EP0784661B1 - Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets - Google Patents

Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets Download PDF

Info

Publication number
EP0784661B1
EP0784661B1 EP95935425A EP95935425A EP0784661B1 EP 0784661 B1 EP0784661 B1 EP 0784661B1 EP 95935425 A EP95935425 A EP 95935425A EP 95935425 A EP95935425 A EP 95935425A EP 0784661 B1 EP0784661 B1 EP 0784661B1
Authority
EP
European Patent Office
Prior art keywords
depolymerized
depolymerized material
depolymerizate
coal
reactor
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
EP95935425A
Other languages
German (de)
English (en)
Other versions
EP0784661A1 (fr
Inventor
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.)
CLAUS STRECKER
KLAUS NIEMANN
ROLF HOLIGHAUS
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
Priority claimed from DE4435238A external-priority patent/DE4435238A1/de
Application filed by Veba Oel AG filed Critical Veba Oel AG
Publication of EP0784661A1 publication Critical patent/EP0784661A1/fr
Application granted granted Critical
Publication of EP0784661B1 publication Critical patent/EP0784661B1/fr
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
    • 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 obtaining chemical raw materials and / or liquid fuel components made from old or waste plastics where the old or waste plastics at an elevated temperature, possibly with the addition of a liquid Auxiliary phase, a solvent or solvent mixture, depolymerized and the resulting gaseous and condensable depolymerization products (Condensate) as well as a pumpable viscous depolymerization products containing the bottom phase (depolymerized product) is withdrawn in separate substreams and Condensate and depolymerizate are worked up separately as well as the use of a manufactured by this method Depolymerizates.
  • process parameters are preferably chosen so that the highest possible Share of condensate arises.
  • the individual product streams, especially the condensate, can further processing afterwards in the sense of raw material recycling, e.g. B. used as raw materials for olefin production in ethylene plants.
  • An advantage of the method is that inorganic Minor components of the old or waste plastics are concentrated in the sump phase be, while the condensate not containing these ingredients in less complex process can be processed.
  • the process parameters temperature and dwell time can be set be 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 under the process conditions remains pumpable.
  • a useful approximation can be that an increase the temperature around 10 ° C with an average residence time the yield of the in volatile phase passing products increased by more than 50%.
  • the residence time dependency 6 shows two typical temperatures.
  • the preferred temperature range for the depolymerization process is 150 to 470 ° C.
  • a range of 250 is particularly suitable up to 450 ° C.
  • the residence time can be 0.1 to 20 hours. As generally sufficient a range of 1 to 10 h has been found.
  • the pressure is less critical Size. So it may be preferable to use the vacuum method perform, e.g. B. if volatile components due to procedural reasons have to be deducted. However, relatively high pressures are practicable, too however, a higher expenditure on equipment. In general, the pressure should be are in the range from 0.01 to 300 bar, in particular 0.1 to 100 bar.
  • the procedure can preferably be good at normal pressure or slightly above z. B. up to about 2 bar perform, which significantly reduces the expenditure on equipment.
  • the depolymerization can be carried out in a conventional reactor, e.g. B. a stirred tank reactor, be carried out on the appropriate process parameters, such as pressure and temperature is designed.
  • Suitable reactors are in the unpublished German patent applications P 44 17 721.6 and P 44 28 355.5.
  • the reactor contents are protected against overheating circulatory system connected to the reactor.
  • This circulatory system in a preferred embodiment comprises an oven / heat exchanger and one powerful pump.
  • the advantage of this method is that high circulation flow through the external furnace / heat exchanger is achieved on the one hand the necessary temperature increase of that in the circulatory system Material remains low, on the other hand favorable transmission conditions in the furnace / Allow heat exchangers to have moderate wall temperatures. This will make local Overheating and thus uncontrolled decomposition and coke formation largely avoided.
  • the heating of the reactor contents is comparatively very gentle.
  • a high circulation flow can preferably be achieved with powerful centrifugal pumps to reach.
  • the reactor is designed so that the extraction device for the circulation (circulation system) lies in a riser for the essentially liquid reactor content.
