis gas.
  • a quantity of process circuit water or fresh water that can be adjusted with a valve 10 is continuously fed in via a line 9.
  • a level control 11 keeps the water level constant by actuating a throttle element 12 in a drain line 13 which contains a cooler 41 and a further cooler 54. Granulated residues with poor sedimentation behavior are removed with the aid of a conveyor unit 7, e.g.
  • a pump which is connected to the separation chamber via a line 40, 16 and valve 8, is withdrawn from the water bath 2 into the separation chamber 43.
  • the hot water is separated from the slag in the separation chamber.
  • the water discharged from the separation chamber then returns to the water bath with the process circuit water via a line 36.
  • the separation chamber 43 consists of a central feed channel 45, which is designed as a tube in the upper part, and the lower part 44 of which is formed by conically shaped plates arranged in parallel, which have a central opening on the guide surfaces pointing downward.
  • the last of these conical plates has an extension piece in the middle that protrudes into the lock container 6.
  • valve 10 and the valve 12 are closed at the same time.
  • the water supply via line 9 and the water discharge via line 13 are interrupted.
  • valve 5 By closing valve 5, the connection to the water bath and the return of the water from the separation chamber into the water bath is ended by closing valve 42.
  • valve 37 By opening valve 37, the hot water in the separation chamber is established by means of a cooling system 38 provided in line 39 via line 39, which creates the connection to suction line 40 of delivery unit 7 via line 45, separation chamber 43 and ring line 16 cooled down. After the hot water has cooled, the pressure release can be initiated.
  • cold water from line 9 via a line 53 the.
  • Line 9 connects to the supply channel 45 via a valve 52, is fed to the separation chamber and the hot water in the separation chamber is discharged via the ring line 16, line 13, cooler 41 and valve 12, which is open to a certain amount.
  • the valves 8 and 37 are closed. After the hot water has been displaced and after valve 12 has been closed, the pressure in the separation chamber 43 and lock container 6 can be released.
  • Another possibility is the hot, under pressure in the separation chamber To displace water by adding cold water to the water bath.
  • the water is added, as described above, via line 9, line 53, valve 52 and feed channel 45.
  • the hot water to be displaced comes from the separation chamber 43 via the ring line 16, line 40, valve 8, which is opened, pump 7, valve 42, which is opened, and via line 36 into the water bath 2.
  • valves 52 and 8 are shut off. Then the pressure release of the separation chamber 43 and lock container 6 can take place.
  • the pressure release from the separation chamber 43 and lock container 6 takes place via the ring line 16 into a line 17 which, by opening valve 15 with simultaneously closed valves 8 and 37, separates the separation chamber via a line 17 with a water reservoir 18 which is under a pressure of 0. 05 to 4 bar, and is connected to an exhaust gas network 19, is brought about.
  • Valve 15 is then closed.
  • the pressure release to atmospheric pressure takes place via a line 51, which is also connected to the ring line 16, by opening valve 46 into a collecting container 22 which is provided with a mechanical separating device 49 for separating slag and water and is under atmospheric pressure.
  • Quantities of gas are drawn off in the collecting container 22 via a line 50 and, for example, fed to a combustion.
  • the separation chamber and the lock container connected to it are emptied by opening valve 24, which is located in a connecting line 47 between water storage container 18 and line 40, and by opening valve 21, which is installed in the connecting line between lock container 6 and collecting container 22. brought about.
  • the water-slag mixture passes through the previously opened valve 21 in the collecting container 22, where water and slag, for example with a mechanical device such as a slag scraper 49.
  • Water from the collecting container 22 passes through a pump 32 and a valve 30 controlled by a fill level measuring device 33 and a line 31 into the storage container 18. Water losses resulting from the. Water-slag separation occur in the collecting container 22, are supplemented via line 31 with the aid of a fill level measuring device 29 attached to the storage container 18, which opens a valve 34 located in a line 35. In this way, a predetermined degree of filling is ensured in the reservoir 18.
  • valves 21, 46 and 24 are closed.
  • the lock container 6 and the separation chamber 43 are thus constantly filled with water.
  • the sluice container 6 can then be filled with slag again.
  • the pressure equalization between water bath 2 and lock container 6 takes place by opening valve 26 in a line 27 which connects lines 40 and 36 to one another.
  • a differential pressure measuring device 28 indicates this pressure compensation. Since the connecting lines 45, 40 and 9, like the separation chamber, are completely filled with water, the pressure equalization between the water bath 2 and the separation chamber 43 takes place momentarily via the incompressible medium water.
  • By closing the valves 26 and 37 and. by opening the shut-off devices 5, 8 and 42 the original connection between the water bath and the separation chamber is restored and the separation chamber is filled again with slag from the water bath 2.
  • the level control 11 via the valves 10 and 12 is brought back into operation.

