EP0692009B1 - Verfahren zur verarbeitung von alt- oder abfallkunststoffen - Google Patents

Verfahren zur verarbeitung von alt- oder abfallkunststoffen Download PDF

Info

Publication number
EP0692009B1
EP0692009B1 EP94913053A EP94913053A EP0692009B1 EP 0692009 B1 EP0692009 B1 EP 0692009B1 EP 94913053 A EP94913053 A EP 94913053A EP 94913053 A EP94913053 A EP 94913053A EP 0692009 B1 EP0692009 B1 EP 0692009B1
Authority
EP
European Patent Office
Prior art keywords
phase
depolymerization
process according
condensate
subjected
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
EP94913053A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0692009A1 (de
Inventor
Rolf Holighaus
Klaus Niemann
Martin Rupp
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.)
Der Gruene Punkt Duales System Deutschland AG
Original Assignee
Veba Oel AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Veba Oel AG filed Critical Veba Oel AG
Publication of EP0692009A1 publication Critical patent/EP0692009A1/de
Application granted granted Critical
Publication of EP0692009B1 publication Critical patent/EP0692009B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/005—Coking (in order to produce liquid products mainly)
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
    • 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
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • 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
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste

Definitions

  • the invention relates to a method for processing old or waste plastics for the purpose of obtaining chemical raw materials and liquid fuel components.
  • the invention is based on a process for the hydrotreatment of carbon-containing material, in which polymers, in particular polymer wastes in comminuted or dissolved form, are added to a high-boiling oil and this mixture is hydrogenated in the presence of hydrogen in order to obtain fuel components and chemical raw materials (cf. DD 254 207 A1).
  • a process for converting used tires, rubber and / or other plastics into liquid, gaseous and solid products by depolymerizing treatment in a solvent under elevated pressure and elevated temperature has been described in DE-A-25 30 229.
  • no harmful substances such as SO 2 , soot or the like should enter the atmosphere in this process.
  • hydrogen tires were added to a hydrogenation reactor under hydrogenation at a hydrogen pressure of 150 bar and a temperature of 450 ° C. in the presence of substances catalyzing the cleavage and hydrogenation reactions.
  • DE-A-2 205 001 describes a process for the thermal treatment of waste and rubber, in which the waste is split at temperatures from 250 to 450 ° C. in the presence of an auxiliary phase which is liquid at the reaction temperature.
  • a method is also known in which polymer waste, in particular waste rubber, is dissolved in the residue products of petroleum processing. The resulting mixture is then coked to coke. Here there are gaseous and liquid products. The latter are suitable as fuel components when processed accordingly, cf. DD 0 144 171.
  • the polymer concentration in the hydrogenation feed is, for example, between 0.01 and 20% by weight according to the process according to DD 254 207.
  • the joint hydrogenating treatment of heavy oils with dissolved and / or suspended polymers is limited to hydrogenation processes in which the hydrogenation is carried out in tubular reactors with or without a suspended catalyst. If reactors were operated with fixedly arranged catalysts, the use of polymers was only possible to a limited extent, in particular if polymers were added which already depolymerize in the heating phase up to approximately 420 ° C. before the reactor enters.
  • Another task is to relieve or better utilize complex and capital-intensive process steps such as smoldering, gasification or bottom phase hydrogenation with regard to the required throughput quantities.
  • the invention consists in a process for processing waste or waste plastics for the purpose of obtaining chemical raw materials and liquid fuel components by depolymerizing the starting materials without adding hydrogen to a pumpable and a volatile phase, separating the volatile phase into a gas phase and a condensate which is subjected to the standard refinery procedures is, wherein the pumpable phase remaining after separation of the volatile phase is subjected to a bottom phase hydrogenation, gasification, smoldering or a combination of these process steps.
  • the resulting gaseous depolymerization products gas
  • the resulting condensable depolymerization products condensate
  • the pumpable, viscous depolymerization products containing, bottom phase depolymerized product
  • the process parameters are preferably selected so that the highest possible proportion of the so-called condensate is formed.
  • the plastics to be used in the present process are e.g. B. Mixed fractions from waste collections, including by Duale System Kunststoff GmbH (DSD). In these mixed fractions z. B. contain polyethylene, polypropylene, polyvinyl chloride, polystyrene, polymer blends such as ABS and polycondensates. Plastic production waste, commercial packaging waste made of plastic, residual, mixed and pure fractions from the plastic processing industry can also be used, the chemical composition of this plastic waste not being critical for the suitability for use in the present process. Suitable insert products are also elastomers, technical rubber articles or used tires in a suitable pre-shredded form.
  • the used plastics or waste plastics come from molded parts, laminates, composite materials, foils or synthetic fibers, for example.
  • halogen-containing plastics are chlorinated polyethylene (PEC), polyvinyl chloride (PVC), polyvinylidene chloride (PVDC), chloroprene rubber, to name just a few important representatives.
  • sulfur-containing plastics such as polysulfones or rubbers cross-linked with sulfur bridges, such as in old tires, are produced in large quantities and, if the appropriate equipment for pre-shredding and pre-sorting in plastic and metal components is used for depolymerization and further processing to obtain chemical raw materials or fuel components accessible.
  • thermoplastics this also includes thermosets and polyadducts and products based on cellulose such as cellulose and paper.
  • the products made from this include semi-finished products, individual parts, components, packaging, storage and transport containers and consumer goods.
  • the semi-finished products also include boards and boards (printed circuit boards) as well as laminated boards, some of which may still contain metal coatings and which, like the other products to be used, have been pre-shredded to particle or piece sizes of 0.5 to 50 mm, possibly of metal or glass. or ceramic components can be separated using suitable classification processes.
  • the old and waste plastics mentioned generally also contain inorganic secondary components such as pigments, glass fibers, fillers such as titanium or zinc oxide, flame retardants, pigment-containing printing inks, carbon black and also metals such as. B. metallic aluminum.
  • inorganic secondary components such as pigments, glass fibers, fillers such as titanium or zinc oxide, flame retardants, pigment-containing printing inks, carbon black and also metals such as. B. metallic aluminum.
  • the old and waste plastics mentioned, the z. B. from the collections of the DSD in mixtures or batches of different compositions can contain up to 10, possibly up to 20 wt .-% of inorganic minor components.
  • These plastic mixtures are usually used in shredded or preconditioned form z. B. used as granules or chips or the like in the present process:
  • the individual product streams in particular the condensate, can subsequently be processed in the course of further processing in the sense of raw material recycling, eg. B. used as raw materials for olefin production in ethylene plants.
  • An advantage of the process according to the invention is that inorganic secondary constituents of the old or waste plastics are concentrated in the sump phase, while the condensate not containing these constituents can be processed further by less complex processes.
  • by optimally setting the process parameters temperature and residence time it can be achieved that, on the one hand, a relatively high proportion of condensate is formed and, on the other hand, the viscous depolymerizate of the bottom phase remains pumpable under the process conditions.
  • a useful approximation is that an increase in temperature by 10 ° C. with an average residence time increases the yield of the products passing into the volatile phase by more than 50%.
  • the residence time dependency for two typical temperatures is shown in FIG. 3.
  • Typical of the present process is a condensate yield of about 50% by weight and more based on the total amount of the plastics used in the depolymerization. This advantageously considerably relieves the cost-intensive process stages of pressure gasification, bottom phase hydrogenation and smoldering (pyrolysis).
  • the preferred temperature range for the depolymerization for the process according to the invention is 150 to 470 ° C. A range from 250 to 450 ° C. is particularly suitable.
  • the residence time can be 0.1 to 20 hours. A range from 1 to 10 h has proven to be generally sufficient.
  • the pressure is in the invention Procedure a less critical size. So it may be preferable to carry out the process under negative pressure, e.g. B. if volatile components have to be deducted for procedural reasons. Relatively high pressures are also practicable, however, they require more equipment. In general, the pressure should be in the range from 0.01 to 300 bar, in particular 0.1 to 100 bar.
  • the method can preferably be good at normal pressure or slightly above z. B.
  • the depolymerization can preferably be carried out with the addition of a catalyst, for example a Lewis acid such as aluminum chloride, a radical-forming substance such as a peroxide or a metal compound, for example a zeolite impregnated with a heavy metal salt solution.
  • a catalyst for example a Lewis acid such as aluminum chloride, a radical-forming substance such as a peroxide or a metal compound, for example a zeolite impregnated with a heavy metal salt solution.
  • the depolymerization can take place under turbulent flow conditions, e.g. B. by mechanical stirrer, but also by pumping around the reactor contents.
  • inventions of the process consist of depolymerization under inert gas, ie gas which is essentially inert towards the starting materials and depolymerization products, e.g. B. N 2 , CO 2 , CO or hydrocarbons.
  • inert gas ie gas which is essentially inert towards the starting materials and depolymerization products, e.g. B. N 2 , CO 2 , CO or hydrocarbons.
  • stripping gases and stripping vapors such as nitrogen, water vapor or hydrocarbon gases.
  • Suitable liquid auxiliary phases or solvents or solvent mixtures are, for example, used organic solvents, that is to say waste solvents, incorrect production batches of organic liquids, waste oils or fractions from petroleum refining, for example vacuum residues.
  • the depolymerization can be carried out in a conventional reactor, e.g. B. a stirred tank reactor with external circulation, which is designed for the corresponding process parameters, such as pressure and temperature, and whose container material is resistant to the acidic components that may arise, such as hydrogen chloride.
  • a conventional reactor e.g. B. a stirred tank reactor with external circulation, which is designed for the corresponding process parameters, such as pressure and temperature, and whose container material is resistant to the acidic components that may arise, such as hydrogen chloride.
  • suitable "unit operations" methods can be considered, such as those used for the so-called visbreaking of heavy crude oils or of residual oils from mineral oil processing. Possibly. they must be adapted according to the requirements of the method according to the invention.
  • This process stage is advantageously designed for continuous operation, i. H. the plastic is continuously introduced into the liquid phase of the depolymerization reactor and the depolymerizate and top product are continuously removed.
  • the equipment required for depolymerization is comparatively low. This applies in particular if the process is carried out in the vicinity of normal pressure, ie in the range from 0.2 to 2 bar. In comparison to hydrogenating pretreatments, the expenditure on equipment is also significantly lower. With optimal depolymerization process control, the subsequent process steps can be relieved by up to 50% and more. At the same time, a large proportion of condensable hydrocarbons is deliberately produced in the depolymerization, which can be worked up to valuable products by known and comparatively inexpensive processes.
