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EP0644789B1 - Procede de traitement de dechets organiques - Google Patents

Procede de traitement de dechets organiques Download PDF

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Publication number
EP0644789B1
EP0644789B1 EP93915232A EP93915232A EP0644789B1 EP 0644789 B1 EP0644789 B1 EP 0644789B1 EP 93915232 A EP93915232 A EP 93915232A EP 93915232 A EP93915232 A EP 93915232A EP 0644789 B1 EP0644789 B1 EP 0644789B1
Authority
EP
European Patent Office
Prior art keywords
molten metal
carbon
enriched
organic waste
hydrogen
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.)
Expired - Lifetime
Application number
EP93915232A
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German (de)
English (en)
Other versions
EP0644789A1 (fr
Inventor
Christopher J. Nagel
Kevin A. Sparks
Casey E. Mcgeever
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.)
Molten Metal Technology Inc
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Molten Metal Technology Inc
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Filing date
Publication date
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Publication of EP0644789A1 publication Critical patent/EP0644789A1/fr
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    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A62D3/32—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents by treatment in molten chemical reagent, e.g. salts or metals
    • 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
    • C10J3/57—Gasification using molten salts or metals
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/20—Organic substances
    • 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

Definitions

  • the present invention relates to a method for treating organic waste in molten metal contained in a vessel to sequentially form enriched hydrogen gas and carbon oxide gas streams.
  • an organic waste containing hydrogen and carbon is introduced into molten metal, without the addition of a separate oxidizing agent and under conditions sufficient to decompose the organic waste and to generate an enriched hydrogen gas stream and to carbonize the molten metal.
  • the enriched hydrogen gas stream is substantially removed from the vessel.
  • a separate oxidizing agent is added into the carbonized molten metal to oxidize carbon contained in the carbonized molten metal to form an enriched carbon oxide gas stream.
  • the enriched carbon oxide gas stream is substantially removed from the vessel.
  • the organic waste is introduced into molten metal contained in a vessel which comprises two immiscible metals wherein the first immiscible metal has a free energy of oxidation, at the operating conditions, greater than that for oxidation of carbon to carbon monoxide and the second immiscible metal has a free energy of oxidation, at the operating conditions, greater than that for oxidation of carbon monoxide to carbon dioxide, without the addition of a separate oxidizing agent and under conditions sufficient to decompose the organic waste and to generate an enriched hydrogen gas stream and to carbonize at least one of the two immiscible metals.
  • the enriched hydrogen gas stream is substantially removed from the vessel. Thereafter, a separate oxidizing agent is added into the carbonized molten metal to oxidize carbon contained in the carbonized molten metal to generate an enriched carbon monoxide and carbon dioxide gas stream having a significantly increased ratio of carbon dioxide/carbon monoxide compared to that produced in molten iron under the same conditions and decarbonizing the molten metal.
  • the enriched carbon oxide gas stream is substantially removed from the vessel.
  • This invention has the advantage of treating organic waste to form an enriched stream of hydrogen gas and a separate enriched stream of carbon oxide gas, such as carbon monoxide or carbon dioxide or both.
  • Enriched hydrogen and/or carbon oxide gas streams are often desired.
  • an enriched stream of hydrogen gas is particularly useful in the synthesis of ammonia or oxoalcohol and in hydrogenation or desulfurization processes.
  • Hydrogen is also an excellent "clean" or "greenhouse gas free” fuel.
  • Figure 1 is a schematic representation of a system for sequentially forming enriched hydrogen and enriched carbon oxide gas streams from an organic waste in molten metal by a method according to this invention.
  • Figure 2 is a plot of the free energies at varying temperatures for the oxidation of nickel, iron and carbon.
  • the present invention generally relates to a method for treating organic waste in molten metal to separately form enriched hydrogen and carbon oxide gas streams.
  • This invention is an improvement of the Bach/Nagel method disclosed in U.S. Patents 4,574,714 and 4,602,574, the teachings of which are incorporated by reference.
  • system 10 includes reactor 12.
  • reactor 12 examples include appropriately modified steelmaking vessels known in the art as K-BOP, Q-BOP, argon-oxygen decarbonization furnaces (AOD), BOF, etc.
