EP0236701A1 - Procédé de récupération de déchets contenant du carbone - Google Patents

Procédé de récupération de déchets contenant du carbone Download PDF

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Publication number
EP0236701A1
EP0236701A1 EP87100875A EP87100875A EP0236701A1 EP 0236701 A1 EP0236701 A1 EP 0236701A1 EP 87100875 A EP87100875 A EP 87100875A EP 87100875 A EP87100875 A EP 87100875A EP 0236701 A1 EP0236701 A1 EP 0236701A1
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EP
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Prior art keywords
waste
bar
hydrogen
hours
products
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EP87100875A
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German (de)
English (en)
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EP0236701B1 (fr
Inventor
Joachim Dr. Korff
Axel Dr. Giehr
Karl-Heinz Keim
Kurt Erdt
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RWE Entsorgung AG
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RWE Entsorgung AG
Union Rheinische Braunkohlen Kraftstoff AG
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Priority to AT87100875T priority Critical patent/ATE53859T1/de
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S423/00—Chemistry of inorganic compounds
    • Y10S423/18—Treating trash or garbage

Definitions

  • the invention relates to an improved process for reprocessing carbon-containing wastes by thermal pretreatment thereof in the presence or absence of hydrogen and subsequent hydrogenation of the pretreated material at elevated temperature and at least 200 bar hydrogen pressure.
  • Waste has been used in landfills for decades, e.g. stored in abandoned gravel pits, mine pits and elsewhere. For a long time, the chemical structure of the waste and its long-term effects on soil and groundwater have not been taken into account. More recently, certain waste has been stored in so-called special landfills. Here, efforts are made to seal the landfill from groundwater and soil.
  • Pyrolysis is now also being operated on a technical scale (see, for example, "United Economic Services GmbH", October 4, 1985, p. 9).
  • pyrolysis has the disadvantages of the predominant formation of gaseous products and a heavily contaminated coke residue in a relatively large amount and the formation of effluent containing hydrochloric acid from waste containing nitrogen (Rubbish and Waste, 6 (1980) p. 189, right column).
  • This invention relates to the hydrating treatment with or without catalyst, synthetic waste materials such as.
  • synthetic waste materials such as.
  • the hydrogenating treatment at pressures from 30 to 500 bar, preferably from 50 to 450 bar and particularly preferably from 50 to 350 bar is carried out and at temperatures from 200 to 600 ° C, preferably from 200 to 540 ° C and particularly preferably from 300 to 540 ° C and residence times from 1 minute to 8 hours, preferably from 10 minutes to 6 hours and particularly preferably from 15 minutes up to 4 hours.
  • Rubbing oils can be added to the waste feed products as well as coal, coal components, crude oil, crude oil components and crude oil residues, shale oils and shale oil components, oil sand extracts and their components, bitumen, asphalt, asphaltenes and similar materials.
  • the feed product or the feed mixture can also be treated with solvents and then the extract can be used in the hydrogenating treatment.
  • the pre-sorting of waste materials is preferably carried out in such a way that carbon-containing organic wastes of synthetic origin, such as plastics and mixtures of plastics, rubber, waste tires, textile wastes or mixtures of these materials, as well as further organic synthetic wastes, are at least roughly separated from vegetable waste and / or biomass be and are subsequently subjected to a hydrotreating or the same organic chemicals, waste from industrial plants, organic synthetic shredder waste from the automobile industry, sewage sludge, waste oils or other industrial organic waste olisten mixed with organic industrial waste synthetic origin, such as paints and F, synthetic origin of the Be subjected to hydrogenation.
  • organic wastes of synthetic origin such as plastics and mixtures of plastics, rubber, waste tires, textile wastes or mixtures of these materials, as well as further organic synthetic wastes
  • waste materials such as paper, food scraps, agricultural and forestry waste, plant residues and others can be roughly separated or remain to some extent in the synthetic portion.