  • rate of climb essentially determined through the dimensioning of the ascent section and the dimensioning of the circulating current, particles with a higher sink rate, which are the cause of the erosion, be kept out of circulation.
  • the Rise path within the reactor can be designed in the form of a tube, which in the is mounted essentially vertically in the reactor (see FIG. 1).
  • the Riser can also be realized in that a partition in the reactor Segments divided (see Figure 2).
  • the tube or the partition does not close with the reactor cover, protrude but beyond the fill level.
  • the pipe or partition are far enough from the reactor floor removed that the reactor contents unimpeded and without major turbulence in the ascent can flow in.
  • the solids are drawn off at the bottom of the reactor together with the amount of depolymerizate that is to be used for further processing. So that the sedimented Inert substances are removed from the reactor as completely as possible the removal device for the depolymerizate preferably in the lower area, especially attached to the bottom of the reactor.
  • the reactor preferably tapers downward in the bottom area, e.g. B. tapered, or as a standing on its top Cone jacket.
  • Figure 1 shows such a device in the sense of an embodiment.
  • reactor (1) from storage container (13) old and waste plastic via addition device (18) by means of a gas-tight metering device (14) z. B. on introduced by pneumatic means.
  • a gas-tight metering device is, for example a cellular wheel sluice well suited.
  • the depolymerizate including the contained Inert substances can be removed via device (7) at the bottom of the reactor.
  • the plastic is added and the depolymerized product is removed advantageously continuously and is designed so that approximately a certain Filling level (3) of the reactor content is maintained.
  • the resulting device (4) Gases and condensable products from the top of the reactor deducted.
  • the contents of the reactor are transferred to the circulation system via a discharge line (16) via pump (5) for gentle heating in furnace / heat exchanger (6) and recirculated to reactor (1) via inflow (17).
  • tube (20) is vertical arranged, which forms a riser (2) for the reactor recycle stream.
  • the depolymerization stream withdrawn from the reactor is a factor of 10 to 40 less than the circulating current.
  • This depolymerization stream is z. B. on wet mill (9) driven to the inert components contained therein for further use Bring processing allowable size.
  • the depolymerization stream can also over a further separation device (8), where it is from the inert components is largely exempt. Suitable separation devices are, for example Hydrocyclones or decanters.
  • the inert components (11) can then be separated removed and recycled, for example.
  • the rest of the processing is z. B. bottom phase hydrogenation, Smoldering or gasification fed (12). Part of the depolymerizate can be taken directly from the circulatory system via a line (15) and the Further processing can be supplied.
  • FIG. 2 shows a similarly constructed reactor as in FIG. 1 with the difference that that the ascent section is not formed by a tube, but by a reactor segment, which is separated from the rest of the reactor content by a partition (19) is.
  • Figure 3 shows a depolymerization system with two containers, each on different Temperature level can be operated.
  • the first depolymerization tank (28) is equipped, for example, with a stirrer (33) to control the Lock (31) used and waste plastics quickly fed into the present to be able to mix in hot depolymerizate.
  • the downstream second depolymerization tank (1) corresponds to the reactor from Fig. 1.
  • the circuit for gentle Heating up, essentially consisting of pump (5) and furnace / heat exchanger (6) is therefore low in solids.
  • the depolymerizate including the solid components is withdrawn from the bottom of the reactor.
  • the solid / liquid ratio on the removal device (7) of the container (1) between 1: 1 and 1: 1000.
  • the removal device (7) is preferably a drop section (21) with one for this purpose immediately downstream branch (22), which is essentially at right angles.
  • Falling section (21) and branch (22) can be designed as a T-shaped tube.
  • the branch can also be equipped with mechanical separation aids (23) be.
  • a stream of organic under the present conditions derived essentially liquid components of the depolymerizate will.
  • the depolymerizate is conveyed via pump (27) for further processing or can also be returned at least partially via line (32) to reactor (1).
  • the amount derived can be up to a thousand times the amount of solids discharged be. In extreme cases and temporarily if necessary, nothing can be said about Branch (22) can be derived. By determining the via branch (22) deducted amount of depolymerizate can suitable flow conditions for the safe discharge of the solids can be guaranteed. At the same time, the Derived current should be such that solid particles are not as significant as possible Scope to be swept away. The ratio is preferably from discharged amount of solids to the derived amount 1:50 and 1:200.
