EP0644788B1 - Verfahren und vorrichtung zur behandlung von organischen abfallstoffen - Google Patents

Verfahren und vorrichtung zur behandlung von organischen abfallstoffen Download PDF

Info

Publication number
EP0644788B1
EP0644788B1 EP93914428A EP93914428A EP0644788B1 EP 0644788 B1 EP0644788 B1 EP 0644788B1 EP 93914428 A EP93914428 A EP 93914428A EP 93914428 A EP93914428 A EP 93914428A EP 0644788 B1 EP0644788 B1 EP 0644788B1
Authority
EP
European Patent Office
Prior art keywords
molten metal
carbon
reactor
hydrogen
organic waste
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
EP93914428A
Other languages
English (en)
French (fr)
Other versions
EP0644788A1 (de
Inventor
Kevin A. Sparks
Christopher J. Nagel
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
Original Assignee
Molten Metal Technology Inc
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 Molten Metal Technology Inc filed Critical Molten Metal Technology Inc
Publication of EP0644788A1 publication Critical patent/EP0644788A1/de
Application granted granted Critical
Publication of EP0644788B1 publication Critical patent/EP0644788B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • A62D2203/00—Aspects of processes for making harmful chemical substances harmless, or less harmful, by effecting chemical change in the substances
    • A62D2203/10—Apparatus specially adapted for treating harmful chemical agents; Details thereof
    • 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 an organic waste containing hydrogen and carbon in molten metal to form enriched hydrogen and carbon oxide gas streams.
  • organic waste containing hydrogen and carbon is introduced into molten metal contained in a carbonization reactor without the addition of a separate oxidizing agent and under conditions sufficient to decompose the organic waste and to generate hydrogen gas and carbonize the molten metal.
  • Carbonized molten metal is transferred from the carbonization reactor to a decarbonization reactor.
  • An oxidizing agent is introduced into the carbonized molten metal in the decarbonization reactor to oxidize carbon contained therein thereby decarbonizing the molten metal and generating an enriched stream of carbon oxide gas.
  • the decarbonized molten metal is then directed from the decarbonization reactor to the carbonization reactor.
  • the organic waste is introduced into molten metal contained in a carbonization reactor without the addition of a separate oxidizing agent and under conditions sufficient to decompose the organic waste and to generate hydrogen gas and carbonize the molten metal.
  • the molten metal includes two immiscible metals wherein the first immiscible metal has a free energy of oxidation greater than that for oxidation of atomic carbon to form carbon monoxide and the second immiscible metal has a free energy of oxidation greater than that of oxidation of carbon monoxide to form carbon dioxide.
  • the free energies of the aforementioned first and second immiscible metals are taken at the operating conditions.
  • the carbonized molten metal is transferred from the carbonization reactor to a decarbonization reactor and an oxidizing agent is introduced into the carbonized molten metal in the decarbonization reactor to oxidize carbon contained therein thereby decarbonizing the molten metal and generating an enriched stream of carbon oxide gas having an increased molar ratio of carbon dioxide/carbon monoxide.
  • the decarbonized molten metal is then directed from the decarbonization reactor to the carbonization reactor.
  • An apparatus for carrying out the method of the present invention includes a carbonization reactor having a molten metal inlet, a molten metal outlet and a hydrogen off-gas outlet and organic waste injection means for directing organic waste into molten metal contained in the carbonization reactor.
  • the apparatus further includes a decarbonization reactor having a molten metal inlet, a molten metal outlet and a carbon oxide off-gas outlet, means for directing the carbonized molten metal from the carbonization reactor to the decarbonization reactor and then returning molten metal from the decarbonization reactor to the carbonization reactor, and oxidizing agent injection means for injecting an oxidizing agent into the decarbonization reactor.
  • 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 forming enriched hydrogen and carbon oxide gas streams from an organic waste in molten metal according to this invention.
  • Figure 2 is a schematic representation of second system for forming enriched hydrogen and carbon oxide gas streams from an organic waste in molten metal according to this invention.