  • Household waste can be processed, for example, in such a way that plastics, rubber, textiles and other synthetic materials are roughly separated and separately subjected to a hydrogenation treatment, or mixed with waste tires and / or industrial chemicals and / or plastic waste and / or waste oils and others are subjected to this hydrating treatment.
  • coal components such as, for example, residual oils from coal, coal oils, pyrolysis oils, crude oil, residual oils from crude oil, other crude oil components, oil shale and oil shale components, oil sand extracts, asphalt and Bitumen and similar materials as well as mixtures of these materials.
  • the separation of the above-mentioned inorganic materials from the carbon-containing waste can be carried out according to the prior art. These inorganic materials can be stored in landfills unless they are recycled and reprocessed. The crushing and shredding and separation of waste materials can also be carried out according to the prior art. If this is not contradicted by equipment, the process can also be carried out in the presence of inorganic materials.
  • Waste components that cannot be converted to hydrocarbons such as sulfur, nitrogen, oxygen and halogens in the form of their compounds, are converted into their gaseous hydrogen compounds, namely H 2 S, NH 3 , HC1, H 2 0 and others. These compounds can be separated by gas washing and further work-up according to the prior art.
  • Another advantage of the process is that the formation of hazardous compounds which occur during waste incineration, namely NO, SO or dioxins, is avoided. Furthermore, plastics, such as polyvinyl chloride, which are problematic in combustion, can be obtained without risk the environment.
  • the hydrogenation of carbon-containing waste materials can, according to this disclosure, be carried out with very good results in the absence of catalysts. However, improved results, particularly with regard to the selective formation of certain hydrocarbon fractions, can be obtained in the presence of catalysts, e.g. in the presence of metals and their compounds which are catalytically active in hydrogenation reactions, e.g.
  • catalysts can consist of a single active component or a mixture of at least 2 of the components mentioned, and wherein these metals or their compounds can be used on catalyst supports, such as on aluminum oxide, silicon oxide, aluminum silicate, zeolites and other supports which are known from the prior art, as well as on mixtures of these supports or also without a support. Certain zeolites and other carriers are also active as catalysts in the disclosed process without doping.
  • Suitable catalysts are so-called Wegwerfkata- ysatoren l as lignite coke, gasification dusts and -slag, ash such as high-temperature Winkler dust and ash, dusts and ashes which are obtained in the hydrogenating coal gasification, is formed in the methane (HKV dust) , also materials containing iron oxides such as red mud, Bayer mass, Lux mass, dusts from the steel industry and others.
  • These materials can be used as such as catalysts or doped with metals and / or metal compounds which are active in hydrogenations, in particular with heavy metals and / or their compounds such as Fe, Cr, Zn, Mo, W, Mn, Ni, Co, Pt , Pd, furthermore alkali and alkaline earth metals or their compounds such as Li, Na, K, Rb, Be, Mg, Ca, Sr or Ba and mixtures of these metals and / or their compounds.
  • heavy metals and / or their compounds such as Fe, Cr, Zn, Mo, W, Mn, Ni, Co, Pt , Pd, furthermore alkali and alkaline earth metals or their compounds such as Li, Na, K, Rb, Be, Mg, Ca, Sr or Ba and mixtures of these metals and / or their compounds.
  • the catalysts can optionally be sulfided before or during the process.
  • All catalysts can be used as individual components or in a mixture of at least two of the components.
  • the hydrating treatment can be carried out within wide limits of temperature and pressure, depending on the waste material used, namely from 200-600 ° C. and 30-500 bar, with residence times of 1 minute to 8 hours.
  • the hydrogenation gas can be of different quality, it can contain, for example, certain amounts of CO, CO 2 , H 2 S, methane, ethane, steam and others in addition to hydrogen.
  • Suitable hydrogen qualities are, for example, those which are obtained when gasifying carbon-containing materials.
  • Such materials can be residues from mineral oil processing or other oils or hydrocarbons from mineral oil origin, or coal such as lignite, but also hard coal, wood, peat or residues from coal processing such as coal hydrogenation.