  • Falling section (21) or the downspout is in a special embodiment at the bottom Provide a lock (24) at the end. Above this lock is an addition device (25) attached for flushing oil.
  • FIG. 5 shows a procedural alternative, in which the drop section (21) Separating device (26) is connected directly downstream. There is preferably an addition device on this (25) attached for flushing oil.
  • Rinsing oil with a higher density than that of the depolymerizate is added via the addition device (25) added in an amount that has a low upward flow rate the liquid within the drop distance between the addition device (25) and branch (22). This ensures that the drop distance (21) or Down pipe below the branch (22) is always filled with relatively fresh flushing oil. In this part of the drop section (21) there is a so-called stable stratification Flushing oil. If nothing is diverted via branch (22), the flushing oil rises in the falling section (21) and ultimately arrives in reactor (1).
  • the depolymerizate While preferably the majority of the organic components of the depolymerizate is derived through branch (22), pass through the depolymerizate contained, predominantly inorganic solid particles, which are sufficient Have sink rate, the part of the drop section (21) filled with flushing oil. For this purpose, the organic depolymerizate constituents still adhering to the solid particles washed off or dissolved in the flushing oil.
  • the difference in density between the depolymerizate and the flushing oil should be at least 0.1 g / ml, preferably 0.3 to 0.4 g / ml.
  • the depolymerizate has one Temperature of 400 ° C a density of the order of 0.5 g / ml.
  • Flushing oil can e.g. B. a heated to about 100 ° C vacuum gas oil with a density of approx. 0.8 g / ml can be used.
  • the length of the portion of the drop section (21) filled with flushing oil is dimensioned such that the solid particles at the lower end of the drop section (21) at least largely are free from adhering organic depolymer components. It is also dependent of type, composition, temperature and the quantities enforced of the depolymerizate and the flushing oil used. Those skilled in the art can use relative simple tests the optimal length of the part of the drop section filled with flushing oil (21) determine.
  • Lock (24) is used for pressure separation of the previous and the following plant section.
  • a cellular wheel sluice is preferred used.
  • other types of locks e.g. B. cycle locks are suitable for this purpose.
  • the discharged mixture has a solids content from about 40 to 60% by weight.
  • lock (24) is followed by a further separation device (26) for separation of flushing oil and solid particles.
  • a scraper conveyor or a screw conveyor is preferably used as the separating device (26) used. These are directed obliquely upwards in the conveying direction. Prefers is an angle to the horizontal of 30 to 60 °, in particular about 45 °.
  • FIG. 5 shows another process variant.
  • the solid particles pass through here after passing the falling distance (21) immediately the separating device (26).
  • Most of flushing oil freed solid particles are then over lock (24), z. B. a cellular wheel lock or cycle lock, discharged.
  • a drainage screw (26) is shown schematically in FIG Separator can act.
  • a flushing oil can also be carried out via line (30) with a lower density, e.g. B. a middle distillate oil.
  • the used flushing oil can be discharged via line (29), or at least partially into the via branch (22) derived depolymerizate can be introduced.
  • the separator (26) works here preferably under atmospheric conditions. The so separated Solid particles are discharged via line (11) and can be recycled be fed.
  • the solid discharged via line (11) consists predominantly of metallic Aluminum, which is then used for recycling this material can be.
  • FIG. 4 shows an enlarged detail of FIG. 3, the T-shaped arrangement of Fall section (21) and branch (22). Mechanical separation aids are also shown (23) and the flow conditions shown schematically with arrows.
  • the depolymerizate After separation of gas and condensate, the depolymerizate is easy to handle, since it remains well pumpable above 200 ° C and is a good feed material in this form for the subsequent process stages and other uses represents.
  • the depolymerizate can also solidify by means of a so-called cooling belt and thus brought into a solid form.
  • a so-called cooling belt are suitable for.
  • endless belts made of stainless steel. They usually run under tension over cylindrical ones Deflection drums or deflection disks.
  • the product can, for example, by means of a Broadband nozzle can be applied as a film in the front area of the cooling belt.