  • the depolymerizate is easy to handle, since it remains pumpable and, in this form, is a good starting material for the subsequent process stages.
  • the depolymerized material and the condensate are worked up separately from one another.
  • the condensable depolymerization products are preferably subjected to a hydrogenating refining on fixed granular catalyst.
  • the condensate can be subjected to conventional hydrotreating using commercially available nickel / molybdenum or cobalt / molybdenum contacts at hydrogen partial pressures of 10 to 250 bar and temperatures of 200 to 430 ° C.
  • a guard bed for trapping entrained ash components or coke-forming components is expediently connected upstream.
  • the contact is arranged on solid trays as usual and the direction of flow of the condensate can be provided from the tray towards the top of the hydrotreating column or in the opposite direction.
  • acidic components such as hydrogen halide, hydrogen sulfide and. The like.
  • the feeding of water, alkali compounds and possibly corrosion inhibitors into the condensation part of appropriate separators is expedient.
  • the condensable depolymerization products or the condensate can also be subjected to hydrogenating refining on a moving catalyst or in a flowing catalyst bed.
  • the condensate obtained during the depolymerization is, for example, an excellent starting material for a steam cracker after it has passed through the hydrotreater.
  • the Z. B. liquid product obtained in the hydrotreater is processed as synthetic crude oil (syncrude) in conventional refinery structures for the production of fuel components or as a chemical raw material, for example for ethylene production in ethylene plants.
  • gaseous components obtained during hydrotreating are suitable, for example, to be added to the products used for steam reforming.
  • At least a partial stream of the depolymerizate is subjected to pressure gasification.
  • all entrained-flow carburettors (Texaco, Shell, Prenflo), fixed bed carburettors (Lurgi, Espag) and Ziwi carburettors are suitable as devices for pressure gasification.
  • Processes for the thermal decomposition of hydrocarbons with oxygen are particularly suitable, as are carried out in processes of oil gasification by partial oxidation of the hydrocarbons as a flame reaction in a combustion chamber. The reactions are autothermal - not catalytic.
  • the crude gas which essentially consists of CO and H 2 and is produced in the pressure gasification, can be worked up to synthesis gas or used to generate hydrogen.
  • At least a partial stream of the depolymerizate is fed to a bottom phase hydrogenation.
  • the bottom phase hydrogenation is particularly preferred when a high proportion of liquid hydrocarbons is to be obtained from the depolymerizate.
  • the bottom phase hydrogenation of the pumpable liquid-viscous depolymerizate is carried out, for example, in such a way that any petroleum-derived vacuum residue is mixed in and hydrogenation gas is added after compression to 300 bar.
  • the reaction material passes through heat exchangers connected in series, in which the heat exchange with product streams takes place, for example, a hot separator top product.
  • the reaction mixture which has been preheated to typically 400 ° C., is further heated to the desired reaction temperature and then fed to the reactor or a reactor cascade in which the bottom phase hydrogenation takes place.
  • the gaseous components at reaction temperature are separated from liquid and solid components under process pressure.
  • the latter also contain the inorganic minor components.
  • the heavier oil components are separated from the gaseous fraction in a separator, which can be fed to an atmospheric distillation after expansion.
  • the process gases are first removed from the uncondensed portion, which are worked up in a gas scrubber and recycled as recycle gas.
  • the remaining amount of the hot separator product is, for example, freed from the process water after further cooling and fed to an atmospheric column for further processing.
  • the bottom draw of the hot separator can expediently be expanded in two stages and subjected to vacuum distillation to remove residual oil.
  • the thickened residue which also contains the inorganic secondary constituents, can be fed to the gasification device in liquid or solid form for the purpose of generating synthesis gas.
  • the residues obtained in the bottom phase hydrogenation (hot separator residue) and the smoldering coke obtained when the depolymerizate smells, each containing the inorganic secondary constituents, can be utilized by a further thermal process step, the residues obtained there containing the inorganic secondary constituents e.g. B. can be further processed for the purpose of metal recovery.
  • the light and medium oil fractions obtained from the bottom phase hydrogenation can be used in refinery structures as valuable raw materials for the production of fuels or plastic precursors such as olefins or aromatics. If these products from the bottom phase hydrogenation should not be stable in storage, they can be subjected to the hydrotreating treatment provided for condensate or condensable components in the present process.
  • a preferred embodiment of the process according to the invention consists in that the pumpable viscous depolymerizate, after separating off the gaseous and condensable depolymerization products as a liquid product, is each divided into a partial gasification which is to be pressurized and also a partial stream to be fed to a bottom phase hydrogenation.
  • the division of the pumpable viscous depolymerizate according to the invention into one partial pressure gasification and one partial phase hydrogenation and possibly pyrolysis feed in connection with the separate processing of the condensable components in a hydrotreating step leads to one significantly improved plant utilization.
  • Devices such as those developed for the pressure gasification of solid fuels or for the thermal decomposition of hydrocarbons with oxygen or in plants for the sump phase hydrogenation of carbon-containing materials under high pressure are very capital-intensive plant parts, the throughput capacity of which is optimally used when it is used by Feed materials are relieved, as previously separated in the present process as a condensate stream and subjected to a separate workup in a hydrotreater under comparatively mild process conditions.
  • Another preferred option of the present method is to subject at least a partial stream of the depolymerization to a smoldering process to obtain smoldering gas, smoldering tar and smoldering coke.
  • the gaseous hydrogen chloride gas or condensable in the form of an aqueous solution during depolymerization can be used separately in the sense of material recycling. Remaining fractions which are not components of the gaseous depolymerization products which can be condensed as a liquid product yield and which u. a. chlorine-organic as well as sulfur- and nitrogen-containing compounds can be freed from the heteroatoms chlorine, sulfur, nitrogen or oxygen in the course of the bottom phase hydrogenation or the residue processing integrated into the same, which are separated off as hydrogen compounds.
  • the gaseous depolymerization products if appropriate freed from acidic components such as hydrogen halides, can preferably be fed to the hydrogen feed gas or the hydrogen cycle gas of the bottom phase hydrogenation.
  • the combination of depolymerization, hydrogenating treatment of the preferred distillate components, bottom phase hydrogenation, gasification (partial oxidation) and / or smoldering of the depolymerizate of the bottom phase means that the latter treatment stages, which are technologically particularly complex and complex but tolerate inorganic ingredients, can be relieved in terms of capacity.
  • the method according to the invention offers a high material recycling potential of the plastics used.
  • a flow chart for the system configuration according to FIG. 1 is given as follows in the sense of an exemplary embodiment for the specified feed products.
  • the appropriately comminuted, possibly washed and dried waste plastic is continuously fed to the depolymerization reactor 1, which is provided with heating, stirring, pressure-maintaining devices, associated inlet and outlet valves and measuring and control devices for checking the level.
  • 25.0% by weight of the bottom phase hydrogenation 3 and 25.0% by weight of the gasification device 4 are fed in from the depolymerizate.
  • 25.0% by weight of vacuum residue are fed to the bottom phase hydrogenation 3 as a recycle stream.
  • the reaction product of the gasification device consists in a typical procedure of 24.0% by weight of a synthesis gas and approximately 1.0% by weight of an ash-containing soot.
  • the product stream of the depolymerizate from reactor 1 can be partly fed to pyrolysis or smoldering plant 5 for the production of pyrolysis coke, smoldering tar and smoldering gas.
  • the pyrolysis coke is fed to the gasification device, the smoldering tar and the smoldering gas of the bottom phase hydrogenation.
  • the inorganic secondary constituents enriched in the depolymerizate are further concentrated in the subsequent workup. If the depolymerizate is fed to gasification, the inorganic secondary components are subsequently found in the discharged slag. In the case of the bottom phase hydrogenation, they are contained in the hydrogenation residue and in the smoldering in the smoked coke. If the hydrogenation residue and / or the smoked coke are also fed to the gasification, all of the inorganic secondary constituents entered in the process according to the invention leave the processing stage as gasification slag.
  • the old or waste plastic enters the silo 1 and from there into the reactor 2 via the conveying device 16.
  • the reactor contents are heated by means of a circulation system consisting of a circulation pump 4 and a furnace 3.
  • a stream is withdrawn from the circulation via the suspension pump 5, which flow into the insert container 6
  • Vacuum residue supplied via line 14 is mixed and then fed to further processing via high pressure pump 7.
  • the gases and condensable components formed in reactor 2 are passed through condenser 8 and separated. After passing through hydrochloric acid washer 9, the cleaned gases 10 are passed on for further use.
  • the acid components previously contained are removed after washing as aqueous hydrochloric acid 12.
  • the condensate separated in condenser 8 is fed from there for further use.
  • the plastic mixture was depolymerized in the reactor at temperatures between 360 ° C and 420 ° C. Four fractions were formed, the quantity distribution depending on the reactor temperature is shown in the following table:
  • the depolymerized material stream (III) was drawn off continuously and fed to a bottom phase hydrogenation plant together with petroleum-derived vacuum residue for further cleavage.
  • the viscosity of the depolymerizate was 200 mPas at 175 ° C.
  • the hydrocarbon condensates (stream II) were condensed in a separate plant and sent for further processing in a hydrotreater.
  • the gaseous hydrogen chloride (stream IV) was taken up with water and released as 30% aqueous hydrochloric acid.
  • the hydrocarbon gases (stream 1) were fed to the bottom phase hydrogenation plant for conditioning.
  • Condensate from a depolymerization plant which was obtained at a temperature between 400 and 420 ° C from a plastic mixture (DSD house collection), was freed of HCI by washing with ammoniacal solution. It then had a Cl content of 400 ppm.
  • This pretreated condensate was subjected to a catalytic dechlorination process in a continuously operating apparatus.
  • the condensate was first compressed to 50 bar and then subjected to hydrogen, so that a gas / condensate ratio of 1000 l / kg was maintained.
  • the mixture was heated and reacted in a fixed bed reactor over a NiMo catalyst. After leaving the reactor, the reaction mixture was quenched with ammoniacal water so that the HCl formed completely passed into the aqueous phase. Before the reaction mixture was let down, a gas / liquid phase separation was carried out so that the gas and liquid phases could be released separately. After relaxation, the liquid phase was broken down into an aqueous and an organic phase.
  • the organic phase which represented more than 90% by weight of the condensate used, showed the following Cl contents [ppm] depending on the chosen reaction conditions: Temperature [° C] WHSV [kg oil / kg cat./h] 0.5 1 2nd 370 - ⁇ 1 3rd 390 3rd ⁇ 1 ⁇ 1 410 ⁇ 1 ⁇ 1