  • Suitable V are ergasungsmaterialien biomass of vegetable and portion vomHausmüll. Of course, pure hydrogen qualities, such as those obtained electrolytically, are also very suitable.
  • Household waste can accordingly be processed in such a way that first a separation into a vegetable and a synthetic part takes place and then the vegetable Portion is gasified to provide hydrogen in the H y, third process, while the synthetic portion is treated with hydrogen.
  • treatment with suitable solvents is also possible, in particular with hydrogen-transferring solvents, this treatment being carried out before the actual hydrogenation.
  • dissolved and undissolved material can be separated from one another and subjected separately to a hydrogenation, or dissolved and undissolved material can be reacted together in a reactor in a hydrogenating manner.
  • the solvent can be separated off and recycled by subsequent distillation.
  • the undissolved material can be subjected to gasification or coking.
  • waste material used can be mixed with coal and coal components, crude oil and crude oil components and other similar materials, as already stated above.
  • Suitable hydrogen-transferring solvents are, for example, tetralin, anthracene oil, isopropanol, oils containing cresols, decalin, naphthalene, tetrahydrofuran, dioxane and other hydrocarbons from crude oil and coal or hydrocarbons which originate from the process itself, and also oxygen-containing hydrocarbons and oils.
  • water and steam can also be added, the latter also being able to be added to the alternative hydrogenating treatments already explained above.
  • the waste material can first of all be separated into a vegetable, bicmass or cellulose fraction and a synthetic fraction, with both fractions being processed separately, and with the vegetable, bicmass or cellulose fraction being split essentially hydrolytically, for example in the presence of bases or acids, this conversion preferably being carried out in the presence of protic solvents, in particular water and alcohols and / or in the presence of carbon monoxide and / or hydrogen and, on the other hand, the essentially synthetic portion of the hydrogenating treatment described above .
  • the pretreatment according to the invention can be carried out in the presence of hydrogen and / or hydrogen-containing gases and / or hydrogen-transferring solvents and in an inert atmosphere or in solvents which do not act as hydrogen transfer agents.
  • the process can also be carried out with or without catalysts.
  • the splitting pretreatment is carried out according to the invention in mixing devices in a general sense, in particular in extruders and mixing / kneading devices, since these generally convey into a downstream apparatus without pulsation.
  • extruders can be used, for example, with single or multiple screw conveyors or, for example, those as described in DE-OS 30 01 318 or in DE-OS 29 49 537, in the latter the screw conveyor (s) behind the actual conveyor section into one extended reaction space protrudes, so that this additional diam by the screw (s).
  • numerous other mixing devices such as kneading disc screw presses, kneaders, hollow screw heat exchangers,
  • Screw kneaders, kneading extruders, stirring apparatuses, continuous mixers, kneaders, grinding devices or mills such as bead, hammer or vibrating mills are suitable for the pretreatment according to the invention.
  • a feed extruder can optionally be connected downstream, which brings about an increase in pressure up to the pressure of the hydrogenation reactor.
  • Apparatus which are very suitable according to the invention are, in particular, apparatus which mix and knead at the same time.
  • the desired plasticization, dispersion, homogenization, degassing and degradation reaction which leads to the desired viscosities, takes place in a particularly suitable manner.
  • the reaction rate can also be increased by improving the mixing.
  • the devices mentioned can optionally also be adapted to certain feedstocks, such as containing gas feeds, feed devices at different points on the pretreatment section, drying, heating and cooling sections, addition devices for liquid feed products and the like. Furthermore, several of the devices mentioned can be connected in series or in parallel so that overall at the input of (the) downstream of the hydrogenation reactor (s) is a feedstock mixture of the desired characteristics is present, in particular with respect to degree of degradation and viscosity by V is-.