  • Reactor 12 includes upper portion 14 and lower portion 16.
  • Off-gas outlet 18 extends from upper portion 14 and is suitable for conducting an off-gas composition out of reactor 12.
  • Organic waste inlet tube 20 includes organic material inlet 22 and extends from lower portion 16 of reactor 12.
  • Line 24 extends between organic waste source 26 and organic waste inlet tube 20.
  • Pump 28 is disposed in line 24 for directing organic waste from organic waste source 26 through organic waste inlet tube 20 and into molten metal contained in reactor 12.
  • Tuyere 30 is disposed at lower portion 16 of reactor 12.
  • Tuyere 30 includes oxidizing agent tube 32 for injection of a separate oxidizing agent at oxidizing agent inlet 34.
  • Line 36 extends between oxidizing agent tube 32 and oxidizing agent source 38.
  • Outer tube 40 of tuyere 30 is disposed concentrically about oxidizing agent tube 32 at oxidizing agent inlet 34.
  • Line 42 extends between outer tube 40 and shroud gas source 44 for conducting a suitable shroud gas from shroud gas source 44 through the concentric opening between outer tube 40 and oxidizing agent tube 32 to oxidizing agent inlet 34.
  • organic waste tube or more than one oxidizing agent tube, or combinations thereof can be disposed at the lower portion of reactor 12 for introduction of organic waste and an oxidizing agent into reactor 12.
  • Suitable organic waste can also, optionally, be introduced into reactor 12 through port 46 and/or conducted from organic waste source 26 through line 47 to reactor 12.
  • Other means, such as an injection lance (not shown), can also be employed to introduce organic waste into molten metal in carbonization reactor 12.
  • Bottom tapping spout 48 extends from lower portion 16 of reactor 12 and is suitable for removal of molten metal from reactor 12.
  • Induction coil 50 is disposed at lower portion 16 for heating molten metal 56 in reactor 12. It is to be understood that, alternatively, reactor 12 can be heated by other suitable means, such as by oxyfuel burners, electric arcs, etc.
  • Trunions 52 are disposed at reactor 12 for manipulation of reactor 12.
  • Seal 54 is disposed between off-gas outlet 18 and port 46 and is suitable for allowing partial rotation of reactor 12 about trunions 52 without breaking seal 54.
  • Molten metal 56 is disposed within reactor 12.
  • molten metal 56 comprises a metal having a free energy of oxidation, at operating conditions of system 10, which is greater than the free energy for conversion of atomic carbon to carbon monoxide.
  • suitable metals include iron, chromium and manganese.
  • Molten metal 56 can include more than one metal.
  • molten metal 56 can include a solution of miscible metals, such as iron and chromium.
  • Suitable metals are those with melting points within the operating conditions of the system. It is preferred, for example, to run system 10 in a temperature range of from about 1300°C to about 1700°C.
  • Suitable metals must also have a carbon solubility sufficient to allow significant amounts of hydrogen to be generated as organic waste is decomposed and the molten metal becomes carbonized.
  • metals with a carbon solubility of greater than about 0.5 percent, by weight are preferred, and those with a carbon solubility of greater than about two percent, by weight, are particularly preferred.
  • at least one of the metals should have the aforementioned carbon solubility.
  • the viscosity of the molten metal in reactor 12 less than about ten centipoise at the operating conditions of reactor 12.
  • Molten metal 56 is formed by at least partially filling reactor 12 with a suitable metal. The metal is then heated to a suitable temperature by activation of induction coil 52 or by other suitable means, not shown. Suitable operating conditions of system 10 include a temperature sufficient to at least partially convert organic waste by decomposition to hydrogen and carbon. Generally, a temperature in the range of between about 1,300° and about 1,700°C is suitable.
  • molten metal 56 can have vitreous or slag layer 62.
  • Vitreous layer 62 which is disposed on molten metal 56, is substantially immiscible with molten metal 56.
  • Vitreous layer 62 can have a lower thermal conductivity than that of molten metal 56. Radiant heat loss from molten metal 56 can thereby be reduced to significantly below the radiant heat loss from molten bath where no vitreous layer is present.
  • a vitreous layer 62 includes at least one metal oxide having a free energy of oxidation, at the operating conditions of system 10, which is less than that for the oxidation of atomic carbon to carbon monoxide, such as calcium oxide (CaO).
  • Vitreous layer 62 can contain a suitable compound for scrubbing halogens, such as chlorine or fluorine, to prevent formation of hydrogen halide gases, such as hydrogen chloride.
  • organic waste is suitable for treatment by this invention.