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
EP94913053A 1993-04-03 1994-03-25 Verfahren zur verarbeitung von alt- oder abfallkunststoffen Expired - Lifetime EP0692009B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4311034A DE4311034A1 (de) 1993-04-03 1993-04-03 Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoff
DE4311034 1993-04-03
PCT/EP1994/000954 WO1994022979A1 (de) 1993-04-03 1994-03-25 Verfahren zur verarbeitung von alt- oder abfallkunststoffen

Publications (2)

Publication Number Publication Date
EP0692009A1 EP0692009A1 (de) 1996-01-17
EP0692009B1 true EP0692009B1 (de) 1997-05-28

Family

ID=6484696

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94913053A Expired - Lifetime EP0692009B1 (de) 1993-04-03 1994-03-25 Verfahren zur verarbeitung von alt- oder abfallkunststoffen

Country Status (23)

Country Link
US (1) US5849964A (pl)
EP (1) EP0692009B1 (pl)
JP (2) JP3385025B2 (pl)
KR (2) KR100293752B1 (pl)
CN (1) CN1049237C (pl)
AT (1) ATE153692T1 (pl)
AU (1) AU681652B2 (pl)
BG (1) BG62572B1 (pl)
CA (1) CA2158032A1 (pl)
CZ (1) CZ292837B6 (pl)
DE (3) DE4311034A1 (pl)
DK (1) DK0692009T3 (pl)
ES (1) ES2104375T3 (pl)
FI (1) FI954685L (pl)
GR (1) GR3024422T3 (pl)
HU (1) HU218853B (pl)
NO (1) NO953758D0 (pl)
NZ (1) NZ265043A (pl)
PL (1) PL178639B1 (pl)
RU (1) RU2127296C1 (pl)
SK (1) SK280953B6 (pl)
UA (2) UA39203C2 (pl)
WO (1) WO1994022979A1 (pl)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005010151B3 (de) * 2005-03-02 2006-09-14 Clyvia Technology Gmbh Verfahren zum katalytischen Depolymerisieren von kohlenwasserstoffhaltigen Rückständen sowie Vorrichtung zum Durchführen dieses Verfahrens
DE102008021629B4 (de) * 2008-04-25 2017-09-14 Technische Werke Ludwigshafen Ag Vorrichtung zur Herstellung von Roh-, Brenn- und Kraftstoffen aus organischen Substanzen