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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)
  • Gasification And Melting Of Waste (AREA)
EP83107632A 1982-08-13 1983-08-03 Procédé et appareil pour décharger des restes de combustibles contenant des cendres Expired EP0101005B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3230088 1982-08-13
DE19823230088 DE3230088A1 (de) 1982-08-13 1982-08-13 Verfahren und vorrichtung zum ausschleusen von rueckstaenden aschehaltiger brennstoffe

Publications (3)

Publication Number Publication Date
EP0101005A2 true EP0101005A2 (fr) 1984-02-22
EP0101005A3 EP0101005A3 (en) 1985-01-09
EP0101005B1 EP0101005B1 (fr) 1987-01-07

Family

ID=6170744

Family Applications (1)

Application Number Title Priority Date Filing Date
EP83107632A Expired EP0101005B1 (fr) 1982-08-13 1983-08-03 Procédé et appareil pour décharger des restes de combustibles contenant des cendres

Country Status (11)

Country Link
US (1) US4541840A (fr)
EP (1) EP0101005B1 (fr)
JP (1) JPS5956489A (fr)
AU (1) AU558293B2 (fr)
BR (1) BR8304239A (fr)
CA (1) CA1211287A (fr)
DE (2) DE3230088A1 (fr)
IN (1) IN159749B (fr)
PL (1) PL139176B1 (fr)
SU (1) SU1301318A3 (fr)
ZA (1) ZA835787B (fr)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0690120A1 (fr) * 1994-06-27 1996-01-03 Texaco Development Corporation Système et méthode pour le traitement de scories
WO2010012404A2 (fr) * 2008-07-29 2010-02-04 Uhde Gmbh Évacuation des scories d'un réacteur de production de gaz de synthèse
WO2010090784A3 (fr) * 2009-01-21 2010-10-07 Conocophillips Company Procédés et systèmes permettant de traiter des scories de gazéification
EP2300569A2 (fr) * 2008-07-15 2011-03-30 Uhde GmbH Dispositif d'extraction de laitier contenu dans un réacteur de gazéification de charbon

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4533363A (en) * 1984-01-20 1985-08-06 Texaco Development Corporation Production of synthesis gas
US4852997A (en) * 1987-10-05 1989-08-01 Shell Oil Company Slag water bath process
DE10118443A1 (de) * 2001-04-12 2002-10-17 Bokela Ing Gmbh Verfahren und Vorrichtung zur Stofftrennung
US20070210012A1 (en) * 2006-03-09 2007-09-13 Energy & Environmental Research Center Foundation Wet solids removal and separation system
DE102006040077C5 (de) * 2006-08-28 2014-06-05 Siemens Aktiengesellschaft Vorrichtung zum Austrag von Schlacke aus Vergasungsreaktoren
US20080115479A1 (en) * 2006-11-17 2008-05-22 Mitsubishi Heavy Industries, Ltd. Pressurized coal gasifier and coal gasification combined cycle power plant
EP1978074A1 (fr) * 2007-04-06 2008-10-08 Waterim Ltd Appareil de purification d'un débit de gaz de synthèse obtenu à partir de la gazéification de déchets et/ou biomasses
JP5484850B2 (ja) * 2009-09-30 2014-05-07 三菱重工業株式会社 スラグ排出システム
CN112210406B (zh) * 2020-10-13 2022-01-07 海泉风雷新能源发电股份有限公司 一种无炉排下吸式生物质颗粒热解炉
CN112961708A (zh) * 2021-02-07 2021-06-15 恒力石化（大连）炼化有限公司 一种气化炉下降管保护装置
CN113072980B (zh) * 2021-04-28 2021-12-07 宁夏神耀科技有限责任公司 一种过热蒸汽的下行全废锅气流床气化设备和煤化工系统

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3235313A (en) * 1964-05-18 1966-02-15 Koppers Co Inc Sluicing solid materials from spaces under superatmospheric pressure
DE2348845A1 (de) * 1973-09-13 1975-04-10 Escher Wyss Gmbh Dekanter
FR2417326A1 (fr) * 1978-02-15 1979-09-14 Tepral Grpt Interet Economique Ensemble a effet gravitaire pour la decantation en continu
DE2829629A1 (de) * 1978-07-06 1980-01-24 Ruhrchemie Ag Verfahren und vorrichtung zum ausschleusen von rueckstaenden aus dem drucksystem einer druckvergasungsanlage

