EP1745115B1 - Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux - Google Patents

Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux Download PDF

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Publication number
EP1745115B1
EP1745115B1 EP05701145A EP05701145A EP1745115B1 EP 1745115 B1 EP1745115 B1 EP 1745115B1 EP 05701145 A EP05701145 A EP 05701145A EP 05701145 A EP05701145 A EP 05701145A EP 1745115 B1 EP1745115 B1 EP 1745115B1
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European Patent Office
Prior art keywords
oil
gas
condenser
heat
order
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EP05701145A
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German (de)
English (en)
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EP1745115A1 (fr
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Wolf-Eberhard Nill
Anton Schmillen
Gerold Weser
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Nick Wolfgang
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Nick Wolfgang
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Priority claimed from DE102004003667A external-priority patent/DE102004003667A1/de
Application filed by Nick Wolfgang filed Critical Nick Wolfgang
Priority to PL05701145T priority Critical patent/PL1745115T3/pl
Priority to EP05701145A priority patent/EP1745115B1/fr
Priority to SI200531238T priority patent/SI1745115T1/sl
Publication of EP1745115A1 publication Critical patent/EP1745115A1/fr
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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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/006—Combinations of processes provided in groups C10G1/02 - C10G1/08

Definitions

  • the invention relates to a method for obtaining fractionated hydrocarbons from plastic materials and / or from oil-containing residues, wherein the plastic materials and / or residues sorted by variety and compacted using a registration system and the compacted mass to a melting vessel, preferably below the liquid level, fed and is heated so that a separation into a first liquid phase, a first gas phase and a residue portion takes place, according to the preamble of claim 1;
  • the invention relates to an apparatus for performing the method according to the preamble of claim 16 for obtaining fractionated hydrocarbons from plastic materials and / or from oil-containing residues.
  • Plastics such as polypropylene (PP), polyethylene (PE) or polystyrene, which consist of long-chain macromolecules, must be split into small molecules for their utilization. Through a conversion plant, such plastics can be converted in a low-temperature cracking process into an oil-like product with gaseous admixtures and a solid residue.
  • PP polypropylene
  • PE polyethylene
  • polystyrene which consist of long-chain macromolecules
  • the resulting gas during the cracking process consists of a mixture of methane, ethane, ethene, propane, propylene, i-butene, i-butane, 1-butene, 1-butane, pentane, etc., and a small amount of water vapor.
  • the polystyrene-derived oil consists of more than 50% styrenes and also contains 2-methyl-styrenes, toluene, ethylbenzene and benzene.
  • the oil obtained from polyethylene and polypropylene consists mainly of paraffins and olefins and contains only small amounts of aromatics.
  • the low-volatile residues consist of cokes, heavy oil-like long-chain hydrocarbons. The oil-like residue can in a further process step be mixed with water. This produces an oil-water emulsion, which can be utilized energetically, for example as a lighting agent.
  • the device has a first heatable melting container to which the plastics are fed via a feed screw and in which the melting of the plastics results in a first liquid phase which can be fed to a further second container to which a cracking tower for oil extraction is connected. From the second container, the liquid phase is traceable back into the heatable first melt container in a circulation process for further heating.
  • plastic raw materials for melting and vaporization are brought within a container (melting and cracking reactor), which are supplied to the container via a feed screw.
  • the plastic raw materials are heated to 280 ° C to 380 ° C and cracked.
  • the disadvantage here is the single-stage entry of the necessary heat energy.
  • the high heat flow density leads to strong partial overheating. These then lead to the formation of encrustations, which worsen the further heat input. As a result, the heat consumption is high in relation to the yield.
  • the CN 2435146Y Furthermore, a similar method has become known.
  • the device has a heatable with a burner first reaction vessel, which is preceded by a receptacle from which by means of a screw conveyor, the plastic waste together with a Catalyst in the reaction vessel to be promoted to melting.
  • the gaseous, distilled product is conveyed to a second heated reaction vessel which has a catalyst bed of catalyst particles of size between 1 mm to 15 mm in diameter, namely calcined zeolite particles about 10 mm in diameter, whereby the gas is catalytically decomposed.
  • the catalyst material which has been added to the plastic waste is recovered from the first reaction vessel and heated above 500 ° C, after which the catalyst material can be reused.
  • the invention has for its object to further develop the aforementioned method and apparatus that the energy input is improved and that in particular by an optimal and targeted use of energy and heat recovery in different areas of the efficiency of the method and the device is improved.