  • the underside of the cooling belt is sprayed with cooling liquid, the product but is not wetted. This cooling of the strip also causes this to happen existing product lowers temperature and solidifies.
  • the depolymerizate can be cooled by supply air from above.
  • the solid film formed can at the end of the cooling belt z.
  • the depolymerizate can be pumped directly into the subsequent process stages introduced or used for other purposes. If intermediate storage is necessary, this should be done in tanks in the the depolymerizate is kept at temperatures at which it is easy to pump remains, usually at over 200 ° C. If longer storage is desired, please do so lends itself to storing the depolymerizate in solid form. In broken form the depolymerizate can be transported in the same way as fossil fuel hard coal, stored and fed to subsequent processes and uses.
  • the present invention relates to methods according to claims 1, 3 and 5 and uses according to claims 7 and 8.
  • a depolymerizate is preferred used, which is at least largely of coarser inorganic Solid particles, especially metallic aluminum, are freed.
  • At least a partial stream of the depolymerized product is subjected to coking together with coal.
  • coal is suitable for the production of high quality coke.
  • a such coke for example metallurgical coke, should be as coarse as possible and less friable be. It must have a minimum strength so that it is sufficient Filling in the blast furnace can be achieved without the coke under the weight the bed disintegrates and as a result the blast furnace is clogged.
  • Suitable coals are, for example, the baking fat coal of the Ruhr area or gas coal Such baking coals are available in limited quantities and are more expensive than, for example, boiler coal.
  • the depolymerizate is a suitable fuel for use in all types of power plants and in cement plants.
  • the depolymerizate both liquid at temperatures above 200 ° C over lances, e.g. B. as a substitute for heavy fuel oil, be injected or in solid form, e.g. B. broken or ground, introduced.
  • At least one Partial stream of the depolymerized product is used as a reducing agent in a blast furnace process.
  • the depolymerizate can also be used as a substitute for heavy fuel oils, which are usually used for this purpose. It turns out here, as in thermal recycling, the relative low chlorine of the Depolymerizate of less than 0.5 wt .-% as a special advantage.
  • the depolymerizate leaves It is therefore advantageous as a binding additive in the coking of coal, as a reducing agent in blast furnace processes and as fuel in combustion plants, power plants and cement plants.
  • Polymer modified bitumen is used in many areas of the Construction industry, especially used in roof sealing materials and in road construction.
  • the polymers contained in the depolymer ize the properties of the Bitumen such as toughness, stretchability and abrasion ability improved.
  • the depolymerizate works due to its residual reactivity when heated together with bitumen and bitumen derivatives chemical bonds. This is partly the cause of the mentioned and desired property improvements.
  • This modification can reduce the cold flexibility and the stability of the bituminous Material can be improved.
  • An improvement in the elastic properties the bitumen and the adherence to the mineral filling material can also be achieved by admixing polymers.
  • the chemical reaction with the bitumen also has the advantage that z. B. in hot storage none Segregation can take place or this is severely restricted.
  • the residual reactivity the depolymerizate can be introduced by introducing functional groups, for example according to the procedures according to European patent applications EP 0 327 698, EP 0 436 803 and EP 0 537 638 can be increased. If necessary. can the so modified Bitumen or bituminous products also contain crosslinking agents (see EP 0 537 638 A1).
  • a stirred tank reactor with 80 m 3 content which is provided with a circulation system with a capacity of 150 m 3 / h
  • 5 t / h mixed agglomerated plastic particles with an average grain diameter of 8 mm were fed pneumatically.
  • the mixed plastic was material that came from a household collection of the Dual System Germany (DSD) and typically contained 8% PVC.
  • 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: I. II III IV T [° C] Gas [wt%] Condensate [% by weight] Depolymerizate [% by weight] HCl [% by weight] 360 4th 13 81 2nd 380 8th 27 62 3rd 400 11 39 46 4th 420 13 47 36 4th
  • the depolymerizate stream (III) was drawn off continuously.
  • the viscosity of the depolymerizate was 200 mPas at 175 ° C.
  • Depolymerizate from processing from waste plastics from household collections of the DSD according to Example 1 was one in different proportions Coking coal added. The mixtures were coked in a test coke oven.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Coke Industry (AREA)
  • Working-Up Tar And Pitch (AREA)