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2444819B2 (de) * 1974-09-19 1980-01-03 Steag Ag, 4300 Essen Verfahren zum Reinigen des bei der Kohledruckvergasung erzeugten Gases
DE2455127C2 (de) * 1974-11-21 1986-02-27 Shell Internationale Research Maatschappij B.V., Den Haag Verfahren zum Ausschleusen von Rückständen aus einem unter erhöhtem Druck stehenden Vergasungsraum
DE2815329A1 (de) * 1978-04-08 1979-10-18 Ruhrkohle Ag Verfahren zur aufbereitung von wasser/kohlenstoffsuspensionen, die beim auswaschen des gases anfallen, das bei der vergasung von mineralischen rohstoffen entsteht
US4342638A (en) * 1979-04-02 1982-08-03 Envirotech Corporation Flashed-down residue treatment including filtering and solvent repulping
BR8105270A (pt) * 1980-11-12 1982-08-31 Texaco Development Corp Processo para producao de gas de sintese substancialmente isento de particulas
US4459134A (en) * 1982-09-15 1984-07-10 Texaco Inc. Outlet structure for a downflow generator

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3235313A (en) * 1964-05-18 1966-02-15 Koppers Co Inc Sluicing solid materials from spaces under superatmospheric pressure
DE2348845A1 (de) * 1973-09-13 1975-04-10 Escher Wyss Gmbh Dekanter
FR2417326A1 (fr) * 1978-02-15 1979-09-14 Tepral Grpt Interet Economique Ensemble a effet gravitaire pour la decantation en continu
DE2829629A1 (de) * 1978-07-06 1980-01-24 Ruhrchemie Ag Verfahren und vorrichtung zum ausschleusen von rueckstaenden aus dem drucksystem einer druckvergasungsanlage

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0690120A1 (fr) * 1994-06-27 1996-01-03 Texaco Development Corporation Système et méthode pour le traitement de scories
EP2300569A2 (fr) * 2008-07-15 2011-03-30 Uhde GmbH Dispositif d'extraction de laitier contenu dans un réacteur de gazéification de charbon
WO2010012404A2 (fr) * 2008-07-29 2010-02-04 Uhde Gmbh Évacuation des scories d'un réacteur de production de gaz de synthèse
DE102008035386A1 (de) 2008-07-29 2010-02-11 Uhde Gmbh Schlackeaustrag aus Reaktor zur Synthesegasgewinnung
WO2010012404A3 (fr) * 2008-07-29 2010-05-27 Uhde Gmbh Évacuation des scories d'un réacteur de production de gaz de synthèse
RU2508392C2 (ru) * 2008-07-29 2014-02-27 Уде Гмбх Выгрузка шлака из реактора для получения синтез-газа
TWI461524B (zh) * 2008-07-29 2014-11-21 Uhde Gmbh 自合成氣體淬取用的反應器排出爐渣的方法
US9102883B2 (en) 2008-07-29 2015-08-11 Thyssenkrupp Uhde Gmbh Slag discharge from reactor for synthesis gas production
AP3484A (en) * 2008-07-29 2015-12-31 Uhde Gmbh Slag discharge from reactor for synthesis gas production
WO2010090784A3 (fr) * 2009-01-21 2010-10-07 Conocophillips Company Procédés et systèmes permettant de traiter des scories de gazéification
US9074149B2 (en) 2009-01-21 2015-07-07 Lummus Technology Inc. Methods and systems for treating a gasification slag product

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BR8304239A (pt) 1984-04-24
EP0101005B1 (fr) 1987-01-07
PL139176B1 (en) 1986-12-31
CA1211287A (fr) 1986-09-16
US4541840A (en) 1985-09-17
PL243333A1 (en) 1985-06-04
DE3368952D1 (en) 1987-02-12
IN159749B (fr) 1987-06-06
AU558293B2 (en) 1987-01-22
SU1301318A3 (ru) 1987-03-30
DE3230088A1 (de) 1984-02-16
ZA835787B (en) 1984-04-25
AU1796383A (en) 1984-02-16
JPS5956489A (ja) 1984-03-31
EP0101005A3 (en) 1985-01-09

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