  • Figure 3 is a schematic representation of a third system for simultaneously forming enriched hydrogen and carbon oxide gas streams from an organic waste in molten metal according to this invention.
  • Figure 4 is a schematic representation of a fourth system for simultaneously forming enriched hydrogen and carbon oxide gas streams from an organic waste in molten metal according to this invention.
  • Figure 5 is a plot of the free energies, at varying temperatures, for the oxidation of nickel, iron and carbon.
  • the viscosity of the molten metal in carbonization reactor 12 and decarbonization reactor 14 is also preferred to have the viscosity of the molten metal in carbonization reactor 12 and decarbonization reactor 14 at less than about ten centipoise at the operating conditions of the reactors.
  • Carbon oxide off-gas outlet 40 extends from the upper portion of decarbonization reactor 14 and is suitable for conducting an enriched carbon oxide off-gas composition generated in decarbonization reactor 14 to a collection means (not shown) or to means for venting the gas.
  • Tuyere 42 is disposed at the lower portion of decarbonization reactor 14.
  • Tuyere 42 includes oxidizing agent tube 44 for injection of a separate oxidizing agent at oxidizing agent inlet 46.
  • Line 48 extends between oxidizing agent tube 44 and oxidizing agent source 50. It is to be understood, however, that more than one oxidizing agent tube can be disposed at the lower portion of decarbonization reactor 14 for introduction of oxidizing agent into decarbonization reactor 14.
  • Other means for introducing the separate oxidizing agent can, of course, also be employed alone or in combination with tuyere 42.
  • Induction coil 54 is disposed at the lower portion of decarbonization reactor 14 for heating carbonized metal in reactor 14.
  • Decarbonization reactor 14 can be, of course, heated by other suitable means, such as by oxyfuel burners, electric arcs, etc.
  • Molten metal 56 in decarbonization reactor 14 is the carbonized molten metal that was formed in carbonization reactor 12 before it was directed to decarbonization reactor 14.
  • Conduit 60 disposed between carbonization reactor 12 and decarbonization reactor 14, is employed to transfer carbonized molten metal from carbonization reactor 12 to decarbonization reactor 14.
  • Conduit 62 disposed between decarbonization reactor 14 and carbonization reactor 12, is employed to transfer decarbonized molten metal from decarbonization reactor 14 to carbonization reactor 12.
  • Suitable operating conditions for carbonization reactor 12 include a temperature sufficient to at least partially convert organic waste, such as by decomposition, to its constituents including hydrogen and carbon. Generally, a temperature in the range of between about 1,300° and about 1,700°C is suitable.
  • molten metal 36 can have vitreous or slag layer 64.
  • Vitreous layer 64 which is disposed on molten metal 36, is substantially immiscible with molten metal 36.
  • Vitreous layer 64 can have a lower thermal conductivity than that of molten metal 36. Radiant heat loss from molten metal can thereby be reduced to significantly below the radiant heat loss from molten metal where no vitreous layer is present.
  • Decarbonization reactor 14 can have a similar vitreous phase, decarbonization vitreous layer 66.
  • a vitreous layer 64 or 66 includes at least one metal oxide having a free energy of oxidation, at the operating conditions, which is less than that of conversion of atomic carbon to carbon monoxide.
  • An example is calcium oxide (CaO).
  • Vitreous layer 64 can also 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 enriched hydrogen gas.
  • a preferred organic waste is containing carbonaceous waste having a relatively high hydrogen content, such as propane, butane, etc.
  • a preferred organic waste includes a carbonaceous waste with a relatively low hydrogen content, such as tars, oils, olefins, etc.
  • the organic waste directed into molten metal 36 is converted to carbon, hydrogen, and other atomic constituents.
  • Atomic hydrogen combines to generate hydrogen in decarbonizing reactor 12.
  • Molten metal 36 contained therein 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 generated migrates through molten metal 36, such as by diffusion, bubbling or other means. At least a portion of the hydrogen gas migrates to a portion of molten metal 36 proximate to hydrogen off-gas outlet 16 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 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.
  • System 100 can operate at varying pressures in order to cause the desirable circulation of molten metal.