Families Citing this family (142)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4323320C2 (de) * 1993-07-06 2003-05-08 Hendrickx Heinz Verfahren zur Trennung, Reinigung, Sortierung und zum Recycling von Mischungen und/oder Verbunden von Kunststoffen untereinander und/oder mit anderen Werkstoffen mit Lösungsmittelverfahren
DE4328188C2 (de) * 1993-08-21 1996-04-18 Hoechst Ag Verfahren zur Herstellung von Synthesegas
DE4344311A1 (de) * 1993-12-23 1995-06-29 Linde Ag Verfahren und Vorrichtung zur thermischen Depolymerisation von Kunststoffen
DE4428355A1 (de) * 1994-05-20 1996-02-15 Veba Oel Ag Vorrichtung zur Depolymerisation von Alt- und Abfallkunststoffen
RU2151163C1 (ru) * 1994-10-04 2000-06-20 Феба Ель АГ Способ использования пластмассовых вторичных материалов или отходов
DE19504595A1 (de) * 1995-02-11 1996-08-14 Basf Ag Verfahren zur gemeinsamen Hydrierung von kohlenwasserstoffhaltigen Gasen und Kondensaten
DE19516379A1 (de) * 1995-05-04 1996-11-07 Veba Oel Ag Verfahren zur Verarbeitung von Alt- oder Abfallkunststoffen
NL1006179C2 (nl) * 1997-05-30 1998-12-01 Alcoa Nederland Bv Werkwijze voor het verwerken van materiaal uit aluminium en kunststof.
NL1007710C2 (nl) * 1997-12-05 1999-06-08 Gibros Pec Bv Werkwijze voor het verwerken van afval- respectievelijk biomassamateriaal.
HU218968B (hu) * 1997-12-05 2001-01-29 Tvk-Ecocenter Kft. Eljárás vegyes műanyaghulladék átalakítására
KR100322663B1 (ko) * 2000-03-20 2002-02-07 곽호준 폐플라스틱을 이용한 휘발유, 등유 및 경유의 연속식제조방법 및 그 시스템
RU2156270C1 (ru) * 2000-03-21 2000-09-20 Общество с ограниченной ответственностью "Научно-экологические программы" Способ переработки резиносодержащих и органических промышленных и бытовых отходов
WO2002010228A2 (en) * 2000-07-27 2002-02-07 E.I. Dupont De Nemours And Company Transformation of polymers to useful chemicals by oxidation
DE10049377C2 (de) * 2000-10-05 2002-10-31 Evk Dr Oberlaender Gmbh & Co K Katalytische Erzeugung von Dieselöl und Benzinen aus kohlenwasserstoffhaltigen Abfällen und Ölen
PL351272A1 (en) * 2001-12-19 2003-06-30 Igor Skworcow Method of and an apparatus for obtaining ronnage carbon and engine fuel while processing used tyres and other polymeric wastes
US6822126B2 (en) * 2002-04-18 2004-11-23 Chevron U.S.A. Inc. Process for converting waste plastic into lubricating oils
US6703535B2 (en) 2002-04-18 2004-03-09 Chevron U.S.A. Inc. Process for upgrading fischer-tropsch syncrude using thermal cracking and oligomerization
US6774272B2 (en) 2002-04-18 2004-08-10 Chevron U.S.A. Inc. Process for converting heavy Fischer Tropsch waxy feeds blended with a waste plastic feedstream into high VI lube oils
RU2223172C2 (ru) * 2002-04-25 2004-02-10 Денисов Михаил Владимирович Устройство для утилизации отходов резинотехнических изделий
RU2231536C1 (ru) * 2002-12-24 2004-06-27 Государственное образовательное учреждение высшего профессионального образования Тюменский государственный нефтегазовый университет Способ переработки твердых бытовых отходов
DE10356245B4 (de) * 2003-12-02 2007-01-25 Alphakat Gmbh Verfahren zur Erzeugung von Dieselöl aus kohlenwasserstoffhaltigen Reststoffen sowie eine Vorrichtung zur Durchführung dieses Verfahrens
EP1716920A4 (en) * 2004-02-13 2013-11-06 Univ Osaka Prefect Public Corp METHOD FOR PRODUCING A PRODUCT DECOMPOSED WITH SUBCITRIC WATER AND DECORATIVE TREATMENT DEVICE WITH UNDERCRITICAL WATER
EA010464B1 (ru) * 2004-02-26 2008-08-29 Игорь Антонович Рожновский Устройство для переработки углеродсодержащих отходов
EP1725633B1 (en) * 2004-03-14 2018-10-24 Future Energy Investments Pty Ltd Process and plant for conversion of waste material to liquid fuel
DE102004038220B4 (de) 2004-08-05 2009-07-23 Proton Technology Gmbh I.Gr. Thermische Biomassenverölung
AP2676A (en) * 2006-08-01 2013-05-30 Vwp Waste Proc Ltd Recycling of waste material
US8193403B2 (en) 2006-08-24 2012-06-05 Agilyx Corporation Systems and methods for recycling plastic
US7758729B1 (en) * 2006-08-24 2010-07-20 Plas2Fuel Corporation System for recycling plastics
US8192586B2 (en) 2010-03-31 2012-06-05 Agilyx Corporation Devices, systems, and methods for recycling plastic
WO2008055149A2 (en) * 2006-10-30 2008-05-08 University Of Utah Research Foundation Blending plastic and cellulose waste products for alternative uses
ITBO20070104A1 (it) * 2007-02-21 2008-08-22 Kdvsistemi Brevetti S R L Apparato per la produzione di combustibile sintetico
US20080295390A1 (en) * 2007-05-04 2008-12-04 Boykin Jack W System for the production of synthetic fuels
US7626062B2 (en) 2007-07-31 2009-12-01 Carner William E System and method for recycling plastics
ITBO20070770A1 (it) * 2007-11-22 2009-05-23 Vuzeta Brevetti S R L Metodo e apparato per il trattamento di materiali di rifiuto
DE102008003837B4 (de) * 2008-01-04 2010-10-07 Wolf Eberhard Nill Verfahren zur Reinigung von organischen Reststoffen in einer Vorstufe der Thermolyse und Vorrichtung zur Durchführung des Verfahrens
EP2082857B1 (de) 2008-01-25 2011-07-13 Ekotoner Ltd. Verfahren und Anlage zur Behandlung von Tonerbehältern und Kartuschen als gefährlicher Büroabfall zum Zweck einer Wiederverwertung
GB0801787D0 (en) * 2008-01-31 2008-03-05 Reclaim Resources Ltd Apparatus and method for treating waste
US20090299110A1 (en) * 2008-05-30 2009-12-03 Moinuddin Sarker Method for Converting Waste Plastic to Lower-Molecular Weight Hydrocarbons, Particularly Hydrocarbon Fuel Materials, and the Hydrocarbon Material Produced Thereby
PL218781B1 (pl) 2009-05-25 2015-01-30 Bl Lab Spółka Z Ograniczoną Odpowiedzialnością Sposób wytwarzania wysokowartościowych produktów węglowodorowych z odpadowych tworzyw sztucznych i układ do sposobu wytwarzania wysokowartościowych produktów węglowodorowych z odpadowych tworzyw sztucznych
FR2946054B1 (fr) * 2009-06-02 2012-09-28 Alfyma Ind Procede de transformation de granulats de caoutchouc pour produire du carbonisat semi-actif et du plastifiant.
RU2430121C2 (ru) * 2009-10-14 2011-09-27 Институт Катализа Им. Г.К. Борескова Сибирского Отделения Российской Академии Наук Способ утилизации отходов полимеров
PL2516592T3 (pl) * 2009-12-22 2019-04-30 Plastic Energy Ltd Przeróbka odpadowego materiału tworzywa sztucznego na paliwo
ES2448956T3 (es) * 2010-01-22 2014-03-17 Erema Engineering Recycling Maschinen Und Anlagen Gesellschaft M.B.H. Procedimiento para el acondicionamiento y detoxificación de un material
JP2013523944A (ja) * 2010-03-31 2013-06-17 アジリックス コーポレイション プラスチックをリサイクルするためのシステムおよび方法
