EP0713906B1 - Procédé de recyclage de matériaux plastiques dans une unité de vapocraquage - Google Patents

Procédé de recyclage de matériaux plastiques dans une unité de vapocraquage Download PDF

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Publication number
EP0713906B1
EP0713906B1 EP95118124A EP95118124A EP0713906B1 EP 0713906 B1 EP0713906 B1 EP 0713906B1 EP 95118124 A EP95118124 A EP 95118124A EP 95118124 A EP95118124 A EP 95118124A EP 0713906 B1 EP0713906 B1 EP 0713906B1
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Prior art keywords
column
products
steam cracker
fraction
reactor
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EP95118124A
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German (de)
English (en)
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EP0713906A1 (fr
Inventor
Uwe Dr. Stabel
Helmut Dr. Wörz
Rüdiger Dr. Kotkamp
Andreas Dr. Fried
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Der Gruene Punkt Duales System Deutschland AG
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BASF SE
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    • 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
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours

Definitions

  • the invention relates to a method for recycling plastics in a steam cracker.
  • plastics for example pure polymer plastic waste, mixed plastic waste or film waste, including any Soiling, adhesive materials, fillers, residues of content etc., in high-quality ingredients for the well-known steam cracker process being transformed.
  • feedstocks will be again in the known steam cracker process into fission products such as Converted ethylene, propylene, C4 mixtures, pyrolysis gasoline etc., the same in almost the same or even higher yield as if the steam cracker with the traditional Input materials such as naphtha, liquid petroleum gas (LPG) and gas oil is driven.
  • LPG liquid petroleum gas
  • the method according to the invention therefore becomes essential economic contribution to the recycling of plastics accomplished.
  • plastic waste in the garbage 70% by weight of polyolefins such as polyethylene and polypropylene, approx. 15% by weight from styrene polymers, approx. 10 wt .-% of PVC and in small minor amounts of approx. 5% by weight from other plastics such as polyurethane, polyester and polyamide.
  • polyolefins such as polyethylene and polypropylene
  • styrene polymers such as polyethylene and polypropylene
  • PVC polyurethane
  • plastics such as polyurethane, polyester and polyamide
  • the bottle or hollow body fraction may be mentioned, consisting of bottles, containers etc., which in the essentially from polyolefins such as polyethylene or polypropylene consist of a mixed plastic fraction, consisting essentially of made of polyolefins such as polyethylene (PE), polypropylene (PP), styrene5 polymer such as polystyrene (PS) and polyvinyl chloride (PVC); a Foil fraction consisting essentially of PE and PP etc. and a light fraction consisting essentially of PE, PP and PS, each with adhering soiling, adhesive materials, Fillers, leftover content etc.
  • the fractions are different from the plastics mentioned only in minor quantities, for example less than 10% by weight, in many cases less than 5% by weight, and in particular contain less than 2% by weight.
  • WO 93/18112 describes a process for the production of olefins Plastic waste by setting a desired viscosity through thermal pretreatment of plastic waste in one Temperature range from 380 to 680 ° C and subsequent thermal Treatment of the product at a temperature of 700 to 1100 ° C described.
  • the process does not concern separation by distillation of the product.
  • the process cannot be residue-free produce vaporizable product.
  • a method is described in PCT application WO-A-9 503 375 (EP 94/01647), in which one receives a melt obtained from plastic waste 400 to 550 ° C converted into products, one from the products Separates the distillate fraction and feeds it to a steam cracker. Inert conditions when melting the plastic waste not described.
  • the task was to provide a method that Can be used on an industrial scale, with which plastic waste into high-quality Feedstocks for an existing one Steam crackers are converted to use these feedstocks without adding, for example, naphtha, LPG and gas oil in the Steam cracking process Fission products such as ethylene, propylene, 04 mixtures and pyrolysis gasoline can be obtained in high yield can.
  • the melt obtained at 370 to 550 ° C preferably converts 380 to 530 ° C into products from which Products a distillate fraction at 150 to 280 ° C, often at 200 to 280 ° C preferably at 220 to 260 ° C and especially at 230 up to 250 ° C and a steam cracker feeds.
  • the melting and usually also the following steps of the process according to the invention are carried out under inert conditions, ie while avoiding oxygen.
  • a particular advantage of the process is that the formation of ultra poison such as halogenated dibenzodioxins and dibenzofurans (dioxin) is significantly reduced.
  • the plastic wastes are interted before being fed into the melting device by exchanging the air for an inert gas such as nitrogen, argon, CO 2 or a hydrocarbon gas such as methane or a cracked gas, preferably nitrogen.
  • Fume 5 is well suited as cracked gas after removal of the HCl and D in FIG. 2. Since no oxygen is introduced in the further process, the inert conditions are present throughout the process.
  • the process is advantageous for hollow body fractions and Foil fractions used.
  • the melting of the plastic waste is preferably done at 280 to 350 ° C, in some Cases at 300 to 350 ° C, especially 290 to 320 ° C and the conversion in the reactor preferably at 400 to 450 ° C.