  • the pressure in carbonization reactor 106 is less than the pressure in molten metal reactor 102 to promote the desirable circulation of molten metal.
  • system 200 has molten metal vessel 202 with molten metal 204 disposed therein.
  • Carbonization reactor 206 and decarbonization reactor 208 are disposed within molten metal vessel 202.
  • Carbonization reactor 206 has carbonization reactor inlet 210, carbonization reactor outlet 212 and hydrogen off-gas outlet 214. Carbonization reactor inlet 210 and carbonization reactor outlet 212 are connected to carbonization reactor inlet tube 216 and carbonization reactor outlet tube 218, respectively. Carbonization reactor inlet tube 216 and carbonization reactor outlet tube 218 are of sufficient length whereby portions of inlet tube 216 and outlet tube 218 are submerged beneath the surface of molten metal 204 in molten metal vessel 202.
  • Organic waste containing carbon and hydrogen is introduced by injection means 220, which is disposed at carbonization reactor inlet tube 216, for introducing organic waste into molten metal 211 contained within carbonization reactor 206.
  • Injection means 220 include organic waste source 222, line 224 and inlet tube 226.
  • Carbon is simultaneously dissolved in molten metal 211 to form carbonized molten metal.
  • the movement of hydrogen gas through molten metal 211 causes circulation from carbonization reactor inlet 210 through carbonization reactor 206 to carbonization reactor outlet 212.
  • molten metal flows from vessel 202 into reactor 206, where it is carbonized, and back to vessel 202.
  • Decarbonization reactor 208 has molten metal inlet 232, outlet 234 and carbon oxide off-gas outlet 236.
  • Inlet 232 and outlet 234 are connected to decarbonization reactor inlet tube 238 and decarbonization reactor outlet tube 240, respectively.
  • Inlet tube 238 and outlet tube 240 are of sufficient length, so that portions of inlet tube 238 and outlet tube 240 are submerged beneath the surface of molten metal 204 in molten metal vessel 202.
  • An oxidizing agent is introduced by injection means 242, including oxidizing agent source 244, line 246 and oxidizing agent tube 248.
  • oxidizing agent is injected carbon oxide gas is formed and molten metal 233 causes the molten metal to circulate from decarbonization reactor inlet 232 through decarbonization reactor 208 to decarbonization reactor outlet 234 and back to molten metal 204 in vessel 202.
  • System 200 can operate at varying pressures to cause the desirable circulation of molten metal.
  • the pressure in carbonization reactor 206 and decarbonization reactor 208 is less than the pressure in molten metal vessel 202 to promote the desirable circulation.
  • system 300 has molten metal vessel 302 containing molten metal 304 and vitreous layer 308.
  • Baffle 310 is disposed within molten metal vessel 302. Baffle 310 extends substantially into molten metal 304 to define carbonization reactor region 312 and decarbonization reactor region 314, whereby essentially all of the hydrogen gas is formed in carbonization reactor region 312 while not allowing a substantial loss of hydrogen gas to decarbonization reactor region 314 and whereby essentially all of the carbon oxide gas is formed in decarbonization reactor region 314 while not allowing a substantial loss of carbon oxide gas to carbonization reactor region 312.
  • Carbonization reactor region 312 has hydrogen gas region 316, and decarbonization reactor region has carbon oxide gas region 318. There is no communication between hydrogen gas region 316 and carbon oxide gas region 318 except through molten metal 304.
  • Hydrogen off-gas outlet 320 is above the surface of molten metal 304 in carbonization reactor region 312, and carbon oxide off-gas outlet 322 is above the surface of molten metal 304 in decarbonization region 314.
  • Organic waste tube 324 includes organic waste inlet 326 and is located at the lower portion of carbonization reactor region 312 for injection of the organic waste at organic waste inlet 326 in a substantially vertical direction into molten metal 304.
  • the injected organic waste forms a field of flow, which remains substantially in carbonization reactor region 312, while not allowing a substantial loss of hydrogen gas to decarbonization reactor region 314.
  • Line 328 extends between organic waste source 330 and organic waste tube 324.
  • Pump 332 is disposed in line 328 for directing organic feed from organic waste source 330 to organic material inlet 326.
  • Oxidizing agent tube 334 is disposed at the upper portion of decarbonization reactor region 314 for injection of the separate oxidizing agent at oxidizing agent inlet 336 in a substantially vertical direction into molten metal 304.