Claims (10)

  1. Procédé d'obtention de matériau brut chimique et de composant combustible liquide à partir de matière plastique usée ou de rejet, dans lequel on dépolymérise les matières plastiques usées ou de rejet à une température augmentée, le cas échéant en ajoutant une phase auxiliaire liquide, d'un solvant ou mélange de solvants, et l'on retire les produits de dépolymérisation (produit de condensation) gazeux et condensables apparus ainsi qu'une phase de décantation contenant des produits de dépolymérisation visqueuse et pompable (produit de dépolymérisation) dans des courants partiels séparés, et on traite le produit de condensation ainsi que le produit de dépolymérisation séparément l'un de l'autre,
    caractérisé en ce qu'
    on soumet au moins un courant partiel du produit de dépolymérisation à du charbon cokéfiant pour améliorer le processus de chauffage lors de la cokéfaction
    et en ce qu'
    on le soumet à une cokéfaction avec le charbon.
  2. Procédé selon la revendication 1,
    caractérisé en ce qu'
    on utilise le produit de dépolymérisation et le charbon dans un rapport de 1:200 à 1:10, de préférence de 1:50 à 1:20.
  3. Procédé selon le préambule de la revendication 1,
    caractérisé en ce qu'
    on soumet au moins un courant partiel du produit de dépolymérisation à une oxydation en utilisant la chaleur de réaction alors apparue.
  4. Procédé selon la revendication 3,
    caractérisé en ce que
    l'oxydation du produit de dépolymérisation s'effectue dans les centrales électriques et les usines de ciment.
  5. Procédé selon le préambule de la revendication 1,
    caractérisé en ce qu'
    on valorise au moins un courant partiel du produit de dépolymérisation comme réducteur dans un procédé se déroulant dans un haut fourneau.
  6. Procédé selon au moins l'une des revendications précédentes,
    caractérisé en ce qu'
    on utilise le produit de dépolymérisation comme masse pompable ayant une température supérieure à 200°C ou comme solide de préférence broyé ou concassé après refroidissement.
  7. Utilisation d'un produit de dépolymérisation fabriqué selon un procédé du préambule de la revendication 1 comme combustible dans les installations de mise à feu, les centrales électriques et les usines de ciment, et comme réducteur dans des processus se déroulant dans des hauts fourneaux, ainsi que comme additif liant lors de la cokéfaction du charbon.
  8. Utilisation d'un produit de dépolymérisation fabriqué selon un procédé du préambule de la revendication 1 comme additif à des bitumes et à des produits bitumineux.
  9. Utilisation selon la revendication 8,
    caractérisée en ce qu'
    on ajoute pour 100 parties en poids de bitume de 1 à 20, de préférence de 5 à 15 parties en poids de produit de dépolymérisation.
  10. Utilisation selon l'une des revendications 7 à 9,
    caractérisée en ce qu'
    on utilise un produit de dépolymérisation qui est au moins largement débarrassé des particules solides inorganiques les plus grossières.
EP95935425A 1994-10-04 1995-10-02 Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets Expired - Lifetime EP0784661B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4435238 1994-10-04
DE4435238A DE4435238A1 (de) 1993-04-03 1994-10-04 Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoffen
PCT/EP1995/003901 WO1996010619A1 (fr) 1994-10-04 1995-10-02 Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets

Publications (2)

Publication Number Publication Date
EP0784661A1 EP0784661A1 (fr) 1997-07-23
EP0784661B1 true EP0784661B1 (fr) 1998-07-22

Family

ID=6529787

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95935425A Expired - Lifetime EP0784661B1 (fr) 1994-10-04 1995-10-02 Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets

Country Status (24)