  • An example of a suitable organic waste is a hydrogen-containing carbonaceous material, such as oil or a waste which includes organic compounds containing nitrogen, sulfur, oxygen, etc.
  • the organic waste can include inorganic compounds.
  • the organic waste can include other atomic constituents, such as halogens, metals, etc.
  • Organic waste does not need to be anhydrous.
  • significant amounts of water in the organic waste can cause the water to act as an oxidizing agent, thereby interfering with the formation of an enriched hydrogen gas.
  • a preferred organic waste includes a relatively high hydrogen containing carbonaceous material, such as propane, butane, etc.
  • a preferred organic waste includes a low hydrogen containing carbonaceous material, such as tars, oils, olefins, etc.
  • Organic waste is directed from organic waste source 26 through line 24 by pump 28 and is injected into molten metal 56 through organic waste tube 20.
  • the organic waste is a fluid which can include organic waste components dissolved or suspended within a liquid.
  • solid particles of organic waste components are suspended in an inert gas, such as argon.
  • Organic waste directed into molten metal 56 is converted to carbon, hydrogen and its other atomic constituents.
  • the atomic hydrogen is then formed into hydrogen gas in the absence of an oxidizing agent and the molten metal is concurrently carbonized.
  • carbonize means the addition of atomic carbon to molten metal to increase the overall quantity of carbon contained in the molten metal without any substantial losses of carbon from the molten metal due to oxidation by a separately added oxidizing agent. It is understood, of course, that the organic waste may contain one or more oxidizing agents but these are not considered separately added oxidizing agents.
  • Hydrogen gas migrates through molten metal 56, by diffusion, bubbling or other means. At least a portion of the hydrogen migrates to a portion of molten metal 56 proximate to off-gas outlet 18 to form an enriched hydrogen gas stream.
  • An enriched hydrogen gas stream means a gas stream wherein the molar fraction of hydrogen contained in the gas stream, based upon the total hydrogen and carbon oxide in the gas stream, is greater than that generally produced in a typical process disclosed by Bach/Nagel in U.S. Patents 4,574,714 and 4,602,574 for the simultaneous, combined decomposition and oxidation of an organic waste.
  • the molar fraction of hydrogen is the ratio of the moles of hydrogen contained in a gas stream to the sum of the moles of hydrogen and moles of carbon oxide gases contained in the gas stream.
  • the concentration of dissolved carbon in carbonized molten metal 36 is preferably limited to an amount below the saturation point for carbon at the temperature of molten metal 36.
  • the concentration of atomic carbon preferably is limited to a concentration of less than about five percent, by weight, at 1,800°C.
  • the saturation point of carbon is in the range of between about three percent at 1,400°C and about 4.3 percent, by weight, at 1,800°C.
  • the saturation point of carbon is in the range of between about eight percent at 1,400°C and about 8.5 percent, by weight, at 1,800°C.
  • the saturation point of carbon is in the range of between about eleven percent at 1,800°C and about fifteen percent, by weight, at 2,000°C.
  • suitable apparatus known in the art can be used to separate the entrained carbon dust from the hydrogen gas stream. Examples of suitable apparatus include a cyclone separator or baghouse filter.
  • a suitable separate oxidizing agent is directed from oxidizing agent source 38 through line 36 and is injected through oxidizing agent tube 32 into molten metal 56.
  • the separate oxidizing agent is directed into molten metal 56 when the carbon, which is dissolved in the molten metal, approaches saturation in the molten metal.
  • the separate oxidizing agent is directed into the molten metal separately from the organic waste.
  • suitable oxidizing agents include oxygen, air, iron oxide, etc., with the preferred oxidizing agent being oxygen gas.
  • An enriched carbon oxide gas stream means a gas stream wherein the molar fraction of carbon oxide gas contained in the gas stream based upon the total hydrogen and carbon oxide in the gas streams, is greater than that generally produced in a typical process disclosed by Bach/Nagel in U.S. Patents 4,574,714 and 4,602,574 for the simultaneous, combined decomposition and oxidation of an organic waste.
  • the molar fraction of carbon oxide gas is the ratio of the moles of carbon oxide gas contained in a gas stream to the sum of the moles of hydrogen and moles of carbon oxide gases contained in the gas stream.
  • the separate introduction of the oxidizing agent from the organic waste into the molten metal means an injection of oxidizing agent separate chronologically from the organic waste in order to allow the formation of a distinct hydrogen gas stream and a distinct carbon oxide gas stream to be produced.