  • the oxidizing agent forms a field of flow, which remains essentially in decarbonization reactor region 314, while not allowing a substantial loss of carbon oxide gas to carbonization reactor region 312.
  • Organic waste is introduced into molten metal 304 in carbonization reactor region 312 under conditions sufficient to decompose the organic waste.
  • Hydrogen gas is generated while the molten metal is carbonized in region 312.
  • Baffle 310 extends sufficiently into molten metal 304 to allow the decomposition of organic waste into hydrogen and carbon while not allowing substantial loss of hydrogen into decarbonization reactor region 314.
  • Carbon dissolves concurrently in molten metal 304.
  • the injection of organic waste into carbonization reactor region 312 can cause sufficient circulation in molten metal 304 to distribute the dissolved carbon throughout molten metal 304.
  • the enriched hydrogen gas is removed from carbonization reactor region 312 through hydrogen gas region 316 to hydrogen gas off-gas outlet 320.
  • Oxidizing agent is introduced into molten metal 304 in decarbonization reactor region 314 under conditions to oxidize carbon contained therein, thereby forming an enriched stream of carbon oxide gas.
  • Baffle 310 also extends sufficiently into molten metal 304 to allow the oxidation of dissolved carbon into carbon oxide gases while not allowing substantial loss of oxidizing agent into carbonization reactor region 312.
  • Dissolved carbon is oxidized, thereby decarbonizing the molten metal and forming an enriched carbon oxide gas stream.
  • the enriched carbon oxide gas stream is removed from decarbonization reactor region 314 through carbon oxide off-gas outlet.
  • the evolving carbon oxide gas causes sufficient circulation of molten bath 304 to return decarbonized molten metal to carbonization reactor region 312.
  • An organic waste containing an organic compound having hydrogen and carbon, such as butane, is fed into a carbonization reactor of a system, as shown in Figure 1.
  • the molten metal in the system is iron at a temperature of 1,800°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 an enriched hydrogen gas stream and to carbonize the molten iron.
  • the hydrogen gas is removed from reactor through the hydrogen off-gas outlet.
  • Carbonized molten iron is directed to a decarbonization reactor where, an oxidizing agent, oxygen gas, is then added to carbonized molten iron in the system.
  • 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 5, the free energy of oxidation of carbon (Curve 1) is lower than that for oxidation of iron (Curve 2) at the operating temperature.
  • Carbon preferentially forms carbon monoxide to iron oxide or carbon dioxide because the free energy of oxidation of carbon 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 continuously to the molten metal.
  • the carbon monoxide is separated from molten metal through the carbon oxide off-gas outlet decarbonization reactor which can then be directed to a carbon oxide collection tank, not shown, or vented to the atmosphere.
  • the decarbonized metal is returned to the carbonization reactor continuously.
  • organic waste containing an organic compound having hydrogen and carbon, such as butane, is fed into the molten metal of carbonization reactor.
  • the molten metal is nickel at a temperature of 1,800°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 an enriched hydrogen gas stream and to carbonize the molten nickel.
  • the hydrogen gas is remove from reactor through the hydrogen off-gas outlet.
  • Carbonized molten nickel is directed to a decarbonization reactor where, oxidizing agent, oxygen gas, is then added to the carbonized nickel.
  • 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 5, the free energy of oxidation of carbon (Curve 1) is lower than that of the nickel (Curve 4) at the temperature of molten nickel.
  • 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 both less than the free energy of oxidation of nickel.
  • Oxygen gas is added continuously to the carbonized molten metal to decarbonize it.
  • the carbon oxide gases are separated from the molten metal through a carbon oxide off-gas outlet which can then be directed to a carbon oxide collection tank, not shown, or vented to the atmosphere.
  • the decarbonized metal is returned to the carbonization reactor continuously
  • simultaneous generation allows for the simultaneous generation of enriched hydrogen and carbon oxide gas streams.
  • simultaneous generation is not necessary and sequential generation may be preferred in some instances.