Country Link
US (1) US5789636A (fr)
EP (1) EP0784661B1 (fr)
JP (1) JP3462216B2 (fr)
CN (1) CN1159821A (fr)
AT (1) ATE168714T1 (fr)
AU (1) AU688145B2 (fr)
BG (1) BG63346B1 (fr)
BR (1) BR9509235A (fr)
CA (1) CA2201777A1 (fr)
CZ (1) CZ101897A3 (fr)
DE (1) DE59502919D1 (fr)
DK (1) DK0784661T3 (fr)
ES (1) ES2120770T3 (fr)
FI (1) FI971375A (fr)
GR (1) GR3027760T3 (fr)
HU (1) HUT77197A (fr)
NO (1) NO971486L (fr)
NZ (1) NZ294602A (fr)
PL (1) PL185814B1 (fr)
RO (1) RO118134B1 (fr)
RU (1) RU2151163C1 (fr)
SK (1) SK283104B6 (fr)
WO (1) WO1996010619A1 (fr)
ZA (1) ZA958364B (fr)

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE60107959T2 (de) * 2000-07-27 2005-12-15 E.I. Du Pont De Nemours And Co., Wilmington Oxidative umsetzung von polymeren zu anwendbaren chemikalien
ES2224863B1 (es) * 2003-07-07 2006-12-16 Consejo Sup. De Invest. Cientificas Procedimiento para la utilizacion de plasticos de desecho como fuente nutritiva carbonada de microorganismos de interes biotecnologico industrial.
ITTP20030002A1 (it) * 2003-10-09 2005-04-10 Giovanni Maurizio Di Processo ossidoriduzione per riciclare qualsiasi frazione rifiuto:fanghi, scarti industriali, agroalimentari, macellazione, ittici, ecc. in biostabilizzato sterile e/o polixano espanso isolante termoacustico, in innovativo impianto mobile o fisso con
DE102004038220B4 (de) * 2004-08-05 2009-07-23 Proton Technology Gmbh I.Gr. Thermische Biomassenverölung
UA90089C2 (ru) * 2006-02-08 2010-04-12 Григорий БЕРЕЗИН Способ производства кокса из неспекающихся марок угля и устройство для его осуществления
ES2294964B1 (es) * 2007-04-27 2009-04-16 Sistemas De Reciclaje Y Energia, S.L Sistema y proceso de reciclado de plasticos.
US8317980B2 (en) * 2008-09-17 2012-11-27 Nantong Tianyi Environment And Energy Technology Limited Corporation Reactor for converting waste materials into fuel, a feeding system for feeding waste materials into the reactor, and methods for converting waste materials into fuel
US20100065410A1 (en) * 2008-09-17 2010-03-18 Jianguo Li High temperature separable continuous residue discharging system and method of using the same
WO2011144322A2 (fr) * 2010-05-17 2011-11-24 Dieter Wagels Procédé et installation de dépolymérisation de matières contenant des hydrocarbures
CN102344823B (zh) * 2011-09-06 2014-01-01 六盘水师范学院 一种温和条件下使煤与废塑料共液化的方法
PL422836A1 (pl) * 2017-09-14 2019-03-25 Polymer Energy Polska Spółka Z Ograniczoną Odpowiedzialnością Dodatek w postaci preparatu do stałych paliw biomasowych i odpadów biomasowych a także do uzdatnionych mułów i flotów węglowych oraz osadów ściekowych i paliw formowanych z odpadów, przeznaczony zwłaszcza do procesów spalania, współspalania, zgazowania i odgazowania paliw stałych
TWI694064B (zh) * 2018-09-26 2020-05-21 遠東新世紀股份有限公司 對苯二甲酸的製造方法及其系統
BE1026748B1 (nl) * 2018-10-31 2020-06-04 Montair Process Tech Systeem en werkwijze voor het pyrolyseren van organisch afval
US11852258B2 (en) * 2020-12-31 2023-12-26 Tapcoenpro, Llc Systems and methods for purging an isolation valve with a liquid purge medium

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2202903B1 (de) * 1972-01-21 1972-11-30 Karwat Ernst Dr Ing Verfahren zur Beseitigung und Verwertung von Kraftfahrzeugreifen-Altmaterial
JPS51135901A (en) * 1975-05-21 1976-11-25 Mitsui Cokes Kogyo Kk Process for producing coke
DE2530229A1 (de) * 1975-07-07 1977-01-27 Helmut Dr Ing Wuerfel Verfahren zur umwandlung von altreifen, gummi und/oder anderen kunststoffen
FR2512032B1 (fr) * 1981-09-01 1983-12-16 Bruss Ti Kirova Procede d'obtention d'un ramollissant pour melanges caoutchoucs et de mazout
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
US5364996A (en) * 1992-06-09 1994-11-15 Texaco Inc. Partial oxidation of scrap rubber tires and used motor oil
DE4311034A1 (de) * 1993-04-03 1994-10-06 Veba Oel Ag Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoff

Also Published As

Publication number Publication date
BG101423A (en) 1997-12-30
CA2201777A1 (fr) 1996-04-11
SK41997A3 (en) 1997-09-10
AU3744895A (en) 1996-04-26
RO118134B1 (ro) 2003-02-28
DK0784661T3 (da) 1998-11-16
WO1996010619A1 (fr) 1996-04-11
SK283104B6 (sk) 2003-02-04
ZA958364B (en) 1996-05-13
DE59502919D1 (de) 1998-08-27
BR9509235A (pt) 1997-10-21
NO971486L (no) 1997-05-22
AU688145B2 (en) 1998-03-05
JPH10506662A (ja) 1998-06-30
BG63346B1 (bg) 2001-10-31
PL319453A1 (en) 1997-08-04
ATE168714T1 (de) 1998-08-15
CZ101897A3 (en) 1997-08-13
FI971375A0 (fi) 1997-04-03
US5789636A (en) 1998-08-04
RU2151163C1 (ru) 2000-06-20
EP0784661A1 (fr) 1997-07-23
JP3462216B2 (ja) 2003-11-05
ES2120770T3 (es) 1998-11-01
PL185814B1 (pl) 2003-08-29
FI971375A (fi) 1997-06-03
GR3027760T3 (en) 1998-11-30
NZ294602A (en) 2000-01-28
NO971486D0 (no) 1997-04-02
CN1159821A (zh) 1997-09-17
HUT77197A (hu) 1998-03-02

Similar Documents

Publication Publication Date Title
DE4435238A1 (de) Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoffen
EP2981572B1 (fr) Procédé de décomposition de polymères synthétiques et dispositif permettant la mise en oeuvre du dit procédé
EP0759962B1 (fr) Dispositif de depolymerisation de matieres plastiques usagees et de recuperation
EP0182309B1 (fr) Procédé pour la réutilisation par hydration de déchets contenant du carbone d'origine synthétique
DE69205164T2 (de) Durch Vakuumpyrolyse Rückgewinnung von Kraftfahrzeugzerkleinererrückstand.
EP0784661B1 (fr) Procede pour la recuperation de matieres premieres synthetiques et de composants de carburants provenant de matieres plastiques hors d'usage ou de dechets
DE68908205T2 (de) Wiederverwertung von ölhaltigen Raffinierrückständen.
DE2456575C2 (de) Verfahren zur Herstellung von Elektrodenkoks
EP2705117B1 (fr) Procédé pour préparer de manière énergétiquement efficace des gisements secondaires
EP2876146A1 (fr) Procédé et installation de préparation de substances de valeur en plastique
DE4344311A1 (de) Verfahren und Vorrichtung zur thermischen Depolymerisation von Kunststoffen
EP0713906A1 (fr) Procédé de recyclage de matériaux plastiques dans une unité de vapocraquage
DD158795A5 (de) Verfahren zur herstellung einer normalerweise festen geloesten kohle
WO2014106650A2 (fr) Procédés et dispositifs de dépolymérisation d'une matière première hydrocarbonée
DE3401840A1 (de) Verfahren und anlage zur aufbereitung schwerer rohoele insbesondere zur herstellung von koksen fuer metallurgische zwecke
EP0113811A2 (fr) Procédé pour la production de matières premières à partir de déchets de matières synthétiques et installation pour la mise en oeuvre du procédé
DE3715158C1 (de) Verfahren zur Gewinnung von Schweloel
DE4344845C1 (de) Verfahren zur Herstellung von Kohlenwasserstoffschmelzen aus Polyolefinen
US4146459A (en) Treatment of coal liquefaction effluent
DE4417721A1 (de) Vorrichtung zur Depolymerisation von Alt- und Abfallkunststoffen
DE4417386A1 (de) Verfahren zur Herstellung destillierbarer Kohlenwasserstoffe
DE3339139A1 (de) Verfahren zum trocknen und desoxygenieren von fuer die kohleverfluessigung bestimmter kohle
CH660021A5 (de) Verfahren und anlage zur aufbereitung schwerer rohoele, insbesondere fuer eine nutzung derer kokse fuer metallurgische zwecke.
DE102021133899A1 (de) Pyrolyseverfahren und Pyrolysevorrichtung zur Herstellung von Pyrolysegas und Pyrolysekoks
DE19707304B4 (de) Verfahren zur Gewinnung von Mikrowachsen, Paraffinen und Ölen aus Altkunststoffen oder Altkunststoffgemischen