  • liquid phase and the first gas phase are transported to an evaporation tank in which further heat input, a second liquid phase and a second gas phase is formed, wherein the second liquid phase is transferred to a reheater and further heated there with further heat input so that a third gas phase is formed, after which the second gas phase from the evaporation vessel and third gas phase from the reheater are fed to a cracking tower, where further cracking of the long-chain hydrocarbons into short-chain hydrocarbons takes place and the resulting oil gas is then fed to a condenser, in which the oil gas is condensed to liquid oil, where the oil is the target product, and the process is carried out using a multi-circuit heating system to generate the necessary process heat for the melting tank, the evaporation tank and the reheater, and used as a heat transfer oil or salt or gas.
  • this is carried out using a multi-circuit, indirect heating system which generates the process heat for the melting tank, the evaporation tank and the reheater, it being possible to use oil or salt or gas as the heat carrier.
  • oil or salt or gas as the heat carrier.
  • a non-condensable fraction of the oil gas for thermal utilization can be supplied to the heating system for firing the same in an advantageous manner.
  • the heating system thus comprises all components for the supply of the melting vessel and the evaporation vessel with energy.
  • the thermally recoverable by-products formed in the process such as a proportion of an oil-water emulsion from the residue components from the Aufriti knowledgeer and otherwise unusable gas fractions from the Crackturm and a gas component from a flame arrester, are used in an advantageous manner in the heating system for generating the primary process heat.
  • the capacitor may consist of a precondensator and a main capacitor, which may be connected to a multi-circuit cooling system.
  • the excess heat from the pre-condenser, the main condenser and the residual pre-cooling tank is thus fed to the heating system.
  • the oil-water emulsion for thermal utilization can be supplied to the heating system for firing.
  • the inventive method advantageously has a low energy consumption and optimum energy utilization by means of heat recovery, based on the yield.
  • the heating circuit in the different process areas advantageously heats indirectly and specifically.
  • plastic materials can be recycled in accordance with the waste incineration regulations.
  • a precondensator and a main capacitor are used as the capacitor, the excess heat from the precondensator, the main capacitor and a residual precooling vessel being supplied to the heating system, and the main capacitor being connected to a multi-circuit condensation system.
  • the plastic materials and / or oily residues are comminuted in a pretreatment process after sorting and optionally dried before the cracking process is carried out.
  • the plastic materials are sorted by PP, PE and PS into hard and soft plastic parts. Since the water content of the plastics should be below 1% for energy reasons, plastics with a higher water content are dried beforehand.
  • a plug screw or a Stopftechnik which compacts the residues for oxygen deprivation.
  • the plastic materials should be fed fine shredded the stuffing screw or Stopfwerk.
  • the residue is transported within the Aufschmelz organizationsers in an underlying sedimentation where concentration of the residue is carried out and then the concentrated residue fraction is transferred to a residue precooler, in which a cooling of the residue fraction by means of a cooling medium, preferably below 120
  • the cooled residue fraction can be fed to an emulsion unit in which an oil-water emulsion is prepared from the residue fraction.
  • a precondensator is arranged between the cracking tower and the main condenser, which pre-cools the oil gas and recovers heat at a high temperature level and reduces the temperature gradient between cracking tower and main condenser.
  • the main capacitor and optionally the precondensator can be connected to a multi-circuit cooling system.
  • the inventive method is preferably carried out between 300 to 450 degrees Celsius and normal pressure up to 2 bar overpressure.
  • a device for recovering fractionated hydrocarbons from plastic materials and / or from oil-containing residues, wherein the plastic materials and / or residues are sorted by variety, with a registration system for the compression of the plastic materials and / or oily residues under exclusion of air and with a downstream reflow tank for heating and melting the compacted mass to produce a first liquid phase, a first gas phase and a residue portion, is characterized in that after the melting vessel for generating further heat input of a second liquid phase and a second gas phase, an evaporation vessel is arranged, on which the introduction and Further heating of the second liquid phase, a reheater follows to the emergence of a third gas phase, and to the evaporation vessel and the reheater for breaking (cracking) of the long-chain Hydrocarbons in short-chain hydrocarbons, a cracking tower is connected to which a condenser is connected to the condensation of the oil gas to liquid oil as the target product, the apparatus having a multi-circuit heating system for generating
  • a stuffing screw or a Stopftechnik for compressing the plastic material and / or the oil-containing residues is arranged for entering the plastic materials and / or oily residues in the melting within the registration system, before which optionally a spherical transfer container for transfer into the Plug screw or the stuffing mechanism is located.