Landscapes

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

Claims (9)

  1. Verfahren zur Behandlung eines wasserstoff- und kohlenstoffhaltigen organischen Abfallstoffes in einer Metallschmelze zur Bildung eines wasserstoffreichen Gasstroms und eines kohlenoxidreichen Gasstroms, bestehend aus oder enthaltend folgende Schritte:
    a) Einleiten des wasserstoff- und kohlenstoffhaltigen organischen Abfallstoffes in die in einem Aufkohlungsreaktor vorliegende Metallschmelze ohne gesonderte Zufuhr eines Oxidationsmittels und unter für die Zersetzung des organischen Abfalls, Erzeugung eines wasserstoffreichen Gasstroms in einer ersten Gaszone und Aufkohlung der Metallschmelze ausreichenden Bedingungen, wobei die Metallschmelze so gewählt ist, daß ein im Vergleich zu dem unter gleichen Bedingungen in einem im wesentlichen aus geschmolzenem Eisen bestehenden Schmelzbad deutlich höheres Molverhältnis von Kohlendioxid zu Kohlenmonoxid vorliegt,
    b) Leiten der aufgekohlten Metallschmelze aus dem Aufkohlungsreaktor in einen Entkohlungsreaktor,
    c) Einleiten eines sauerstoffhaltigen Oxidationsmittels in einer Menge in die aufgekohlte Metallschmelze im Entkohlungsreaktor, um den darin enthaltenen Kohlenstoff zu oxidieren, wodurch die Metallschmelze entkohlt und in einer zweiten Gaszone mit einem im Vergleich zu unter gleichen Bedingungen in einem im wesentlichen aus geschmolzenem Eisen bestehenden Schmelzbad deutlich höheren Molverhältnis von Kohlendioxid zu Kohlenmonoxid ein kohlenoxidreicher Gasstrom erzeugt wird, wobei die zweite Gaszone von der ersten getrennt ist, und
    d) Leiten der entkohlten Metallschmelze aus dem Entkohlungsreaktor in den Aufkohlungsreaktor.
  2. Verfahren gemäß Anspruch 1, wobei die Metallschmelz eim wesentlichen aus Mangan oder geschmolzenem Eisen und Kupfer besteht.
  3. Verfahren zur Behandlung eines organischen Abfallstoffes nach einem der vorhergehenden Ansprüche, wobei der wasserstoffreiche Gasstrom und der kohlenoxidreiche Gasstrom gleichzeitig gebildet werden, die Metallschmelze aus einem ersten und einem zweiten geschmolzenen Metall besteht oder dieses enthält und Schritt c) unter Fortsetzung von Schritt a) erfolgt.
  4. Verfahren gemäß Anspruch 3, wobei das erste geschmolzene Metall Eisen und das zweite geschmolzene Metall Kupfer enthält oder daraus besteht.
  5. Verfahren zur Behandlung eines organischen Abfallstoffes nach einem der vorhergehenden Ansprüche, wobei die Metallschmelze unter den Betriebsbedingungen des Aufkohlungsreaktors eine Kohlenstofflöslichkeit von mindestens ungefähr 0,5 Gewichtsprozent aufweist.
  6. Verfahren zur Behandlung eines organischen Abfallstoffes nach einem der vorhergehenden Ansprüche, wobei die Metallschmelze so gewählt ist, daß ein im Vergleich zu dem unter gleichen Betriebsbedingungen in einem im wesentlichen aus gschmolzenem Eisen bestehenden Schmelzbad deutlich höheres Molverhältnis von Kohlendioxid zu Kohlenmonoxid vorliegt, zur gleichzeitigen Bildung eines wasserstoffreichen Gasstroms und eines kohlenoxidreichen Gasstroms, wobei der wasserstoff- und kohlenstoffhaltige organische Abfallstoff in im wesentlichen vertikaler Richtung in die Metallschmelze eingeleitet wird und wobei im Innern des Reaktorbehälters eine Prallfläche angeordnet ist, die weit genug in die Metallschmelze hineinreicht, um den Innenraum des Reaktors in eine Aufkohlungszone und eine Entkohlungszone zu trennen, wobei die Prallfläche die Bildung des im wesentlichen gesamten Wasserstoffgases in der Aufkohlungszone erlaubt, jedoch einen deutlichen Wasserstoffverlust in die Entkohlungszone hinein verhindert, sowie die Bildung des im wesentlichen gesamten Kohlenoxidgases in der Entkohlungszone gestattet, jedoch einen deutlichen Kohlenoxidgasverlust in die Aufkohlungszone hinein verhindert.
  7. Verfahren nach einem der vorhergehenden Ansprüche, wobei das gesonderte Oxidationsmittel aus einem Sauerstoffgas besteht oder dieses enthält.
  8. Verfahren nach einem der vorhergehenden Ansprüche, wobei die Metallschmelze aus zwei nichtmischbaren Metallen besteht oder diese enthält, wobei unter den Betriebsbedingungen das erste nichtmischbare Metall eine freie Oxidationsenergie hat, die größer ist als für die Oxidation von atomarem Kohlenstoff zu Kohlenmonoxid, und das zweite nichtmischbare Metall eine freie Oxidationsenergie hat, die größer ist als für die Oxidation von Kohlenmonoxid zu Kohlendioxid.
  9. Verfahren gemäß Anspruch 8, wobei die erste Metallschmelze aus Eisen und die zweite Metallschmelze aus Kupfer besteht oder dieses enthält.
EP93914428A 1992-06-08 1993-06-08 Verfahren und vorrichtung zur behandlung von organischen abfallstoffen Expired - Lifetime EP0644788B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US89534692A 1992-06-08 1992-06-08
US895346 1992-06-08
PCT/US1993/005445 WO1993025278A1 (en) 1992-06-08 1993-06-08 Method and appartus for treating organic waste