  • Molten metal 56 has a temperature sufficient to cause the organic waste injected into molten metal 56 to be converted to carbon, hydrogen and other atomic constituents and to cause hydrogen in molten metal 56 to form hydrogen gas and to carbonize the molten metal.
  • Oxidizing agent which oxidizes carbon contained in the molten metal, is directed into molten bath after the enriched hydrogen gas is removed and forms a carbon oxide gas, thereby forming an enriched carbon oxide gas stream.
  • the carbon oxide gas composition ratio of carbon monoxide to carbon dioxide can be adjusted by a number of techniques.
  • One relates to the selection of the metal or metals. For example, iron tends to produce carbon monoxide whereas molten nickel or manganese tends to produce an increased amount of carbon dioxide.
  • U.S. Patent 5,177,304 issued to Nagel (January 5, 1993), discloses a method and system for increasing the formation of carbon dioxide from carbonaceous material in a molten bath of immiscible metals.
  • the teachings of this patent are hereby incorporated by reference.
  • an increased amount of carbon dioxide can be produced from a molten metal bath which has two immiscible molten metals wherein the first has a free energy of oxidation greater than that for oxidation for atomic carbon to carbon monoxide and the second has a free energy of oxidation greater than that for oxidation of carbon monoxide to form carbon dioxide.
  • an alternative embodiment can include introducing the organic waste into the molten metal without the addition of a separate oxidizing agent and under conditions sufficient to decompose the organic waste, whereby the molten metal is carbonized and an enriched hydrogen gas stream is formed.
  • the carbonized metal can then be solidified.
  • the carbonized metal can be melted, and a separate oxidizing agent can then be added into the carbonized metal to oxidize carbon contained in the carbonized molten metal to thereby form an enriched carbon oxide gas stream.
  • molten metal can be carbonized to generate an enriched hydrogen gas stream in one portion of a reactor and decarbonized with addition of a separate oxidizing agent to generate an enriched carbon oxide gas stream in another portion of the same vessel.
  • the vessel can have a wide variety of shapes and need not be configured as illustrated in the Figures herein.
  • An organic waste containing an organic compound having hydrogen and carbon, such as butane, is fed into a system, as shown in Figure 1.
  • the metal is iron at a temperature of about 1800°C.
  • the organic waste is decomposed to its atomic constituents, including carbon and hydrogen in the molten metal.
  • Hydrogen gas is generated and removed from reactor through the off-gas outlet as an enriched hydrogen gas stream.
  • the molten metal is simultaneously carbonized.
  • an oxidizing agent oxygen gas
  • the reaction of carbon with the oxidizing agent occurs preferentially to the oxidation of the iron in the molten metal, because, as can be seen in Figure 2, the free energy of oxidation of carbon (Curve 1) is lower than that of the iron (Curve 2) at the temperature of the molten metal.
  • Carbon preferentially forms carbon monoxide to iron oxide or carbon dioxide because the free energy of oxidation to carbon dioxide (Curve 3) is greater than the free energy of oxidation of iron (Curve 2) which is greater than the free energy of oxidation for carbon to form carbon monoxide (Curve 1).
  • Oxygen gas is added until carbon is removed from the molten metal.
  • the carbon monoxide is separated from molten metal through the off-gas outlet which can then be directed to a carbon oxide collection tank, not shown, or vented to the atmosphere.
  • organic waste containing an organic compound having hydrogen and carbon, such as butane, is fed into the molten metal of the reactor.
  • the molten metal is nickel at a temperature of about 1800°C.
  • the organic waste forms the atomic constituents of carbon and hydrogen in the molten metal causing separation of hydrogen from carbon by the decomposition of hydrogen to form hydrogen gas.
  • the hydrogen gas is removed from reactor through the off-gas outlet in an enriched hydrogen gas stream.
  • the molten metal is carbonized.
  • oxidizing agent oxygen gas
  • the reaction of carbon with the oxidizing agent occurs preferentially to the oxidation of the nickel in the molten metal, because, as can be seen in Figure 2, the free energy of oxidation of carbon (Curve 1) is lower than that of the nickel (Curve 4) at the temperature of molten metal.
  • Carbon forms a mixture of carbon monoxide and carbon dioxide because the free energies of oxidation to form carbon dioxide (Curve 3) and to form carbon monoxide (Curve 1) are less than the free energy of oxidation of nickel.
  • Oxygen gas is added until carbon is essentially consumed in the carbonized molten metal.
  • the carbon oxide gases are separated from the molten metal through the off-gas outlet which can then be directed to a carbon oxide collection tank, not shown, or vented to the atmosphere.