  • J e are employed by waste products and biomass in front of the aforementioned devices, for example, coarse mills, cutters, separators for inorganic materials Aufschmelzvortechniken, devices for metal deposition and the like., If necessary. Can also be a G efrierzerkleintation be applied.
  • products with the desired physical states can already be used in the mixing device used for the pretreatment according to the invention.
  • the pretreatment according to the invention is carried out in conjunction with hydrogen, hydrogen-containing gases or hydrogen-transferring solvents, the devices mentioned are preferably selected from the point of view that a sufficient amount of hydrogen required for the reaction reaches the feedstock to be converted.
  • stirring devices for example, stirring devices, mixing / kneading devices, extruders or the devices disclosed in DE-OS 30 01 318 and DE-OS 29 43 537 are suitable or other of the devices mentioned can be used, if appropriate with appropriate feeds for hydrogen.
  • hydrogen can also be supplied upstream of the mixing device.
  • the hydrogenating treatment is carried out in the pretreatment device at a temperature of 75-600 ° C, preferably 75-540 ° C, particularly preferably 120-500 ° C, a pressure of 1-600 bar, preferably 1-500 bar , particularly preferably from 1-350 bar and a residence time from 1 minute to 6 hours, preferably from 1 minute to 4 hours, the desired amount of hydrogen being able to be supplied in one or more stages, depending on the mixing device.
  • the thermal pretreatment is carried out in the mixing device at 75-600 ° C., preferably from 75-540 ° C., particularly preferably at 120-475 ° C., a pressure of 1-600 bar, preferably of 1-500 bar, particularly preferably of 1-350 bar and a residence time of 1 minute to 6 hours, preferably 1 minute to 4 hours.
  • the pretreatment according to the invention in particular in the case of thermal pretreatment, can also be carried out under a pressure lower than 1 bar.
  • inert gas can be introduced in one or more stages, depending on the mixing device used.
  • Inert gases can be, for example, nitrogen, carbon dioxide, steam, carbon monoxide, methane and other low-boiling hydrocarbons, as well as mixtures of these gases.
  • Hydrogen can also be present in small quantities. Small amounts of oxygen or air may also be permitted.
  • mixing devices for hydrating or thermal pretreatment can be combined in parallel connection or in series connection.
  • the gases mentioned can also be added before the actual pretreatment.
  • a hydrogen-transferring solvent or a mixture of such solvents can also be used as such or in combination with additional hydrogen or inert gas.
  • the hydrogenating pretreatment is carried out at a temperature of 75-600 ° C, preferably at 75-540 ° C and particularly preferably at 120-500 ° C, a pressure of 1-600 bar, preferably 1-500 bar and particularly preferably from 1-350 bar and a residence time from 1 minute to 6 hours, preferably from 1 minute to 4 hours.
  • the conversion in the mixing device can also be carried out in the presence of protic solvents, in particular in the presence of water or methanol and / or at least one component from the group: Ethanol, C 3 -C 4 alcohols and higher alcohols.
  • Protic solvents depending on the type of waste used, at least partially lead to hydrolysis. If the reaction is carried out in the pretreatment mixing device, temperatures of 75-600 ° C. are used, preferably from 75-540 ° C and particularly preferably from 120-500 ° C , pressures from 1-600 bar, preferably from 1-500 bar, particularly preferably from 1-350 bar and residence times from 1 minute to 6 hours, preferably from 1 Minute to 4 hours.
  • the hydrolysis can also be carried out in the presence of hydrogen, hydrogen-containing gases or hydrogen-transferring solvents with or without a catalyst or with or without CO. Typical hydrolysis catalysts, such as acids or bases including organic amines, can be used. The catalysts mentioned on pages 6 and 7 can also be included.
  • the pretreatment according to the invention can be carried out in the presence of solvents which do not have a hydrogen transfer effect, such as of aromatics such as benzene, toluene or the xylenes.
  • solvents which do not have a hydrogen transfer effect such as of aromatics such as benzene, toluene or the xylenes.