CA2797282A1 (en) * 2010-04-23 2011-10-27 Regenerative Sciences Patents Limited Method and system for hydrocarbon extraction
US8664458B2 (en) * 2010-07-15 2014-03-04 Greenmantra Recycling Technologies Ltd. Method for producing waxes and grease base stocks through catalytic depolymerisation of waste plastics
US20130118075A1 (en) * 2010-07-19 2013-05-16 Get Patent B.V. System And Method For Thermal Conversion Of Carbon Based Materials
JP5721832B2 (ja) * 2010-08-26 2015-05-20 アーハーデー ヴァジョンケゼルー エーエシュ タナーチャドゥー カーエフテー． Ｐｖｃおよびハロゲン含有ポリマー廃棄物を含有する他の廃棄物の熱分解のための方法
US8969638B2 (en) 2010-11-02 2015-03-03 Fina Technology, Inc. Depolymerizatin of plastic materials
US8480880B2 (en) 2011-01-18 2013-07-09 Chevron U.S.A. Inc. Process for making high viscosity index lubricating base oils
MY150550A (en) * 2011-07-22 2014-01-30 Shamsul Bahar Bin Mohd Nor Thermal de-polymerization process of plastic waste materials
DE202011105051U1 (de) 2011-08-31 2011-10-28 Georg Bogdanow Anlage zur Konvertierung von Wertstoffen
DE102011111526B4 (de) 2011-08-31 2014-06-26 Georg Bogdanow Verfahren zur Konvertierung von Wertstoffen
WO2014106650A2 (de) 2013-01-03 2014-07-10 EZER, Argun Verfahren und vorrichtungen zur verölung von kohlenwasserstoffhaltigem eingangsmaterial
CA3229291A1 (en) * 2013-01-17 2014-07-24 Greenmantra Recycling Technologies Ltd. Catalytic depolymerisation of polymeric materials
US9162944B2 (en) 2013-04-06 2015-10-20 Agilyx Corporation Systems and methods for conditioning synthetic crude oil
PL229433B1 (pl) 2014-09-05 2018-07-31 Realeco Spolka Z Ograniczona Odpowiedzialnoscia Addytyw mineralny, zwłaszcza do stosowania w procesie ciągłego przetwarzania odpadowych tworzyw sztucznych, sposób, w którym wykorzystuje się ten addytyw oraz urządzenie do realizacji tego sposobu
WO2016142805A1 (en) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. Process for dechlorination of hydrocarbon streams and pyrolysis oils
WO2016142809A1 (en) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. A robust integrated process for conversion of waste plastics to final petrochemical products
WO2016142808A1 (en) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. An integrated process for conversion of waste plastics to final petrochemical products
WO2016142807A1 (en) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. Process for preparation of hydrocracking catalyst for use in hydrocracking of hydrocarbon streams
WO2016142806A1 (en) * 2015-03-10 2016-09-15 Sabic Global Technologies, B.V. Process for hydrocracking of hydrocarbon streams and pyrolysis oils
HUE052530T2 (hu) 2015-07-23 2021-05-28 Hoval Ag Hõátadó csõ és ilyen hõátadó csõvel rendelkezõ fûtõkazán
RU2617213C2 (ru) * 2015-08-18 2017-04-24 Федеральное государственное бюджетное образовательное учреждение высшего образования "Тверской государственный технический университет" (ТвГТУ) Способ утилизации полимерных отходов методом низкотемпературного каталитического пиролиза
US10472487B2 (en) 2015-12-30 2019-11-12 Greenmantra Recycling Technologies Ltd. Reactor for continuously treating polymeric material
AU2017218908B2 (en) 2016-02-13 2021-11-04 Greenmantra Recycling Technologies Ltd. Polymer-modified asphalt with wax additive
CN108884264A (zh) 2016-03-24 2018-11-23 绿色颂歌再生科技有限公司 作为用于聚合物的熔体流动改性剂和加工助剂的蜡
EP3484980A1 (en) * 2016-07-13 2019-05-22 SABIC Global Technologies B.V. A process which does simultaneous dehydrochlorination and hydrocracking of pyrolysis oils from mixed plastic pyrolysis while achieving selective hydrodealkylation of c9+ aromatics
US10717936B2 (en) * 2016-08-01 2020-07-21 Sabic Global Technologies B.V. Catalytic process of simultaneous pyrolysis of mixed plastics and dechlorination of the pyrolysis oil
US10829696B2 (en) * 2016-08-01 2020-11-10 Sabic Global Technologies B.V. Dechlorination of mixed plastics pyrolysis oils using devolatilization extrusion and chloride scavengers
EP4640721A3 (en) 2016-09-29 2025-12-31 GreenMantra Recycling Technologies Ltd REACTOR FOR PROCESSING POLYSTYRENE MATERIAL
WO2018069794A1 (en) * 2016-10-11 2018-04-19 Sabic Global Technologies, B.V. Maximizing high-value chemicals from mixed plastic using different steam-cracker configurations
WO2018129298A1 (en) * 2017-01-06 2018-07-12 Smart Tire Recycling, Inc. Continuous recycling of rubber and organic polymers using supercritical water oxidation closed system
PL231852B1 (pl) * 2017-05-03 2019-04-30 Handerek Adam Tech Recyklingu Sposób wytwarzania paliw węglowodorowych z odpadowych tworzyw poliolefinowych
ES2696756A1 (es) 2017-07-17 2019-01-17 Hidalgo Navas Jeronimo Procedimiento de recuperación y transformación de plástico líquido ABS
CA3083380A1 (en) 2017-11-28 2019-06-06 Greenmantra Recycling Technologies Ltd. Encapsulation of modifiers in depolymerized products
CN108203588B (zh) * 2018-01-30 2021-02-09 中国石油大学(华东) 一种氮气氛围低温热解处理废轮胎的方法
JP2021525816A (ja) 2018-05-31 2021-09-27 グリーンマントラ リサイクリング テクノロジーズ リミテッド 解重合ポリスチレンを介して得られるスチレン系ポリマーの使用
NO345506B1 (en) * 2018-07-06 2021-03-15 Quantafuel As Production of hydrocarbon fuels from waste plastic
US10723858B2 (en) 2018-09-18 2020-07-28 Greenmantra Recycling Technologies Ltd. Method for purification of depolymerized polymers using supercritical fluid extraction
DE102019001696B4 (de) * 2019-03-11 2026-05-07 Olaf Heimbürge Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien
CN113853418A (zh) 2019-05-22 2021-12-28 沙特基础全球技术有限公司 处理和蒸汽裂化塑料衍生油和废润滑油的组合以生产高价值化学品
EP4055104A4 (en) 2019-12-11 2023-12-13 GreenMantra Recycling Technologies Ltd COMPOSITION OF POLYMERS FROM THE MALEINATION OF DEPOLYMERIZED POLYPROPYLENE
KR20220119411A (ko) 2019-12-23 2022-08-29 셰브런 유.에스.에이.인크. 정제 원유장치를 통한 플라스틱 폐기물의 폴리에틸렌으로의 순환 경제
JP7623381B2 (ja) 2019-12-23 2025-01-28 シェブロン ユー．エス．エー． インコーポレイテッド 精製ｆｃｃユニットを介したポリプロピレンへの廃プラスチックのサーキュラーエコノミー
US11174437B2 (en) 2019-12-23 2021-11-16 Chevron U.S.A. Inc. Circular economy for plastic waste to polypropylene via refinery FCC and alkylation units
US11518944B2 (en) 2019-12-23 2022-12-06 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery FCC and alkylation units
EP4081616A4 (en) 2019-12-23 2024-02-28 Chevron U.S.A. Inc. CIRCULAR ECONOMY OF POLYETHYLENE PLASTIC WASTE AND CHEMICALS THROUGH A RAW REFINERY UNIT
WO2021133887A1 (en) 2019-12-23 2021-07-01 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene and lubricating oil via crude and isomerization dewaxing units