Publications (2)

Publication Number Publication Date
EP0644788A1 EP0644788A1 (de) 1995-03-29
EP0644788B1 true EP0644788B1 (de) 1997-08-13

Family

ID=25404377

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93914428A Expired - Lifetime EP0644788B1 (de) 1992-06-08 1993-06-08 Verfahren und vorrichtung zur behandlung von organischen abfallstoffen

Country Status (10)

Country Link
EP (1) EP0644788B1 (de)
JP (1) JPH07507593A (de)
AT (1) ATE156716T1 (de)
AU (1) AU668736B2 (de)
BR (1) BR9306673A (de)
CA (1) CA2136073A1 (de)
DE (1) DE69313113T2 (de)
MD (1) MD960311A (de)
RU (1) RU94046339A (de)
WO (1) WO1993025278A1 (de)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998023707A1 (en) * 1996-11-25 1998-06-04 Ashland Inc. Two-zone molten metal hydrogen-rich and carbon monoxide-rich gas generation process
US6270679B1 (en) 1995-05-19 2001-08-07 Lawrence Kreisler 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
US5753125A (en) * 1995-05-19 1998-05-19 Kreisler; Lawrence 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
WO1998022385A1 (en) * 1996-11-22 1998-05-28 Ashland Inc. Molten metal reactor and process
US6717026B2 (en) * 2001-02-27 2004-04-06 Clean Technologies International Corporation Molten metal reactor utilizing molten metal flow for feed material and reaction product entrapment
US8303916B2 (en) * 2008-02-01 2012-11-06 Oscura, Inc. Gaseous transfer in multiple metal bath reactors

