EP0823935A1 - Procede de traitement de matieres plastiques usagees ees ou de dechets de matieres plastiques - Google Patents

Procede de traitement de matieres plastiques usagees ees ou de dechets de matieres plastiques

Info

Publication number
EP0823935A1
EP0823935A1 EP96914161A EP96914161A EP0823935A1 EP 0823935 A1 EP0823935 A1 EP 0823935A1 EP 96914161 A EP96914161 A EP 96914161A EP 96914161 A EP96914161 A EP 96914161A EP 0823935 A1 EP0823935 A1 EP 0823935A1
Authority
EP
European Patent Office
Prior art keywords
condensate
depolymerization
phase
indicates
temperature
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.)
Withdrawn
Application number
EP96914161A
Other languages
German (de)
English (en)
Inventor
Horst Hastrich
Christian Hecka
Rolf Holighaus
Klaus Niemann
Claus Strecker
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.)
Veba Oel 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 EP0823935A1 publication Critical patent/EP0823935A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—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

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 by depolymerizing the starting materials at elevated temperature to a pumpable and a volatile phase and separating the volatile phase into a gas phase and a condensate.
  • the condensable depolymerization products can be subjected to hydrogenating refining on a fixed bed catalyst or else on a moving catalyst or in a flowing catalyst bed.
  • Such hydrogenating refinements represent refining processes which are also referred to in the specialist literature as hydrotreating.
  • the condensates to be subjected to hydrotreating contain non-evaporating constituents originating from the depolymerizer by foaming, spraying or steam inclusions and also re-formed by repolymerization, so that direct loading of a catalyst bed fixedly arranged in a hydrotreater would lead to a rapid inactivation of the same, or very much high catalyst consumption would result.
  • deposits would form on heat exchangers, for example preheaters, which would prevent sufficiently long operating times without interruptions.
  • Document WO 94/22979 teaches that the condensate e.g. B.
  • Another object is to avoid rapid inactivation of the hydrotreating stage catalyst feed.
  • the invention in the method mentioned at the outset is that the depolymerizate remaining after the volatile phase has been separated off is heated together with the condensate or condensate portions in the presence of hydrogen and is subjected to hydrotreating after the removal of non-boiling constituents to obtain a syncrude.
  • the condensate or the high-boiling fraction of the condensate is heated together with the depolymerizate and hydrogen under pressure to above the starting temperature of the hydrotreating catalyst.
  • the process can be carried out in such a way that there is sufficient residence time in the heating section at elevated temperature to achieve a further cleavage and lowering of the viscosity of the depolymerate.
  • the method can also be designed in such a way that a dwell is connected downstream of the preheating section. As a result, the depolymerization is driven so far that losses due to removal of residue can be kept low.
  • the hydrotreating is expediently operated at the temperature specified by the preheater.
  • the presence of hydrogen under pressure and the dilution of the condensate with depolymerize prevent the preheater's heat exchanger tubes from clogging.
  • the Hydrotreater is largely protected from exposure to non-boiling material by installing a highly effective steam / liquid separator. This achieves downtimes that meet commercial requirements.
  • the non-boiling components are removed at the bottom of the steam / liquid separator, also called hot separator, in a flowable consistency. pulled. They can be expanded in several stages and separated, for example in a vacuum column, from the remaining distillable constituents which can be combined with the condensate from the depolymerization.
  • a partial stream of the residue can be branched off from the course of the vacuum distillation and fed to the depolymerizate before it is charged with hydrogen.
  • the process can be designed for very small amounts of residues without the risk of drying the preheating or a downstream retention tank.
  • the recycling rate of vacuum distillation residue based on the amount of depolymerized material is dependent on the quality of the material used, ie. H. depending on its tendency towards depolymerization, under the given conditions 0 to 500%.
  • the recycle rate is 150 to 250%, e.g. B. for typical fractions of old or waste plastics from household collections of the dual system Germany-DSD.
  • the depolymerization is carried out at a pressure of 0.1 to 100 bar, in particular 0.2 to 5 bar, a temperature of 250 to 450 ° C, in particular 370 ° C to 420 ° C and a residence time of 0.1 to 10 h, preferably 0 , 5 to 5 hours.
  • the hydrogen partial pressure in the hydrogenation stage is set to 50 to 200 bar, preferably 100 to 200 bar.
  • the temperature of the depolymerizate and condensate on leaving the preheater is set to 350 to 460, preferably 380 to 425 ° C.
  • the process parameters are expediently chosen so that the proportion of condensate, based on the waste or waste plastic used, is 25 to 75, preferably 40 to 60% by weight.
  • the process is carried out in such a way that suitable mixtures of old or waste plastic are brought into the molten state and depolymerized in depolymerizer 1 at elevated temperature and the selected pressure. Solid constituents, such as aluminum or other metal residues, are drawn off at the bottom of the deposition unit 1.
  • the volatile phase obtained in depolymerizer 1 is converted in at least one condensation stage 5, 6 into a condensed phase, which is heated with exposure to hydrogen and, if necessary, after passing through a residence time section 9 to minimize residues, an effective hot separator 3 for separation into volatile products and residues are supplied.
  • the products withdrawn overhead from the hot separator 3 are fed to hydrotreating in the reactor 4 for catalytic hydrogenation and expediently separated into a syncrude and gaseous products in a cold separator 11 by heat exchange with the preheaters 2. Some of the gaseous products can be added to the fresh hydrogen to be added.
  • the Syncrude is the target product of the present process for the material recycling of old or waste plastics.
  • the residue constituents drawn off from the hot separator 3 are expanded in a device 7 suitable for this purpose and can be separated, for example in a vacuum distillation 8, into traceable distillate fractions and a residue to be discharged, which can also be partly supplied to the depolymerizate.
  • the non-condensed phase obtained in condensation stage 5 or 6 is added to the fresh hydrogen with the interposition of an HCI washer 10 to remove hydrogen chloride.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Selon le procédé décrit, des matières plastiques usagées ou des déchets de matières plastiques sont dépolymérisés en une phase pompable et une phase volatile pour permettre la récupération de matières premières chimiques et de composants carburants liquides. La phase volatile est séparée en une phase gazeuse et en un condensat. Afin que le procédé soit simplifié par rapport à l'état de la technique, le produit dépolymérisé restant après la séparation de la phase volatile est lui aussi chauffé avec le condensat ou des fractions du condensat en présence d'hydrogène sous pression et, après séparation des composants qui n'entrent pas en ébullition, est soumis à un hydrotraitement afin de produire du brut synthétique.
EP96914161A 1995-05-04 1996-05-02 Procede de traitement de matieres plastiques usagees ees ou de dechets de matieres plastiques Withdrawn EP0823935A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19516379A DE19516379A1 (de) 1995-05-04 1995-05-04 Verfahren zur Verarbeitung von Alt- oder Abfallkunststoffen
DE19516379 1995-05-04
PCT/EP1996/001812 WO1996034929A1 (fr) 1995-05-04 1996-05-02 Procede de traitement de matieres plastiques usagees ees ou de dechets de matieres plastiques

