WO2015106790A1 - Procédé de désintégration thermique de déchets organiques - Google Patents

Procédé de désintégration thermique de déchets organiques Download PDF

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Publication number
WO2015106790A1
WO2015106790A1 PCT/EP2014/003431 EP2014003431W WO2015106790A1 WO 2015106790 A1 WO2015106790 A1 WO 2015106790A1 EP 2014003431 W EP2014003431 W EP 2014003431W WO 2015106790 A1 WO2015106790 A1 WO 2015106790A1
Authority
WO
WIPO (PCT)
Prior art keywords
organic waste
gas
bulk material
moving bed
synthesis gas
Prior art date
Application number
PCT/EP2014/003431
Other languages
German (de)
English (en)
Inventor
Leonhard Baumann
Thomas STÜRMER
Xiaowei Huang
Roland Möller
Original Assignee
Ecoloop Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ecoloop Gmbh filed Critical Ecoloop Gmbh
Publication of WO2015106790A1 publication Critical patent/WO2015106790A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/344—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using non-catalytic solid particles
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/42—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0989—Hydrocarbons as additives to gasifying agents to improve caloric properties
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime

Definitions

  • the present invention is concerned with a process for the thermal decomposition of organic wastes having a melting point of less than 250 ° C.
  • CONFIRMATION COPY stood up.
  • the problem is the disposal of organic waste materials, which have a low melting point below the decomposition temperature, for example, a melting point of less than 250 ° C.
  • a melting point for example, a melting point of less than 250 ° C.
  • this is not a problem, but large amounts of additions of such waste together with the moving bed to the fact that the content of evaporated waste in the withdrawn gas is too large.
  • the object of the present invention is to provide a process which enabled the conversion of organic waste material into synthesis gas by thermal cleavage ⁇ light, which have a very low melting point.
  • this object is achieved in that the organic waste in liquid and / or vapor form in the rising gas stream countercurrent to a designed as a heated bulk bed energy buffer are dosed, the organic waste materials are split thermally into synthesis gas during the flow through the energy buffer under reductive conditions and thereby the egg ⁇ gentemperatur of the energy buffer having a gradient which decreases in the flow direction of the synthesis gas formed from ⁇ .
  • Non-decomposed constituents of the organic waste materials can also be absorbed by the bulk material moving bed with the gas flow cooling in the direction of flow when the condensation temperature and optionally also the solidification point are reached, so that they are transported again against the gas flow into areas in which the temperature is sufficient to run the thermal splitting operations.
  • the inventive method is particularly suitable for carbonaceous residues and / or boiling fractions from distillation and / or refining processes from the chemical and / or petrochemical industry, carbonaceous by-products and / or by-products from chemical conversion processes and / or organic residues from the chemical and / or thermal utilization of biomass and carbonaceous residues and / or unusable separation phases from physical and / or chemical separation processes, for example from extraction and / or elution.
  • Such products are generally unsuitable for recycling and can not be readily used thermally, since the substances are unsuitable or contaminated as energy carriers to an extent that a safe flow of the combustion processes is not guaranteed.
  • the invented The method according to the invention is also suitable for the thermal utilization of glycols, which are to be mentioned as an example of substances that accumulate to a considerable extent as waste but so far could be disposed of only very costly, also because they usually mixed with significant amounts of water are.
  • glycols which are to be mentioned as an example of substances that accumulate to a considerable extent as waste but so far could be disposed of only very costly, also because they usually mixed with significant amounts of water are.
  • the addition of water vapor but is unproblematic, depending on the operating conditions even desired.
  • the organic waste materials are metered in at at least one point of the bulk material moving bed at a temperature of at least 400.degree.
  • a temperature of at least 400.degree provides for the already discussed thermal decomposition processes before the gas stream then enters lower temperature regions.
  • the temperature at the point of addition may also be higher, the addition in very hot zones may be problematic, because then possibly the thermal decomposition of organic waste already in the supply lines / nozzles before the actual entry into the
  • Gas flow can take place.
  • the point of addition may therefore be governed by a variety of parameters, the essential factors being the nature of the organic waste, the structural design of the supply lines and the temperature distribution in the bulk material moving bed as the most important factors.
  • the bulk material moving bed may be expedient to heat the bulk material moving bed by partially oxidizing oxidizable substances. in which the oxygen-containing gas required for this purpose is metered into the energy buffer in a substoichiometric amount.
  • the bulk material may consist of metallic and / or mineral materials, with a particle size distribution between 5 and 300 mm, preferably between 10 and 150 mm, having proven advantageous for setting a suitable gas flow. Too small particle sizes hinder the gas flow, while too large particle sizes can cause a too fast gas flow, which can hinder the process of thermal cleavage.