Family Cites Families (9)

* Cited by examiner, † Cited by third party
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
EP0600906B1 (de) * 1991-07-29 1997-05-21 Molten Metal Technology, Inc. Verfahren zur Oxidation in einem Schmelzbad
DE69225470T2 (de) * 1991-12-06 1999-01-14 Tech Resources Pty Ltd Aufbereitung von Abfällen

Also Published As

Publication number Publication date
BR9306673A (pt) 1998-12-08
WO1993025278A1 (en) 1993-12-23
CA2136073A1 (en) 1993-12-23
EP0644788A1 (de) 1995-03-29
DE69313113D1 (de) 1997-09-18
MD960311A (ro) 1998-06-30
JPH07507593A (ja) 1995-08-24
AU668736B2 (en) 1996-05-16
ATE156716T1 (de) 1997-08-15
AU4409293A (en) 1994-01-04
RU94046339A (ru) 1996-10-20
DE69313113T2 (de) 1997-12-11

Similar Documents

Publication Publication Date Title
US5537940A (en) Method for treating organic waste
US5435982A (en) Method for dissociating waste in a packed bed reactor
RU2114356C1 (ru) Способ уничтожения органических отходов
US5695732A (en) Method for treating a halogenated organic waste to produce halogen gas and carbon oxide gas streams
US4681599A (en) Gassification of carbon containing waste, refuse or the like
US5640706A (en) Method and apparatus for producing a product in a regenerator furnace from impure waste containing a non-gasifiable impurity
US5571486A (en) Method and apparatus for top-charging solid waste into a molten metal bath
US5298233A (en) Method and system for oxidizing hydrogen- and carbon-containing feed in a molten bath of immiscible metals
US8808411B2 (en) Gaseous transfer in multiple metal bath reactors
EP0644788B1 (de) Verfahren und vorrichtung zur behandlung von organischen abfallstoffen
KR960029466A (ko) 합금강 제조방법
EP0644789B1 (de) Verfahren zur behandlung von organischen abfallstoffen
US6350289B1 (en) Two-zone molten metal hydrogen-rich and carbon monoxide-rich gas generation process
KR100252708B1 (ko) 용융금속을 생산하기 위한 방법 및 장치
EP0046811B1 (de) Verfahren zum wiedergewinnen von co-reichen gas beim schmelzen von metall
EP0453904A1 (de) Verfahren zur Entsorgung von verbrauchten Batterien und anderen Abfallprodukten mit giftigem Schwermetallgehalt
GR3029444T3 (en) Treatment of fly ash
Thornblom et al. Utilizing plasma technology for chemical reactions in controlled atmosphere
JPH07173520A (ja) 含クロム溶銑および溶鋼の脱燐方法
JPH09316519A (ja) 製錬スラグの改質方法
JPH04224638A (ja) 有機物スクラップの溶鉄製造用熱源としての利用方法
AU2013205149A1 (en) Gaseous transfer in multiple metal bath reactors
WO1996025202A1 (en) Refractory barrier layer and method of formation

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: 19941225

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

17Q First examination report despatched

Effective date: 19960213

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

Owner name: MOLTEN METAL TECHNOLOGY, INC.

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: LI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRE;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.SCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: FR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: ES

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19970813

Ref country code: DK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19970813

Ref country code: CH

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 19970813

Ref country code: BE

Effective date: 19970813

Ref country code: AT

Effective date: 19970813

REF Corresponds to:

Ref document number: 156716

Country of ref document: AT

Date of ref document: 19970815

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REF Corresponds to:

Ref document number: 69313113

Country of ref document: DE

Date of ref document: 19970918

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19971113

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Effective date: 19971118

EN Fr: translation not filed
NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19980527

Year of fee payment: 6

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19980608

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19980608

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19980608

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

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

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 19981231

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19980608

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20000503