Publications (1)

Publication Number Publication Date
EP0823935A1 true EP0823935A1 (fr) 1998-02-18

Family

ID=7761076

Family Applications (1)

Application Number Title Priority Date Filing Date
EP96914161A Withdrawn EP0823935A1 (fr) 1995-05-04 1996-05-02 Procede de traitement de matieres plastiques usagees ees ou de dechets de matieres plastiques

Country Status (7)

Country Link
US (1) US5973217A (fr)
EP (1) EP0823935A1 (fr)
JP (1) JP3334883B2 (fr)
CA (1) CA2219974A1 (fr)
DE (1) DE19516379A1 (fr)
NO (1) NO974802D0 (fr)
WO (1) WO1996034929A1 (fr)

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10136619A1 (de) * 2001-07-19 2003-02-06 Abf Entwicklungsbetr Fuer Inno Vorrichtung zur Aufbereitung von organischen Abfallstoffen
US7048832B2 (en) * 2002-01-07 2006-05-23 Material Conversion Corp. Method and system for extracting hydrocarbon fuel products from plastic material
US20030187311A1 (en) * 2002-03-29 2003-10-02 Barvincak James P. Method of separating and converting hydrocarbon composites and polymer materials
DE102004003667A1 (de) * 2004-01-24 2005-08-11 Nill Tech Gmbh Verfahren zum Gewinnen von fraktionierten Kohlenwasserstoffen aus Kunststoffwertstoffen und/oder ölhaltigen Reststoffen sowie Vorrichtung hierzu
US8192586B2 (en) 2010-03-31 2012-06-05 Agilyx Corporation Devices, systems, and methods for recycling plastic
US7758729B1 (en) * 2006-08-24 2010-07-20 Plas2Fuel Corporation System for recycling plastics
US8193403B2 (en) 2006-08-24 2012-06-05 Agilyx Corporation Systems and methods for recycling plastic
US20090007484A1 (en) * 2007-02-23 2009-01-08 Smith David G Apparatus and process for converting biomass feed materials into reusable carbonaceous and hydrocarbon products
US7893307B2 (en) * 2007-02-23 2011-02-22 Smith David G Apparatus and process for converting feed material into reusable hydrocarbons
WO2014106650A2 (fr) 2013-01-03 2014-07-10 EZER, Argun Procédés et dispositifs de dépolymérisation d'une matière première hydrocarbonée
MX362467B (es) 2013-04-06 2019-01-18 Agilyx Corp Sistemas y metodos para acondicionar petroleo crudo sintetico.
EP4259749A2 (fr) 2020-12-10 2023-10-18 Agilyx Corporation Systèmes et procédés pour le recyclage de déchets plastiques

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2530229A1 (de) * 1975-07-07 1977-01-27 Helmut Dr Ing Wuerfel Verfahren zur umwandlung von altreifen, gummi und/oder anderen kunststoffen
DE3602041C2 (de) * 1986-01-24 1996-02-29 Rwe Entsorgung Ag Verbessertes Verfahren zur Aufarbeitung von Kohlenstoff enthaltenden Abfällen
US5061363A (en) * 1990-10-09 1991-10-29 The United States Of America As Represented By The United States Department Of Energy Method for co-processing waste rubber and carbonaceous material
DE4207976C2 (de) * 1992-03-13 2001-03-15 Rwe Umwelt Ag Verfahren zur Herstellung Olefinen durch thermische Behandlung von Kunststoffabfällen
DE4311034A1 (de) * 1993-04-03 1994-10-06 Veba Oel Ag Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoff
EP0710270B1 (fr) * 1993-07-20 1997-01-02 Basf Aktiengesellschaft Procede de recyclage de matieres plastiques dans un vapocraqueur

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO9634929A1 *

Also Published As

Publication number Publication date
JPH11504955A (ja) 1999-05-11
NO974802L (no) 1997-10-17
JP3334883B2 (ja) 2002-10-15
NO974802D0 (no) 1997-10-17
WO1996034929A1 (fr) 1996-11-07
DE19516379A1 (de) 1996-11-07
US5973217A (en) 1999-10-26
CA2219974A1 (fr) 1996-11-07

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