MX2022007042A (es) 2019-12-23 2022-10-27 Chevron Usa Inc Economia circular para residuos plasticos en polipropileno y aceite lubricante a traves de craqueo catalitico de fluidos (fcc) de refineria y unidades de desparafinado por isomerizacion.
CN119912727A (zh) * 2020-01-23 2025-05-02 普莱米尔塑料公司 用于解聚废塑料的方法和系统
CN115052728A (zh) * 2020-02-10 2022-09-13 伊士曼化工公司 溶剂分解副产物流的化学回收
US11566182B2 (en) 2020-03-30 2023-01-31 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery FCC feed pretreater and FCC units
US11306253B2 (en) 2020-03-30 2022-04-19 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery FCC or FCC/alkylation units
CA3164220C (en) 2020-03-30 2026-06-16 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via refinery fcc or fcc/alkylation units
US11639472B2 (en) 2020-04-22 2023-05-02 Chevron U.S.A. Inc. Circular economy for plastic waste to polyethylene via oil refinery with filtering and metal oxide treatment of pyrolysis oil
MX2022012742A (es) 2020-04-22 2022-11-07 Chevron Usa Inc Economia circular de residuos plasticos a polipropileno mediante una refineria de aceite con filtracion y tratamiento con oxido metalico del aceite de pirolisis.
IT202000014629A1 (it) 2020-06-18 2021-12-18 Eni Spa Composizione di materiale plastico e procedimento per il trattamento di materie plastiche per formare detta composizione.
FI130263B (en) * 2020-08-20 2023-05-19 Teknologian Tutkimuskeskus Vtt Oy Method and process arrangement for producing hydrocarbons and use
WO2022056212A1 (en) 2020-09-14 2022-03-17 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
US11518942B2 (en) 2020-09-28 2022-12-06 Chevron Phillips Chemical Company Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular
ES3034448T3 (en) 2020-12-10 2025-08-18 Agilyx Corp Systems and methods for recycling waste plastics
FI130057B2 (en) 2020-12-30 2025-05-21 Neste Oyj Process for processing liquid waste polymers
FI130067B2 (en) 2020-12-30 2025-05-21 Neste Oyj Process for processing liquid waste polymers
KR20230153399A (ko) 2021-03-10 2023-11-06 에코랍 유에스에이 인코퍼레이티드 플라스틱-유도된 합성 공급원료를 위한 안정제 첨가제
AU2022258316A1 (en) 2021-04-16 2023-10-05 Chevron Phillips Chemical Company Lp Pyrolysis of plastic waste to produce light gaseous hydrocarbons and integration with an ethylene cracker
US20240279553A1 (en) * 2021-06-22 2024-08-22 Sabic Global Technologies B.V. Process for conversion of waste plastics into hydrocarbons
EP4416248A1 (en) 2021-10-14 2024-08-21 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks
CN116355643B (zh) * 2021-12-29 2024-07-05 深圳清研紫光检测技术有限公司 水热处理聚烯烃塑料的方法
IT202200000365A1 (it) * 2022-01-12 2023-07-12 Itelyum Regeneration S P A Procedimento per lo smaltimento di pneumatici
WO2023144632A1 (en) 2022-01-25 2023-08-03 Brasem S.A. Methods and systems for co-feeding waste plastics into a refinery
JP7870171B2 (ja) 2022-01-27 2026-06-04 Ｅｎｅｏｓ株式会社 化成品及び炭化物の製造方法
JP7870170B2 (ja) * 2022-01-27 2026-06-04 Ｅｎｅｏｓ株式会社 化成品の製造方法
US20250136780A1 (en) * 2022-02-08 2025-05-01 Bridgestone Corporation Method of decomposing crosslinked rubber
EP4477696A4 (en) * 2022-02-08 2025-09-24 Bridgestone Corp PROCESS FOR DECOMPOSITION OF CROSSLINKED RUBBER
US20250115732A1 (en) * 2022-02-08 2025-04-10 Bridgestone Corporation Method for decomposing crosslinked rubber
CA3255147A1 (en) 2022-04-01 2023-10-05 Chevron U.S.A. Inc. CIRCULAR ECONOMY FOR POLYPROPYLENE PLASTIC WASTE AND BASE OIL VIA A REFINERY HYDROCRACKER UNIT
CN119032151A (zh) 2022-04-01 2024-11-26 雪佛龙美国公司 通过精炼厂加氢裂化装置从塑料废物到聚乙烯和基础油的循环经济
KR20240171115A (ko) 2022-04-01 2024-12-06 셰브런 유.에스.에이.인크. 플라스틱 폐기물을 정제소 fcc 유닛을 통해 폴리프로필렌으로 전환하는 순환 경제
WO2023192461A1 (en) 2022-04-01 2023-10-05 Chevron U.S.A. Inc. Process for stable blend of waste plastic with petroleum feed for feeding to oil refinery units and process of preparing same
GB2618830B (en) * 2022-05-19 2024-09-11 Quantafuel Asa Processing of plastic
US12460138B2 (en) 2022-07-08 2025-11-04 Chevron U.S.A. Inc. Blend of waste plastic with bio feed and process of preparation
US11802250B1 (en) * 2022-11-10 2023-10-31 Chevron Phillips Chemical Company Lp Systems and processes for processing pyrolysis oil
US12415958B2 (en) 2022-12-12 2025-09-16 Chevron U.S.A. Inc. Process for stable blend of waste plastic with petroleum feed for feeding to oil refinery units and process of preparing same
CA3260893A1 (en) 2022-12-12 2024-06-20 Chevron U.S.A. Inc. PROCESS FOR STABLE MIXING OF PLASTIC WASTE WITH A OIL FILL FOR FEEDING OIL REFINERY UNITS AND ITS PREPARATION PROCESS
US12692448B2 (en) 2023-01-27 2026-07-28 Brightmark Plastics Renewal Technologies Llc Hydrotreatment of pyrolyzed oil derived from plastic waste stock
US12453993B2 (en) 2023-03-31 2025-10-28 Nexus Circular LLC Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof
US12435278B2 (en) 2023-03-31 2025-10-07 Nexus Circular LLC Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof
US12453994B2 (en) 2023-03-31 2025-10-28 Nexus Circular LLC Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof
US12473506B2 (en) 2023-03-31 2025-11-18 Nexus Circular LLC Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof
US12595424B2 (en) 2023-03-31 2026-04-07 Nexus Circular LLC Hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics and methods of making and use thereof
WO2025033362A1 (ja) * 2023-08-04 2025-02-13 株式会社ブリヂストン 架橋ゴムの分解方法
JPWO2025033361A1 (pl) * 2023-08-04 2025-02-13
WO2025033297A1 (ja) * 2023-08-04 2025-02-13 株式会社ブリヂストン 架橋ゴムの分解方法
JPWO2025033264A1 (pl) * 2023-08-04 2025-02-13
DE102023209754A1 (de) * 2023-10-05 2025-04-10 Volkswagen Aktiengesellschaft Verfahren und Anlage zum Recycling von Baugruppen oder Stoffgemischen aus Kunststoff und Biowerkstoffen
US20250215182A1 (en) 2023-12-28 2025-07-03 Chevron U.S.A. Inc. Circular economy for waste polystyrene via refinery fcc unit
WO2025144802A1 (en) 2023-12-28 2025-07-03 Chevron U.S.A. Inc. Process for stable blend of polystyrene plastic with hydrocarbon feed for feeding to oil refinery units and process of preparing same
WO2025144805A1 (en) 2023-12-28 2025-07-03 Chevron U.S.A. Inc. Use of blend of polystyrene with hydrocarbon feedstock for gasoline and chemicals preparation
US20250243410A1 (en) 2024-01-29 2025-07-31 Nexus Circular LLC Systems and methods for making hydrocarbon compositions derived from pyrolysis of post-consumer and/or post-industrial plastics
WO2026036174A1 (en) * 2024-08-13 2026-02-19 Circular Seed Rand Pty Ltd A system and method for processing waste material
WO2026125671A1 (en) * 2024-12-13 2026-06-18 OMV Downstream GmbH Process for recycling plastics material