  • At least partially alkaline material is used, preferably consisting of ⁇ carbonates and / or oxides of Alka ⁇ li- and / or alkaline earth metals.
  • the bulk material moving bed is preferably by its own
  • the bulk material moving bed when entering the reaction chamber has a natural temperature of less than 200 ° C.
  • cooling gas is metered in at the lower end of the reaction space, whereby a cooling zone is formed and the bulk material moving bed is cooled to an own temperature of less than 300 ° C. before exiting the reaction space.
  • oxygen-containing gas and / or CO 2 -containing gas or alternatively synthesis gas generated and cooled in the process itself can be used.
  • the use of synthesis gas can be advantageous if the energy content of the organic waste is not sufficient to assemble the necessary for the production of synthesis gas temperature level to ⁇ .
  • Oxygen-containing gas can be metered in above and / or at the lower end of the cooling zone, in both cases by substoichiometric partial oxidation above the cooling zone an oxidation zone and above due to the oxygen consumed in the oxidation zone forms a reduction zone.
  • the organic waste materials can be metered into the oxidation zone and / or into the reduction zone, where in each case temperatures greater than 400 ° C., in order to ensure the decomposition of organic waste.
  • the organic waste materials can also before entering the reaction space in the form of an emulsion with aqueous liquids and / or together with gaseous substances as
  • Propellant preferably metered together with water vapor and / or air and / or C02-containing gases. Such measures may vary depending on the chemical and physical properties of the organic wastes as well as for process control.
  • organic waste with higher melting points than 250 ° C may present the risk that the liquefaction already proceeds with decomposition processes which may hinder the addition to the process, it is preferably provided that such waste prior to entering the reaction space with other organic waste are mixed with a melting point of less than 250 ° C, whereby mixtures of organic waste materials having a melting point of less than 250 ° C are formed and then brought into ⁇ the reaction chamber.
  • the measure can be used according to the gen ⁇ gene of mixtures whose melting point is well below 250 ° C, z. B. below 200 ° or even lower ⁇ riger.
  • the measure can be used accordingly for generating mixtures whose melting point is interpreting ⁇ Lich below 250 ° C, for example. B. below 200 ° or even lower ⁇ riger.
  • the bulk material moving bed may be advantageous for the bulk material moving bed to have further carbonaceous materials in solid form before it enters the reaction space
  • alkaline substances in fine-grained form can bring advantages in particular when pollutants are to be bound in the organic waste, such. As halogens, or if sulfur binding mechanisms are to be promoted.
  • the bulk material moving bed is at least partially recirculated, wherein it is advantageous to separate the bulk material after leaving the cooling zone by means of physical separation methods in at least one coarse fraction and a fine fraction.
  • the coarse fraction can be recycled back ⁇ minimum can as part of the bulk material moving bed in the reactor again partially.
  • the upper end of the reaction chamber tozo ⁇ gene synthesis gas in the presence of water vapor in a gas ⁇ temperature of more than 450 ° C for a residence time of at least Is treated for 3 seconds.
  • the synthesis gas withdrawn at the upper end of the reaction space may also be advantageous for the synthesis gas withdrawn at the upper end of the reaction space to be freed from fly dust at a gas temperature of more than 300 ° C. by means of physical separation methods.
  • the synthesis gas liberated from the flue dust is preferably removed by means of gas cooling.
  • the additional metering of water and water vapor in the cooling zone or in the oxidation zone may be advantageous, wherein, for example, present in water solution organic waste can be metered without having to first separate the water by distillation or the like.
  • An additional heating of the oxidation zone by means of a burner system may be advantageous, for which fossil fuels are used in ' dusty, liquid and / or gaseous form together with oxygen-containing gas and the burner system is operated at least for the starting process for preheating the bulk material moving bed.
  • Figure 1 shows the use of a shaft reactor as Reakti ⁇ onsraum (1), which is traversed by a bulk material moving bed (2) and is designed as a vertical countercurrent gasifier.
  • the bulk material moving bed used is calcium oxide in a coarse-grained form having a particle size of up to 150 mm. The bulk material moving bed is used
  • the water vapor is used as a gasification agent, this after both the homogeneous water gas shift reaction (CO + H 2 0 -> H 2 + CO2), and according to the heterogeneous water gas reaction (C + H 2 0 - CO + H 2 ) responding.
  • CO + H 2 0 -> H 2 + CO2 the homogeneous water gas shift reaction
  • C + H 2 0 - CO + H 2 the heterogeneous water gas reaction
  • the hot gases from the oxidation zone containing CO 2 , CO, H 2 and N 2 (N 2 from the air used) flow in the chess reactor. gate further up into the reduction zone (11) and heat up the flowing from top to bottom bulk material moving bed. In the reduction zone temperatures of at ⁇ play, 600 to 1200 degrees Celsius and a largely oxygen-free atmosphere prevail.