  • the plastic waste i.e. usually more than 5% by weight of chlorine-containing plastic such as Polyvinyl chloride and / or aromatic-containing plastic such as styrene polymer, such as in a mixed plastic fraction
  • chlorine-containing plastic such as Polyvinyl chloride and / or aromatic-containing plastic such as styrene polymer
  • the plastic waste at 280 to 380, preferably 330 to 380, in particular 320 up to 350 ° C, melt, while the polyvinyl chloride is dehydrohalogenated, and the conversion in the reactor at 390 to 530, preferably 400 to 480 ° C, in particular 410 to 460 ° C in Products.
  • Dehydrohalogenation is sufficient at the temperatures used generally a residence time of 1 hour to 20 hours.
  • the time required depends on the desired degree of dehydrohalogenation and can easily be done by the expert by simple preliminary tests determine. In some cases, especially when the dehydrohalogenation after melting, for example at 250 to 300 ° C, is continued, the desired residence time be about 5 days. This can advantageously during a Temporary storage happen.
  • the heat of condensation of the top product from the first column can be used to generate water vapor of various pressures become.
  • Inertization usually takes place before insertion of plastic waste in the melting apparatus. This can by an inert gas shower or by suitable inert gas inlet into the conveyor and / or the upstream storage or storage containers in a manner known per se. If pneumatic conveying is used, the inert gas can be used as a subsidy on. Sometimes it is also an advantage to add inert gas into the melting apparatus above or below the liquid level initiate.
  • the plastic waste can be melted in suitable equipment take place, the adequate heat transfer and the Ensure the required mixing. It has proven itself Stirred tanks such as stirred tanks or in particular intensive stirred tanks, which can be equipped with a heating jacket and / or internal heating. Usually the melting process is relatively quick, i.e. after 0.5 to 30 minutes.
  • stirred tanks e.g. two or three, operated in cascade.
  • a tube furnace is advantageous. In many cases it has proved to be favorable, a part of those leaving the tube furnace Reaction products to increase the residence time Feed tube furnace again. With this driving style, the Conversion reaction to the products depending on the temperature and Dwell times in part in the return line used for this, optionally in a dwell, instead.
  • the tube furnace is generally a heat exchanger, in the heat from the gas phase outside the tubes in the material in the tubes, for example the Melt is transferred. You can use a reformer furnace Coke oven, refinery oven or in particular a tubular cracking oven use, as used for example in the steam cracker (see e.g. Ullmann's Encyclopedia of Chemical Engineering, 4th edition, volume 3, p. 476 and p. 330/331).
  • Residues and solids in the sense of this invention are such Substances that remain in the separation by distillation and, if at all, do not boil below 500 ° C. It is for example impurities adhering to the plastic waste, Paper residues, coking products, glass and metal residues, Sand, pigment residues, fillers or the like.
  • the bottom product of the first column at least partially as a heating medium through the heating jacket of the reflow tank lead before it is fed back to the reactor.
  • the middle Residence time in the reactor is usually from 0.05 to 10 hours.
  • the process according to the invention is generally carried out in a Pressure of 0.8 to 2.0 bar, preferably at atmospheric pressure, that is 1 bar.
  • the specified boiling points or boiling ranges refer to 1 bar.
  • plastic waste can be used undried or dry become.
  • plastic waste may be required by generally known methods such as shredding or grinding shred. With average particle sizes of 2 to 10 mm achieved good results. Particle sizes from 1 to 10 cm, in some Cases of uncrushed plastic waste are also suitable.
  • a conveyor element 1 - for example a screw conveyor, Carrier chain conveyors or pneumatic conveyors - become dry and crushed plastic waste 2, for example a hollow body fraction, from a storage container 3 one with a heating jacket or heating bundle equipped stirring tank 4 supplied.
  • the storage container 3 is initiated by, for example Nitrogen inertized from below (14). Residual oxygen leaves at 15 the system where excess nitrogen is also released. It makes sense to use a measuring probe known per se to check the Provide oxygen concentration below the inert gas inlet 14.
  • the plastic waste approx. 300 ° C converted into an easily pumpable melt.
  • dehydrohalogenation may occur if by Sorting errors of the plastic waste contain a slip of PVC is.
  • any HCl 5 that arises is removed using known water Process - not relevant to the invention - converted into aqueous HCL, this can be fed to other production processes or be neutralized with NaOH.
  • the above melt is by means of a Pump - forced circulation - a tube cracking furnace 6 (hereinafter Called cracking furnace) supplied.
  • Called cracking furnace the Polymers without the addition of hydrogen, steam, catalysts, Solvents or diluents converted into products that Steam crackers can be vaporized and split in a conventional manner can.
  • a thermal liquid splitting takes place at approx. 420 ° C, furthermore, the residual dehydrohalogenation may take place in the cracking furnace instead of.
  • the necessary heat is external, for example by oil or gas heating. That the cracking furnace leaving liquid-vapor mixture goes directly to a column 7, for example a feed column.