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE597086C (de) * 1932-08-24 1934-05-16 I G Farbenindustrie Akt Ges Verfahren zur Herstellung von hochmolekularen Hydrierungsprodukten von natuerlichem oder synthetischem Kautschuk, Cyclokautschuk, Polymerisationsprodukten von Olefinen, natuerlichen oder kuenstlichen Harzen oder aehnlichen hochpolymeren Stoffen von fester bzw. hochviskoser bis schmieroelartiger Beschaffenheit
DE2530229A1 (de) * 1975-07-07 1977-01-27 Helmut Dr Ing Wuerfel Verfahren zur umwandlung von altreifen, gummi und/oder anderen kunststoffen
GB1544099A (en) * 1975-08-11 1979-04-11 Occidental Petroleum Corp Flash pyrolysis of organic solid waste
US4384150A (en) * 1981-08-20 1983-05-17 Lyakhevich Genrikh D Method of making either a softener for rubber mixtures or a furnace fuel oil
FR2512032B1 (fr) * 1981-09-01 1983-12-16 Bruss Ti Kirova Procede d'obtention d'un ramollissant pour melanges caoutchoucs et de mazout
DE3442506C2 (de) * 1984-11-22 1987-04-16 Union Rheinische Braunkohlen Kraftstoff AG, 5000 Köln Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
DE3602041C2 (de) * 1986-01-24 1996-02-29 Rwe Entsorgung Ag Verbessertes Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
JPS63178195A (ja) * 1987-01-20 1988-07-22 工業技術院長 ポリオレフイン系プラスチツクから低沸点炭化水素油を製造する方法
DE3743752A1 (de) * 1987-12-23 1989-07-13 Asea Brown Boveri Verfahren zum aufarbeiten von abfallmaterial
US5079385A (en) * 1989-08-17 1992-01-07 Mobil Oil Corp. Conversion of plastics
US5070109A (en) * 1989-12-20 1991-12-03 Rubber Waste, Inc. Recovery of hydrocrabon products from elastomers
DE4107046A1 (de) * 1991-03-06 1992-09-10 Menges Georg Verfahren und vorrichtung zum verwerten von organischen abfaellen
DE4129885A1 (de) * 1990-12-06 1993-03-11 Georg Menges Verfahren zur herstellung und verarbeitung von pulvern und granalien aus polymerabfaellen
EP0502618B1 (en) * 1991-03-05 1996-08-14 BP Chemicals Limited Polymer cracking
US5158983A (en) * 1991-10-04 1992-10-27 Iit Research Institute Conversion of automotive tire scrap to useful oils