  • Non-aromatic solvents can also be used, such as saturated or substantially saturated aliphatic hydrocarbons in boiling ranges between, for example, 30 and more than 500 ° C.
  • the high-boiling fractions can, for example, be residual oils, as already mentioned above.
  • the hydrogenating cleavage in the pretreatment device can be set to the desired extent, up to a breakdown as described in the hydrogenating treatment of waste according to DE-PS 34 42 506 or in the European subsequent application No. 85 11 4535.9.
  • a downstream hydrogenation reactor can be dispensed with.
  • the hydrogenating pretreatment can be carried out with or without the catalysts which are disclosed on pages 6 and 7.
  • Catalysts can be introduced into the pretreatment device or added before it.
  • the waste from organic synthetic materials can be converted into liquid hydrocarbons which boil essentially in the naphtha or gasoline range or middle distillate range. Examples of such waste are disclosed on pages 3 and 4.
  • a particular advantage of the method according to the invention results from the fact that the conditions in the pretreatment device can be set so that a product is obtained which can be handled without problems in subsequent steps, for example pumped or conveyed via screw conveyors, the conditions being based on Art of the waste used can be adjusted, which as pointed out above plastic materials, paint residues, paint compositions I ndustriechemikalien such as those that need to be deposited in special dumps according to the prior art, shredded waste from the automobile industry, used lubricating oils, elastomers, fabrics but also in to a certain extent paper, cardboard and other cellulose-containing materials such as wood waste, sawdust or vegetable matter from household waste.
  • the pretreated product can also be conveyed directly from the pretreatment device into the hydrogenation reactor, for example by means of an extruder.
  • the method according to the invention therefore also allows only a little pre-sorted waste to be implemented. However, for reasons of equipment, it is desirable to separate inorganic materials such as stones, metals, glass and others before the pretreatment, at least rough materials.
  • Vegetables can be processed separately, for example by fermentation.
  • An important advantage of the present invention results from the fact that the hydrogenating or thermal pretreatment according to the invention, in combination with the subsequent hydrogenation of the pretreated waste, means that even very inhomogeneous waste mixtures can be used as the feed product, these being converted into valuable liquid hydrocarbons in high yields.
  • the heteroatoms such as oxygen, sulfur, nitrogen or halogens, which are contained in many waste materials, are converted according to the invention into their hydrogen derivatives, which can be worked up further according to the prior art without any problems.
  • halogenated wastes are, for example P olychlorbiphenylene, polyvinyl chloride, fluorine-containing polymers or halogen-containing solvent.
  • a particularly advantageous effect of the thermal or hydrating pretreatment is the result that depends As a result of the temperature, dwell time and pressure, halogens are largely eliminated in the pretreatment, essentially as hydrogen halides. For example, about 90% of the halogen is already removed from waste containing polyvinyl chloride at 250 ° C., a residence time of 30 minutes and a hydrogen or nitrogen pressure of 10 bar or less as hydrogen chloride.
  • Halogen elimination can also be promoted by increasing the temperature and increasing the residence time. Halogen elimination can also be promoted by catalysts such as those mentioned on pages 6 and 7. Such catalysts which are used according to the prior art for the elimination of hydrogen halide, such as Friedel-Crafts catalysts and / or organic amines and / or other basic compounds, can also be used according to the invention. As a result, hydrogen halides can be split off even under mild conditions.
  • materials can also the waste used are added or be added in the preconditioner or the hydrogenation reactor, such as crude oil, R ohölkomponenten and products derived from crude oil, asphalt, bitumen, mineral tars, coal, coal components, products from coal, lignite , Peat, pyrolysis oils such as those obtained from coking processes or pyrolysis processes, oil sands, oil sand products, residual oils from crude oil processing, from cracking plants, vacuum residues, shale oils and shale oil products and similar materials.