  • As Bottom product is the higher boiling at about 350 ° C, not in deducted short chain hydrocarbon converted products.
  • the one entering the packed column Liquid / gas mixture is mixed with water or aqueous NaOH 11 washed out in countercurrent; HCl possibly still contained in the gas is used as aqueous HCl or aqueous NaCl solution with the liquid mixture discharged at the swamp.
  • the one emerging at the swamp Liquid mixture organic liquid / aqueous HCl or aqueous NaCl solution is in a downstream phase separation vessel 12 separated.
  • the specifically lighter, organic phase is on the one hand as feed material A for the steam cracker from the process discharged and, on the other hand, fed as reflux to the column.
  • the specifically heavier, aqueous phase, possibly enriched with HCl or NaCl 13 is removed from the process.
  • the HCl-free gas mixture emerging at the top of the packed column is also added to the steam cracker as feed B.
  • FIG. 2 Comminuted, dry plastic waste 2, for example a mixed plastic fraction, is fed from a storage container 3 to a stirred container 4 equipped with a heating jacket or heating bundle via a conveying element 1 - for example a screw conveyor, carrying chain conveyor or pneumatic conveying.
  • the storage container 3 is rendered inert from below by introducing nitrogen, for example (14). Residual oxygen leaves the system at 15, where excess nitrogen is also released. It makes sense to provide a measuring probe known per se for checking the oxygen concentration below the inert gas inlet 14.
  • the plastic waste is converted into an easily pumpable melt at about 350 ° C.
  • Dehydrohalogenation occurs up to 98-99%, based on the chlorine content in PVC.
  • the resulting HCl 5 is converted into aqueous HCl using known methods - not relevant to the invention - this can be fed to other production processes or neutralized with NaOH.
  • the above melt is fed to a cracking furnace 6 by means of a pump - forced circulation.
  • the polymers are converted without the addition of hydrogen, steam, catalysts, solvents or diluents into products which can be vaporized and split in a conventional manner in the steam cracker.
  • Thermal liquid splitting takes place at approx. 450 ° C, furthermore the residual dehydrohalogenation takes place in the cracking furnace.
  • the necessary heat is supplied externally, for example by oil or gas heating.
  • the liquid-vapor mixture leaving the cracking furnace is fed directly to a column 7, for example a strengthening column.
  • the higher-boiling products which are not converted into short-chain hydrocarbons are withdrawn as the bottom product at about 380 ° C.
  • these are returned directly to the cracking furnace and, on the other hand, they are passed as heat carriers through the melt in the stirred tank and through the heating jacket of the stirred tank and ultimately returned to the cracking furnace.
  • residues and solids 8 are discharged from the bottom product, for example by means of a hydrocyclone 9.
  • the steam mixture emerging at the top of the column at approximately 240 ° C. is, after a partial condensation of another column 10, for example a packed column, at approx 110 ° C supplied.
  • the liquid / gas mixture entering the packed column is washed out with water or aqueous NaOH 11 in countercurrent; the HCl contained in the gas is discharged as aqueous HCl or aqueous NaCl solution with the liquid mixture at the bottom.
  • the liquid mixture emerging at the bottom organic liquid / aqueous HCl or aqueous NaCl solution is separated in a subsequent phase separation vessel 12.
  • the specifically lighter, organic phase - see Table 11 - is fed on the one hand to a distillation or extraction unit 20 suitable for the separation of aromatics and on the other hand fed to the column as reflux.
  • the specifically heavier, aqueous phase, enriched with HCl or NaCl 13 is removed from the process.
  • the HCl-free gas mixture emerging at the top of the packed column is fed to the steam cracker as starting material D.
  • the above organic distillation or extraction unit is separated into feed C for the steam cracker and into an aromatic fraction X in a column 20; both fractions are removed from the process.
  • the feed materials obtained can be conventionally used in steam crackers Be vaporized and split.
  • the method according to the invention has i.a. the advantage that at Operating the steam cracker with that from the plastic waste obtained product of value heating energy versus naphtha as feed can be saved. It comes without adding hydrogen, Diluents or solvents and works practically depressurized. Furthermore, the method has the advantage that Steam crackers with residue-free vaporizable feedstocks supply.
  • - Distillation or extraction unit 20 Process the aromatics obtained. It is generally a mixture of styrene, ethylbenzene, toluene and Benzene as the main ingredients.
  • styrene ethylbenzene
  • Benzene Benzene
  • the fission products thus obtainable from the steam cracker process have the compositions given in the table; Tables 3 and 4.
  • Tables 3 and 4 For comparison, the compositions of the cleavage products are given in both of the latter two tables, if the steam cracker is operated with the classic feed naphtha.
  • the comparison shows that the yield of ethylene and propylene, if the steam cracker is operated with the feed materials - obtained from the hollow fraction - is higher than if the steam cracker is operated with naphtha.
  • Residues (organic, high-boiling hydrocarbons and coke) 3% by weight
  • Solids (residue on ignition) 7% by weight 100% by weight
  • Aromatic fraction, mainly benzene, toluene, ethylbenzene and styrene 28% by weight
  • Residues (organic, high-boiling hydrocarbons and coke) 12% by weight