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005010151B3 (de) * 2005-03-02 2006-09-14 Clyvia Technology Gmbh Verfahren zum katalytischen Depolymerisieren von kohlenwasserstoffhaltigen Rückständen sowie Vorrichtung zum Durchführen dieses Verfahrens
DE102008021629B4 (de) * 2008-04-25 2017-09-14 Technische Werke Ludwigshafen Ag Vorrichtung zur Herstellung von Roh-, Brenn- und Kraftstoffen aus organischen Substanzen

Also Published As

Publication number Publication date
SK280953B6 (sk) 2000-10-09
FI954685A7 (fi) 1995-10-02
CN1049237C (zh) 2000-02-09
KR960701970A (ko) 1996-03-28
NZ265043A (en) 1997-06-24
UA48954C2 (uk) 2002-09-16
DE4435238A1 (de) 1996-04-11
EP0692009A1 (de) 1996-01-17
CN1120347A (zh) 1996-04-10
PL310893A1 (en) 1996-01-08
JPH08508520A (ja) 1996-09-10
NO953758L (no) 1995-09-22
JP2003129066A (ja) 2003-05-08
SK121695A3 (en) 1996-05-08
DE4311034A1 (de) 1994-10-06
WO1994022979A1 (de) 1994-10-13
ES2104375T3 (es) 1997-10-01
CZ254695A3 (en) 1996-03-13
FI954685A0 (fi) 1995-10-02
ATE153692T1 (de) 1997-06-15
DE59402926D1 (de) 1997-07-03
PL178639B1 (pl) 2000-05-31
US5849964A (en) 1998-12-15
CA2158032A1 (en) 1994-10-13
DK0692009T3 (da) 1997-07-14
KR970706371A (ko) 1997-11-03
FI954685L (fi) 1995-10-02
CZ292837B6 (cs) 2003-12-17
GR3024422T3 (en) 1997-11-28
JP3385025B2 (ja) 2003-03-10
UA39203C2 (uk) 2001-06-15
NO953758D0 (no) 1995-09-22
HU218853B (hu) 2001-02-28
BG62572B1 (bg) 2000-02-29
AU6536194A (en) 1994-10-24
RU2127296C1 (ru) 1999-03-10
BG100108A (bg) 1996-07-31
KR100293752B1 (ko) 2001-10-24
HU9502874D0 (en) 1995-11-28
AU681652B2 (en) 1997-09-04
KR100390236B1 (ko) 2003-10-04

Similar Documents

Publication Publication Date Title
WO1994022979A1 (de) Verfahren zur verarbeitung von alt- oder abfallkunststoffen
EP0710270B1 (de) Verfahren zum recyclen von kunststoffabfällen in einem steamcracker
EP0713906B1 (de) Verfahren zum Recyclen von Kunststoffen in einem Steamcracker
DE112020000884B4 (de) Ein Verfahren zur maximalen Produktion von Ethylen oder Propylen
EP0182309B1 (de) Verfahren zur hydrierenden Aufarbeitung von Kohlenstoff enthaltenden Abfällen synthetischen bzw. überwiegend synthetischen Ursprungs
EP0132612B1 (de) Verfahren zur Herstellung flüssiger Kohlenwasserstoffe
EP0759962B1 (de) Vorrichtung zur depolymerisation von alt- und abfallkunststoffen
DE69422027T2 (de) Verfahren zur wiederverwertung von altkunststoff
DE69205164T2 (de) Durch Vakuumpyrolyse Rückgewinnung von Kraftfahrzeugzerkleinererrückstand.
US20240218257A1 (en) Systems and methods for processing mixed plastic waste
EP0784661B1 (de) Verfahren zur gewinnung von chemierohstoffen und kraftstoffkomponenten aus alt- oder abfallkunststoffen
DE4344311A1 (de) Verfahren und Vorrichtung zur thermischen Depolymerisation von Kunststoffen
DE19512029A1 (de) Verfahren zur Herstellung von Paraffinen, Wachsen und Basisölen
EP0123161B1 (de) Verfahren zur Hydrierung von Kohle
DE4417721A1 (de) Vorrichtung zur Depolymerisation von Alt- und Abfallkunststoffen
EP0291698B1 (de) Verbessertes Verfahren zur hydrierenden Spaltung Kohlenstoff enthaltender synthetischer Abfälle
EP0726306B1 (de) Verfahren zur gemeinsamen Hydrierung von kohlenwasserstoffhaltigen Gasen und Kondensaten
US4146459A (en) Treatment of coal liquefaction effluent
DE3715158C1 (de) Verfahren zur Gewinnung von Schweloel
DE4417386A1 (de) Verfahren zur Herstellung destillierbarer Kohlenwasserstoffe
DD214749A3 (de) Verfahren zur hydrierenden spaltung von altgummi und gummiabfaellen
DD254207A1 (de) Verfahren zur hydrobehandlung von kohlenstoffhaltigem material
DD285988A5 (de) Verfahren zur verarbeitung von wirbelschichtteer

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: 19950918

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: 19960701

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

REF Corresponds to:

Ref document number: 153692

Country of ref document: AT

Date of ref document: 19970615

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: TROESCH SCHEIDEGGER WERNER AG

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19970528

REF Corresponds to:

Ref document number: 59402926

Country of ref document: DE

Date of ref document: 19970703

ET Fr: translation filed
REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 19970528

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2104375

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: GR

Ref legal event code: FG4A

Free format text: 3024422

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

Ref country code: PT

Payment date: 20000120

Year of fee payment: 7

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

Ref country code: GR

Payment date: 20000210

Year of fee payment: 7

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

Ref country code: DK

Payment date: 20000303

Year of fee payment: 7

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

Ref country code: MC

Payment date: 20000308

Year of fee payment: 7

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

Ref country code: IE

Payment date: 20000310

Year of fee payment: 7

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

Ref country code: CH

Payment date: 20000530

Year of fee payment: 7

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

Ref country code: DK

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

Effective date: 20010325

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

Ref country code: IE

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

Effective date: 20010326

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: 20010331

Ref country code: LI

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

Effective date: 20010331

Ref country code: GR

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

Effective date: 20010331

Ref country code: CH

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

Effective date: 20010331

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

Ref country code: PT

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

Effective date: 20010930

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

REG Reference to a national code

Ref country code: PT

Ref legal event code: MM4A

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

Effective date: 20010930

NLS Nl: assignments of ep-patents

Owner name: DER GRUENE PUNKT-DUALES SYSTEM DEUTSCHLAND A.G.;RO

BECA Be: change of holder's address

Owner name: *DUALES SYSTEM DEUTDCHLAND A.G.FRANKFURTER STRASSE

Effective date: 20030225

BECH Be: change of holder

Owner name: *DUALES SYSTEM DEUTDCHLAND A.G.

Effective date: 20030225

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

Ref country code: NL

Payment date: 20030317

Year of fee payment: 10

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

Ref country code: FR

Payment date: 20030318

Year of fee payment: 10

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

Ref country code: AT

Payment date: 20030321

Year of fee payment: 10

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

Ref country code: SE

Payment date: 20030324

Year of fee payment: 10

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

Ref country code: LU

Payment date: 20030325

Year of fee payment: 10

Ref country code: ES

Payment date: 20030325

Year of fee payment: 10

Ref country code: DE

Payment date: 20030325

Year of fee payment: 10

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

Ref country code: BE

Payment date: 20030326

Year of fee payment: 10

REG Reference to a national code

Ref country code: GB

Ref legal event code: 732E

REG Reference to a national code

Ref country code: ES

Ref legal event code: PC2A

REG Reference to a national code

Ref country code: GB

Ref legal event code: 732E

REG Reference to a national code

Ref country code: FR

Ref legal event code: TP

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: 20040325

Ref country code: AT

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

Effective date: 20040325

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

Ref country code: SE

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

Effective date: 20040326

Ref country code: ES

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

Effective date: 20040326

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

Ref country code: BE

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

Effective date: 20040331

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

Ref country code: GB

Payment date: 20040913

Year of fee payment: 11

BERE Be: lapsed

Owner name: *DUALES SYSTEM DEUTDCHLAND A.G.

Effective date: 20040331

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 NON-PAYMENT OF DUE FEES

Effective date: 20041001

Ref country code: DE

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

Effective date: 20041001

EUG Se: european patent has lapsed
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

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

Effective date: 20041130

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20041001

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

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

Ref country code: IT

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

Effective date: 20050325

Ref country code: GB

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

Effective date: 20050325

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20040326

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

Effective date: 20050325