  • crude oil, R ohölkomponenten and products derived from crude oil, asphalt, bitumen, mineral tars, coal, coal components, products from coal, lignite , Peat, pyrolysis oils such as those obtained from coking processes or pyrolysis processes, oil sands, oil sand products, residual oils from crude oil processing, from cracking plants, vacuum residues, shale oils and shale oil products and similar materials.
  • a hydrolysis stage can precede the thermal or hydrogenating pretreatment.
  • the hydrolysis reaction is preferably carried out in a mixed premix performed as described above, in the presence of protic solvents - medium, especially in the presence of water and / or methanol and / or at least one component from the group:
  • Ethanol, C 3 -C 4 alcohols and higher alcohols at a pressure of 1-150 bar, preferably of 1-120 bar and a temperature of 50-300 ° C and preferably 75-250 ° C. Lower pressures are preferred if the gases that are formed during the hydrolysis are to be removed from the hydrolysis device.
  • the hydrolysis stage can alternatively be switched between the pretreatment and the actual hydrogenation.
  • the hydrolysis conditions are preferably adapted to the temperature and the pressure in the pretreatment stage or hydrogenation stage or both.
  • vegetables and biomass can be hydrolytically split and separated from waste of synthetic organic origin.
  • the hydrolysis reaction can be accelerated by adding acids or bases in accordance with the prior art.
  • the hydrolytic reaction can also be carried out in the presence of hydrogen, hydrogen-containing gases, hydrogen-transferring solvents, catalysts as exemplified on pages 6 and 7 or solvents which are not suitable for mass transfer, or in the presence of inert gases.
  • So-called Anreiböle may also or adaptationsvortechnisch according to the invention in the V or be added before this or after this.
  • the grinding oils can originate from the process itself or can be of foreign origin.
  • metals or metal compounds which are present in the waste can advantageously be worked up, since they occur in residues or ashes in a relatively high concentration after the hydrogenation. These residues or ashes can be worked up, for example, to obtain the pure metals.
  • Example 1 was repeated, but under a nitrogen pressure of 10 bar. In the case of the temperature of 300 ° C, an additional nitrogen pressure of 2 bar was used. The results are shown in Table 2.
  • a mixture of mineral residual oils and a waste mixture consisting of 10% by weight of old tires, 70% by weight of essentially synthetic-organic waste from a technical waste separation system and 20% by weight of polyvinyl chloride was mixed and kneaded at 350 ° C for 20 minutes and 450 ° C treated with a hydrogen or nitrogen pressure of 200 bar.
  • the ratio of waste to oil was 1: 3.
  • FeSO 4 treated with NaOH was used as the catalyst.
  • Waste which consisted predominantly of organic synthetic material and was obtained from a technical waste sorting plant, with 15% by weight polyvinyl chloride, was treated in a mixer / kneader at 200 bar hydrogen and temperatures of 350 ° C and 470 ° C for 30 minutes each. At the temperature of 350 ° C, an experiment was carried out with and without a catalyst. A nickel / molybdenum catalyst was used as the catalyst. No rubbing oil was used. The viscosities obtained are shown in Table 6.
  • Waste which consisted essentially of organic synthetic material from a technical waste separation plant and which contained 5% by weight of perfluorinated polyethylene (Teflon) and 20% by weight of textile waste from 50% wool and 50% polyacrylonitrile was treated as described in Example 6.
  • the viscosities obtained are shown in Table 8.
  • the results according to the invention are of great importance for waste hydrogenation on an industrial scale, since the downstream hydrogenation reactors and other parts of the plant which are exposed to high pressures can be made from less valuable materials.
  • the process according to the invention is therefore of particular importance for waste feed materials which contain chlorinated constituents.
  • the examples also show that, under suitable conditions and conditions, increased degradation takes place under nitrogen compared to hydrogen.
  • the conditions of the pretreatment can be varied over a wide range of temperature, pressure and residence times, the conditions for the subsequent hydrogenation can also be varied over a wide range, the two treatments complementing one another.