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Processing Of Solid Wastes (AREA)

Claims (10)

  1. Procédé de recyclage de déchets de matières synthétiques dans une unité de vapocraquage, caractérisé en ce qu'on fait fondre dans des conditions inertes des déchets de matières synthétiques, on transforme la masse fondue obtenue en produits à 370 jusqu'à 550°C, on isole des produits une fraction de distillat à 150 jusqu'à 280°C et on amène celle-ci à une unité de vapocraquage comme matière de chargement.
  2. Procédé suivant la revendication 1, caractérisé par les particularités suivantes :
    une fusion des déchets de matières synthétiques,
    une alimentation de la masse fondue dans un réacteur, les polymères étant transformés en produits à 370 jusqu'à 550°C,
    un isolement par distillation d'une fraction de distillat à partir des produits, à 150 jusqu'à 280°C,
    un recyclage des autres produits dans le réacteur à l'exception de résidus et de matières solides et éventuellement d'acides inorganiques, et
    une introduction de la fraction de distillat isolée, éventuellement après une séparation ultérieure, comme matière de chargement dans l'unité de vapocraquage.
  3. Procédé suivant l'une des revendications 1 et 2, caractérisé en ce qu'on effectue l'isolement par distillation de la fraction de distillat à partir des produits avec les étapes suivantes :
    une séparation des produits au moyen d'une première colonne montée directement en aval du réacteur,
    en un produit de bas de colonne qui est obtenu à 350 jusqu'à 470°C et qui est recyclé dans le réacteur après évacuation des résidus et des matières solides, et
    en un produit de tête qui est obtenu à 150 jusqu'à 280°C et qui est amené, après une condensation partielle, à une deuxième colonne à 70 jusqu'à 150°C,
    une séparation du mélange liquide/gaz formé après la condensation partielle au moyen de la deuxième colonne précitée,
    en un mélange liquide sortant du bas de la deuxième colonne, qui, d'une part, est utilisé comme reflux pour la première colonne et, d'autre part, est utilisé comme matière de chargement pour l'unité de vapocraquage, et
    en un mélange gazeux qui sort à la tête de la deuxième colonne et qui est utilisé comme matière de chargement pour l'unité de vapocraquage.
  4. Procédé de recyclage de déchets de matières synthétiques contenant du chlore et/ou des produits aromatiques dans une unité de vapocraque suivant l'une des revendications 1 et 2, caractérisé par les particularités suivantes :
    une fusion des déchets de matières synthétiques à 280 jusqu'à 380°C avec déshydrohalogénation de la matière synthétique contenant du chlore,
    une amenée de la masse fondue dans un réacteur, les polymères étant transformés en produits à 390 jusqu'à 530°C,
    une séparation desdits produits au moyen d'une première colonne montée directement en aval du réacteur,
    en un produit de bas de colonne qui est obtenu à 330 jusqu'à 450°C et qui est recyclé dans le réacteur après évacuation des résidus et des matières solides, et
    en un produit de tête qui est obtenu à 150 jusqu'à 280°C et qui, après une condensation partielle, est amené à une deuxième colonne à 70 jusqu'à 150°C,
    une séparation du mélange liquide/gaz obtenu après la condensation partielle au moyen de ladite deuxième colonne,
    en un mélange liquide sortant du fond de la deuxième colonne, qui, d'une part, est utilisé comme reflux pour la première colonne et, d'autre part, est amené à une unité de distillation ou d'extraction appropriée pour l'isolement de produits aromatiques, et
    en un mélange gazeux qui sort à la tête de la deuxième colonne et qui est utilisé comme matière de chargement pour l'unité de vapocraquage.
  5. Procédé suivant la revendication 4, caractérisé en ce qu'on sépare le mélange liquide amené à l'unité de distillation ou d'extraction
    en une fraction liquide, qui est utilisée comme matière de chargement pour l'unité de vapocraquage, et
    en une fraction de produits aromatiques.
  6. Procédé suivant l'une des revendications 1 à 5, caractérisé en ce que, comme déchets de matières synthétiques, on met en oeuvre une fraction de corps creux, constituée de bouteilles et de récipients essentiellement en polyoléfines avec éventuellement des impuretés adhérentes, des matières collantes, des charges et/ou des résidus de contenu.
  7. Procédé suivant l'une des revendications 1 à 5, caractérisé en ce que, comme déchets de matières synthétiques, on met en oeuvre une fraction de matières plastiques mélangées qui est constituée sensiblement de polyoléfines, de polymère du styrène et de polychlorure de vinyle avec éventuellement des impuretés adhérentes, des matières collantes, des charges et/ou des résidus de contenu.
  8. Procédé suivant l'une des revendications 1 à 5, caractérisé en ce que, comme déchets de matières synthétiques, on met en oeuvre une fraction de feuilles, constituée essentiellement de polyéthylène, de polypropylène, y compris des encrassements éventuels, des matières collantes, des charges, des résidus de contenu.
  9. Procédé suivant l'une des revendications 1 à 5, caractérisé en ce que, comme déchets de matières synthétiques, on met en oeuvre une fraction légère, constituée essentiellement de polyéthylène, de polypropylène, de polystyrène, y compris des encrassements éventuels, des matières collantes, des charges, des résidus de contenu.
  10. Procédé suivant l'une des revendications 1 à 9, caractérisé en ce qu'aux matières synthétiques spécifiées on peut encore ajouter de faibles quantités de déchets contenus dans les ordures, comme des polyuréthannes, des polyesters, des polyamides.
EP95118124A 1994-11-24 1995-11-17 Procédé de recyclage de matériaux plastiques dans une unité de vapocraquage Expired - Lifetime EP0713906B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4441699 1994-11-24
DE4441699A DE4441699A1 (de) 1994-11-24 1994-11-24 Verfahren zum Recyclen von Kunststoffen in einem Steamcracker