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  • Chemical & Material Sciences (AREA)
  • Business, Economics & Management (AREA)
  • Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Management (AREA)
  • Toxicology (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)
  • Fire-Extinguishing Compositions (AREA)

Claims (3)

  1. Procédé de traitement de déchets organiques contenant de l'hydrogène et du carbone dans du métal fondu contenu dans un récipient pour former de manière séquentielle des flux de gaz d'hydrogène et oxyde de carbone enrichis comprenant les étapes de :
    a) introduction des déchets organiques dans du métal fondu, sans addition d'un agent d'oxydation distinct et dans des conditions suffisantes pour décomposer les déchets organiques et pour former un flux de gaz hydrogène enrichi et pour carburer le métal fondu;
    b) extraction substantielle du récipient de tout le flux de gaz hydrogène enrichi;
    c) adjonction ensuite d'un agent d'oxydation distinct dans le métal fondu carburé pour oxyder le carbone contenu dans le métal fondu carburé pour former un flux de gaz oxyde de carbone enrichi et pour décarburer le métal fondu; et
    d) extraction substantielle du récipient de tout le flux de gaz oxyde de carbone enrichi.
  2. Procédé selon la revendication 1, caractérisé en ce que, soit (a) le flux de gaz oxyde de carbone enrichi comprend du monoxyde de carbone, et le métal fondu peut comprendre du fer, et l'agent d'oxydation distinct peut comprendre de l'oxygène gazeux; et/ou (b) le flux de gaz oxyde de carbone enrichi comprend un mélange des gaz monoxyde de carbone et dioxyde de carbone, et le métal fondu peut soit (i) être choisi pour fournir un rapport molaire du dioxyde de carbone/monoxyde de carbone accru de manière significative en comparaison du rapport produit dans le fer fondu, ou (ii) être le manganèse, ou (iii) deux métaux non miscibles à savoir un premier métal non miscible ayant une énergie libre d'oxydation, dans des conditions de maintien du métal à l'état fondu, supérieure à l'énergie d'oxydation du carbone atomique en monoxyde de carbone, et un second métal non miscible ayant une énergie libre d'oxydation, dans des conditions de maintien du métal à l'état fondu, supérieure à l'énergie d'oxydation du monoxyde de carbone en dioxyde de carbone, par exemple ledit métal fondu peut comprendre un mélange non miscible de fer et de cuivre.
  3. Procédé selon la revendication 1 ou la revendication 2, caractérisé en ce que le métal fondu est carburé et décarburé dans le même réacteur pour engendrer des flux de gaz hydrogène et oxyde de carbone enrichis.
EP93915232A 1992-06-08 1993-06-08 Procede de traitement de dechets organiques Expired - Lifetime EP0644789B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US89535892A 1992-06-08 1992-06-08
US895358 1992-06-08
PCT/US1993/005398 WO1993025277A1 (fr) 1992-06-08 1993-06-08 Procede de traitement de dechets organiques

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EP0644789A1 EP0644789A1 (fr) 1995-03-29
EP0644789B1 true EP0644789B1 (fr) 1997-02-05

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EP93915232A Expired - Lifetime EP0644789B1 (fr) 1992-06-08 1993-06-08 Procede de traitement de dechets organiques