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: 19970408

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

AX Request for extension of the european patent

Free format text: LV PAYMENT 970408

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

17Q First examination report despatched

Effective date: 19970926

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

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

AX Request for extension of the european patent

Free format text: LV PAYMENT 970408

REF Corresponds to:

Ref document number: 168714

Country of ref document: AT

Date of ref document: 19980815

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: NV

Representative=s name: TROESCH SCHEIDEGGER WERNER AG

Ref country code: CH

Ref legal event code: EP

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

Effective date: 19980723

REF Corresponds to:

Ref document number: 59502919

Country of ref document: DE

Date of ref document: 19980827

ET Fr: translation filed
REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 19980724

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2120770

Country of ref document: ES

Kind code of ref document: T3

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: GERMAN

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

REG Reference to a national code

Ref country code: IE

Ref legal event code: FD4D

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: GR

Payment date: 19990730

Year of fee payment: 5

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

Ref country code: PT

Payment date: 19990805

Year of fee payment: 5

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

Ref country code: IE

Payment date: 19991021

Year of fee payment: 5

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

Ref country code: MC

Payment date: 19991028

Year of fee payment: 5

Ref country code: DK

Payment date: 19991028

Year of fee payment: 5

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

Ref country code: CH

Payment date: 19991223

Year of fee payment: 5

REG Reference to a national code

Ref country code: IE

Ref legal event code: FD4D

Ref document number: ERRATA: Incorrectly

Country of ref document: IE

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: 20001002

Ref country code: DK

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

Effective date: 20001002

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

Ref country code: MC

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 20001031

Ref country code: LI

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

Effective date: 20001031

Ref country code: GR

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

Effective date: 20001031

Ref country code: CH

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

Effective date: 20001031

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

Ref country code: DE

Payment date: 20001113

Year of fee payment: 8

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: 20010430

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

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

Ref country code: GB

Payment date: 20020909

Year of fee payment: 8

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

Ref country code: NL

Payment date: 20021017

Year of fee payment: 8

Ref country code: FR

Payment date: 20021017

Year of fee payment: 8

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

Ref country code: AT

Payment date: 20021022

Year of fee payment: 8

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

Ref country code: SE

Payment date: 20021023

Year of fee payment: 8

Ref country code: LU

Payment date: 20021023

Year of fee payment: 8

Ref country code: BE

Payment date: 20021023

Year of fee payment: 8

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

Ref country code: ES

Payment date: 20021024

Year of fee payment: 8

BECA Be: change of holder's address

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

Effective date: 20030225

BECH Be: change of holder

Owner name: *DUALES SYSTEM DEUTSCHLAND A.G.

Effective date: 20030225

NLS Nl: assignments of ep-patents

Owner name: CLAUS STRECKER

Owner name: KLAUS NIEMANN

Owner name: ROLF HOLIGHAUS

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

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: 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: 20031002

Ref country code: GB

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

Effective date: 20031002

Ref country code: AT

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

Effective date: 20031002

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: 20031003

Ref country code: ES

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

Effective date: 20031003

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: 20031031

BERE Be: lapsed

Owner name: *DUALES SYSTEM DEUTSCHLAND A.G.

Effective date: 20031031

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: 20040501

Ref country code: DE

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

Effective date: 20040501

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

Effective date: 20031002

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: 20040630

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

Effective date: 20040501

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20031003

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: 20051002