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EP0713906A1 EP0713906A1 (fr) 1996-05-29
EP0713906B1 true EP0713906B1 (fr) 1999-05-26

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US11479726B2 (en) 2020-09-28 2022-10-25 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
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks

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AT518356B1 (de) * 2016-03-07 2018-03-15 Ing Walter Kanzler Dipl Verfahren zur Depolymerisation von Polymeren
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WO2022056212A1 (fr) 2020-09-14 2022-03-17 Ecolab Usa Inc. Additifs d'écoulement à froid pour charge de départ synthétique dérivée de matière plastique
WO2023049025A1 (fr) * 2021-09-21 2023-03-30 Eastman Chemical Company Intégration de chaleur avec de l'huile de pyrolyse et un milieu de transfert de chaleur pour installations chimiques
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CN118159628A (zh) 2021-10-27 2024-06-07 巴斯夫欧洲公司 用于纯化热解产物的方法以及经纯化的热解油的用途
US11542438B1 (en) * 2022-01-14 2023-01-03 Saudi Arabian Oil Company Hydrothermal conversion of plastic to oil
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DE4207976C2 (de) * 1992-03-13 2001-03-15 Rwe Umwelt Ag Verfahren zur Herstellung Olefinen durch thermische Behandlung von Kunststoffabfällen
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US10927315B2 (en) 2016-10-11 2021-02-23 Sabic Global Technologies B.V. Maximizing high-value chemicals from mixed plastic using different steam-cracker configurations
US11479726B2 (en) 2020-09-28 2022-10-25 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
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
US11746297B2 (en) 2020-09-28 2023-09-05 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
US11781073B2 (en) 2020-09-28 2023-10-10 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
US12077713B2 (en) 2020-09-28 2024-09-03 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
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks

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DE59506023D1 (de) 1999-07-01
EP0713906A1 (fr) 1996-05-29
DE4441699A1 (de) 1996-05-30
ES2134396T3 (es) 1999-10-01

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