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EP (1) EP0644789B1 (fr)
JP (1) JPH07507591A (fr)
AT (1) ATE148636T1 (fr)
AU (1) AU667118B2 (fr)
BR (1) BR9306669A (fr)
CA (1) CA2136074A1 (fr)
DE (1) DE69308020T2 (fr)
DK (1) DK0644789T3 (fr)
ES (1) ES2097521T3 (fr)
GR (1) GR3022911T3 (fr)
MD (1) MD960181A (fr)
RU (1) RU2118192C1 (fr)
WO (1) WO1993025277A1 (fr)

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Publication number Priority date Publication date Assignee Title
US6254652B1 (en) * 1995-04-13 2001-07-03 Marathon Ashland Petroleum Llc At least three-step molten metal decomposition process cycle
US6270679B1 (en) 1995-05-19 2001-08-07 Lawrence Kreisler Method for recovering and separating metals from waste streams
US6254782B1 (en) 1995-05-19 2001-07-03 Lawrence Kreisler Method for recovering and separating metals from waste streams
US6274045B1 (en) 1995-05-19 2001-08-14 Lawrence Kreisler Method for recovering and separating metals from waste streams
US5753125A (en) * 1995-05-19 1998-05-19 Kreisler; Lawrence Method for recovering and separating metals from waste streams
US6797195B1 (en) 1995-05-19 2004-09-28 Lawrence Kreisler Method for recovering and separating metals from waste streams
EP0954511A1 (fr) * 1996-11-22 1999-11-10 Ashland Inc. Reacteur a bain de metal fondu et procede associe
CA2761413A1 (fr) * 2009-05-14 2010-11-18 Adam Handerek Procede et installation pour la mise en oeuvre de processus chimiques
DE102013112205A1 (de) * 2012-11-06 2014-05-08 Technische Universität Dortmund Verfahren und Vorrichtung zur Pyrolyse wasserstoffhaltiger Verbindungen

Family Cites Families (9)

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Publication number Priority date Publication date Assignee Title
DE2843997A1 (de) * 1978-10-09 1980-04-10 Kloeckner Humboldt Deutz Ag Verfahren zur herstellung von spaltgas in einem metallbad
DE3203435A1 (de) * 1982-02-02 1983-08-11 Klöckner-Werke AG, 4100 Duisburg Verfahren zur gaserzeugung und metallgewinnung in einem schmelzbadreaktor, insbesondere eisenbadreaktor
DE3434004C2 (de) * 1984-09-15 1987-03-26 Dornier System Gmbh, 7990 Friedrichshafen Verfahren und Vorrichtung zur Müllvergasung
US4574714A (en) * 1984-11-08 1986-03-11 United States Steel Corporation Destruction of toxic chemicals
DE3614048A1 (de) * 1986-04-25 1987-11-05 Kloeckner Humboldt Deutz Ag Verfahren und vorrichtung zur vergasung minderwertiger brennstoffe in einem feuerfluessigen metallschmelzbad
ATE184633T1 (de) * 1990-06-21 1999-10-15 Ashland Inc Verbesserte metallschnelzbadzersetzungsvorrichtung und verfahren
US5177304A (en) * 1990-07-24 1993-01-05 Molten Metal Technology, Inc. Method and system for forming carbon dioxide from carbon-containing materials in a molten bath of immiscible metals
MD960290A (ro) * 1991-07-29 1998-11-30 Molten Metal Technology, Inc. Procedeu de tratare a deşeurilor şi procedeu de transformare a deşeurilor în gaze atmosferice
AU666897B2 (en) * 1991-12-06 1996-02-29 Technological Resources Pty Limited Treatment of waste

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Publication number Publication date
EP0644789A1 (fr) 1995-03-29
RU94046361A (ru) 1997-04-27
WO1993025277A1 (fr) 1993-12-23
MD960181A (ro) 1998-07-31
GR3022911T3 (en) 1997-06-30
BR9306669A (pt) 1998-12-08
DK0644789T3 (da) 1997-08-18
RU2118192C1 (ru) 1998-08-27
DE69308020D1 (de) 1997-03-20
AU4529293A (en) 1994-01-04
CA2136074A1 (fr) 1993-12-23
AU667118B2 (en) 1996-03-07
DE69308020T2 (de) 1997-05-22
JPH07507591A (ja) 1995-08-24
ATE148636T1 (de) 1997-02-15
ES2097521T3 (es) 1997-04-01

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