  • Synthesis gas also longer-chain hydrocarbons of different molecular weights and boiling points, which are not completely split and continue to flow in vapor form with the synthesis gas up into the re-condensation zone (12) where significantly lower temperatures prevail.
  • the hydrocarbons meet colder particles of the bulk material moving bed, causing them to condense at least partially on the particle surfaces and transported again with the bulk material moving bed into the hotter reduction zone, where they are again at least partially split into synthesis gas.
  • the result is a kind of stationary enrichment zone of hydrocarbons in the shaft reactor (1), which leads to a significant 'increase in the average residence time of the hydrocarbons and thus to a higher degree of cleavage of these hydrocarbons to the synthesis gas.
  • the synthesis gas (13) is withdrawn at the top of the shaft reactor at (14), wherein the temperature of the synthesis gas can be increased by dosing of oxygen-containing gas at (15) and / or (16) by partial oxidation, for example, to 600 to 700 degrees Celsius to thermally synthesize last long-chain hydrocarbons to synthesis gas columns.
  • the thermal cleavage is chemically favored among other things by the presence of water vapor.
  • the synthesis gas also contains fly ash, which in this example consists essentially of fine calcium oxide.
  • fly ash is separated from the synthesis gas, for example by filtration (17) at temperatures above 300 degrees Celsius and discharged for further disposal and / or use (18). The high temperature avoids that condensate can clog the filter pores.
  • the dedusted synthesis gas can be cooled in a further step by means of gas cooling (19) to below, for example, 100 degrees Celsius and freed from condensates. As a rule, three different condensation phases can occur. Depending on the amounts of water vapor and / or water used in the shaft reactor, a water phase (20) is obtained.
  • This water ⁇ phase can be recycled into admixture with the organic liquid (5) in the oxidation zone in the shaft reactor, at least partially, for example at (21) in the oxidation zone, and / or (22) in the cooling zone, and / or (23) become. Furthermore, a heavy oil phase (24) can arise. This is preferably at least partially at (25) back into the oxidation zone (7) and / or at (26) in the reduction zone (11) and thereby uses the calorific value to form further synthesis gas. As the third condensate phase, light oil (27) can be formed during gas cooling. This light oil can be analogous to.
  • Heavy oil also at least partially at (25) in the oxidation zone (7) and / or in (26) returned to the reduction zone (11) and thereby the calorific value are used to form further synthesis gas.
  • the cooled synthesis gas (28) can be used thermally and replace fossil primary energy sources and / or be emitted via gas engines and / or gas turbines. Likewise, a use for hot steam generation and / or as a chemical raw material is possible.
  • the cooled synthesis gas can also be used as an alternative to the oxygen-containing gas as the cooling gas at (29) in the cooling zone (10) of the shaft reactor.
  • the syngas can also be used as fuel at (30) in the oxidation zone.
  • Another possibility is to use CC> 2-containing gases, for example
  • synthesis gas (29) can also be used here.
  • the bulk material moving bed further carbon support, for example, coals, cokes, biomass, sewage sludge and / or plastic waste at
  • the bulk material moving bed (35) emerging from the shaft reactor (1) via the emptying system (4) contains coarse-grained bulk material and fine particles which consist essentially of ash, mechanical abrasion and possibly added fine lime. In the fines also the main pollutants are chemically or physically bound.
  • the bulk material moving bed can, for example, be separated by means of screening (36) into at least one fine fraction (37) and one coarse fraction (38).
  • the fine fraction (37) can be discharged for further disposal and / or use.
  • the coarse fraction (38) can be recycled at least partially to (39) as a bulk moving bed into the process.
  • the countercurrent carburettor is equipped with a burner system (40) to start the process.
  • This burner system may be operated at (41) with fossil solid, liquid or gaseous fuels and at (42) with oxygen-containing gas.
  • the burner systems may be designed as combined lance systems, via which a large number of different media can be metered into the shaft reactor (1).
  • the lance systems (6), (21) and (40) can be combined in a multi-substance system.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé qui est utilisé pour désintégrer thermiquement des déchets organiques qui ont un point de fusion inférieur à 250°C. La production par exemple de gaz de synthèse à partir de déchets organiques à faible point de fusion est souvent difficile parce que les matières peuvent s'évaporer et entrer dans le flux de gaz évacué sans être décomposées. Selon l'invention, pour éviter cela, les déchets organiques sont introduits de façon dosée à l'état liquide et/ou sous forme de vapeur à contre-courant dans le flux de gaz ascendant pour obtenir un tampon énergétique configuré sous la forme d'un lit mobile chauffé de matières en vrac et les déchets organiques sont désintégrés thermiquement pour obtenir le gaz de synthèse dans des conditions réductrices au cours de l'écoulement du tampon énergétique, la température propre du tampon énergétique ayant un gradient qui diminue dans la direction d'écoulement du gaz de synthèse formé.
PCT/EP2014/003431 2014-01-16 2014-12-18 Procédé de désintégration thermique de déchets organiques WO2015106790A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014000471.6 2014-01-16
DE102014000471.6A DE102014000471A1 (de) 2014-01-16 2014-01-16 Verfahren zur thermischen Spaltung von organischen Abfallstoffen