  • the pretreatment according to the invention is carried out at a relatively high temperature and residence time or corresponding pressure, in particular at a relatively high hydrogen pressure
  • the subsequent hydrogenation can, depending on the product used, be carried out under relatively mild conditions. This applies in particular if the pretreatment has already led to extensive dismantling.
  • Both stages therefore complement one another in accordance with the invention and can be adapted excellently to the operational waste material as required.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Treating Waste Gases (AREA)
  • Hydrogen, Water And Hydrids (AREA)
EP87100875A 1986-01-24 1987-01-22 Procédé de récupération de déchets contenant du carbone Expired - Lifetime EP0236701B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87100875T ATE53859T1 (de) 1986-01-24 1987-01-22 Verbessertes verfahren zur wiederaufarbeitung kohlennstoff enthaltender abfaelle.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3602041A DE3602041C2 (de) 1986-01-24 1986-01-24 Verbessertes Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
DE3602041 1986-01-24

Publications (2)

Publication Number Publication Date
EP0236701A1 true EP0236701A1 (fr) 1987-09-16
EP0236701B1 EP0236701B1 (fr) 1990-05-02

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ID=6292497

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87100875A Expired - Lifetime EP0236701B1 (fr) 1986-01-24 1987-01-22 Procédé de récupération de déchets contenant du carbone

Country Status (15)

Country Link
US (1) US4982027A (fr)
EP (1) EP0236701B1 (fr)
JP (1) JPS62253689A (fr)
CN (1) CN87101612A (fr)
AT (1) ATE53859T1 (fr)
AU (1) AU583704B2 (fr)
BR (1) BR8700298A (fr)
CA (1) CA1300540C (fr)
DD (1) DD261170A1 (fr)
DE (2) DE3602041C2 (fr)
ES (1) ES2000077B3 (fr)
GR (2) GR880300006T1 (fr)
IN (1) IN169120B (fr)
PL (1) PL263795A1 (fr)
ZA (1) ZA87408B (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3713730A1 (de) * 1987-04-24 1988-11-10 Union Rheinische Braunkohlen Verbessertes verfahren zur aufarbeitung von kohlenstoff enthaltenden abfaellen und biomasse
EP0512482A2 (fr) * 1991-05-03 1992-11-11 RWE Entsorgung Aktiengesellschaft Procédé por diminuer le dépôt de coke dans le traitement thermique de déchets organiques synthétiques
EP0594165A1 (fr) * 1992-10-22 1994-04-27 KUHNE ANLAGENBAU GmbH Procédé pour le récyclage des déchets thermoplastiques et installation pour la mise en oeuvre de ce procédé
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EP0291698A1 (fr) * 1987-04-24 1988-11-23 RWE Entsorgung Aktiengesellschaft Procédé d'hydrocraquage des déchets synthétiques contenant du carbone
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EP0594165A1 (fr) * 1992-10-22 1994-04-27 KUHNE ANLAGENBAU GmbH Procédé pour le récyclage des déchets thermoplastiques et installation pour la mise en oeuvre de ce procédé
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ATE53859T1 (de) 1990-06-15
IN169120B (fr) 1991-09-07
JPS62253689A (ja) 1987-11-05
GR880300006T1 (en) 1989-06-22
CA1300540C (fr) 1992-05-12
BR8700298A (pt) 1987-12-01
EP0236701B1 (fr) 1990-05-02
GR3000553T3 (en) 1991-07-31
ES2000077A4 (es) 1987-11-16
ZA87408B (en) 1987-08-26
CN87101612A (zh) 1987-10-28
AU583704B2 (en) 1989-05-04
AU6809087A (en) 1987-08-06
DE3602041C2 (de) 1996-02-29
DE3762522D1 (de) 1990-06-07
ES2000077B3 (es) 1990-08-16
DD261170A1 (de) 1988-10-19
PL263795A1 (en) 1988-02-04
DE3602041A1 (de) 1987-07-30
US4982027A (en) 1991-01-01

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