Publications (1)

Publication Number Publication Date
WO2015106790A1 true WO2015106790A1 (fr) 2015-07-23

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WO (1) WO2015106790A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106433784A (zh) * 2016-07-08 2017-02-22 王万利 氧化层变化的煤气生产方法
US11225609B2 (en) 2019-11-01 2022-01-18 Exxonmobil Research And Engineering Company Co-processing of waste plastic with biomass

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114479949B (zh) * 2022-02-18 2023-03-03 河南科技大学 一种两段式废塑料热裂解装置及热裂解系统

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US2657124A (en) * 1948-12-30 1953-10-27 Texas Co Generation of heating gas from solid fuels
US3998606A (en) * 1973-04-23 1976-12-21 Nippon Kokan Kabushiki Kaisha Method and apparatus for manufacturing reducing gas
WO2002048292A1 (fr) * 2000-12-11 2002-06-20 Hyun Yong Kim Procede de gazeification de matieres carbonees et appareil correspondant
US20060112639A1 (en) * 2003-11-29 2006-06-01 Nick Peter A Process for pyrolytic heat recovery enhanced with gasification of organic material
WO2012039750A2 (fr) * 2010-09-20 2012-03-29 James Charles Juranitch Augmentation chimique de chaleur d'un traitement au plasma
DE102011014345A1 (de) * 2011-03-18 2012-09-20 Ecoloop Gmbh Verfahren zur energieffizienten und umweltschonenden Gewinnung von Leichtöl und/oder Treibstoffen ausgehend von Roh-Bitumen aus Ölschifer und /oder Ölsanden

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DE2647021A1 (de) * 1976-10-18 1978-04-20 Sueddeutsche Kalkstickstoff Verfahren zum betrieb eines mit einer feuerung zur aufspaltung von altreifen verbundenen kalkschachtofens
DE4244130C2 (de) * 1992-12-24 1999-10-28 Sueddeutsche Kalkstickstoff Brenner für verschiedenartige Brennstoffe zum Brennen von Kalkstein in einem Schachtofen und Verfahren zum Betreiben des Brenners
DE102007062414B4 (de) 2007-12-20 2009-12-24 Ecoloop Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
DE102011014349A1 (de) * 2011-03-18 2012-09-20 Ecoloop Gmbh Wanderbettreaktor
DE102011121508A1 (de) * 2011-12-16 2013-06-20 Ecoloop Gmbh Gegenstromvergasung mit Synthesegas als Arbeitsmedium

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2657124A (en) * 1948-12-30 1953-10-27 Texas Co Generation of heating gas from solid fuels
US3998606A (en) * 1973-04-23 1976-12-21 Nippon Kokan Kabushiki Kaisha Method and apparatus for manufacturing reducing gas
WO2002048292A1 (fr) * 2000-12-11 2002-06-20 Hyun Yong Kim Procede de gazeification de matieres carbonees et appareil correspondant
US20060112639A1 (en) * 2003-11-29 2006-06-01 Nick Peter A Process for pyrolytic heat recovery enhanced with gasification of organic material
WO2012039750A2 (fr) * 2010-09-20 2012-03-29 James Charles Juranitch Augmentation chimique de chaleur d'un traitement au plasma
DE102011014345A1 (de) * 2011-03-18 2012-09-20 Ecoloop Gmbh Verfahren zur energieffizienten und umweltschonenden Gewinnung von Leichtöl und/oder Treibstoffen ausgehend von Roh-Bitumen aus Ölschifer und /oder Ölsanden

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106433784A (zh) * 2016-07-08 2017-02-22 王万利 氧化层变化的煤气生产方法
US11225609B2 (en) 2019-11-01 2022-01-18 Exxonmobil Research And Engineering Company Co-processing of waste plastic with biomass

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