  • the output of the plug screw or the Stopftechniks opens below the liquid level of the molten mass in the Aufschmelz disposer.
  • the same has a multi-circuit heating system for generating the necessary process heat at this optimized temperature levels, serving as a heat carrier oil or salt or gas.
  • a sedimentation compartment for receiving the residue part is arranged below the melting tank.
  • a residue precooling container as well as an emulsion unit for producing an oil-water emulsion from the residue portion.
  • the capacitor is formed of a main capacitor and a precondensator, wherein between the cracking tower and the main capacitor for precooling of the oil gas, the precondensator is arranged. Furthermore, a multi-circuit cooling system can be connected to the main capacitor.
  • the device for generating the process heat for the melting tank, the evaporation tank and the reheater on a multi-circuit heating system In a further embodiment, the device for generating the process heat for the melting tank, the evaporation tank and the reheater on a multi-circuit heating system.
  • the melting tank and the evaporation tank and, if appropriate, the after-heating tank have an externally arranged heating jacket and / or internal heating coils which can be heated via the common heat carrier heating system.
  • the process plant shown in the figures for obtaining fractionated hydrocarbons, from plastic materials and / or oily residues consists of a silo 1, in which the processed plastic materials, preferably in shredded state, are stored. The storage can also be done in a bunker.
  • a transfer container 3 for example, a flanged ball housing for flexible adaptation to different local conditions.
  • a stuffing screw 4 or a Stopftechnik connects, which compresses the plastic materials and thus largely expels the air and thus the oxygen.
  • the lower end of the plug screw 4 or Stopfwerks opens into a melting tank 7 and that below or above its level.
  • a pneumatically operated throttle-check valve 5 is arranged, which is followed by an entry fitting 6 in the form of a ball valve 6.
  • the reflow vessel 7 has at its lower end a sedimentation tray 10 for receiving and concentrating a residue fraction precipitating from the liquid phase of the compacted mass.
  • the sedimentation compartment 10 is conductively connected via three successive residue discharge fittings 11, 12 and 13 to a residue precooling vessel 15, which has an outer cooling jacket 14.
  • a residue precooling vessel 15 which has an outer cooling jacket 14.
  • Within the residue Vorkühl there is an accumulation of the residue and a cooling of the residue by means of a cooling medium from a cooling system 34, preferably below 120 ° C.
  • the pre-cooling of the residue takes place under the possibility of heat recovery in the heating system, thereby reducing the temperature gradient between Melting tank 7 and a subsequent emulsion unit 16 is given.
  • the cooled residue is fed to the emulsion unit 16 in which an oil-water emulsion is produced by means of a motor-driven agitator from the residue fraction.
  • an oil-water emulsion is produced by means of a motor-driven agitator from the residue fraction.
  • the reflow vessel 7 has an agitator 9 for homogenizing the molten plastic mass and a Abrakel adopted 17 for stripping the inner wall of the reflow vessel 7 in the region of the mouth of the screw conveyor 4 or Stopfwerks. Furthermore, the melting tank 7 is closed at the top and has a lateral outlet A in the upper area. This provides great strength in the area of the upper tank bottom by reducing the number of openings. Furthermore, the melting tank 7 is surrounded by an outer heating jacket 8, which is constructed such that a homogeneous heat input is given and in particular heat peaks are avoided during operation. Likewise, the outer heating jacket 8 allows heat removal, condensation, before maintenance or even in case of an accident.
  • the melting tank 7 and the evaporation tank 20 may be equipped with hinged concentric coiled tubing, for example two. By using coiled tubing for heat transfer, a larger transfer area is achieved.
  • the reflow tank 7 there is a heating of the plastic mass, so that a separation into a first liquid phase, a first gas phase and a residue portion takes place, after which the liquid phase and the first gas phase are transported via the outlet A line in an evaporation vessel 20, in which among others Heat input into the mass creates a second liquid phase and a second gas phase.
  • the evaporation vessel 20 is used for evaporation of valuable parts with higher evaporation temperatures.
  • the outlet A of the melting tank 7 and the inlet A of the evaporation tank 20 may have an additional heater 18, such as electric immersion heater, to which a further reheater 19 can connect to increase the heat input in the inlet of the evaporation tank 20.
  • the heat input into the evaporation tank 20 is controlled by a heating jacket 21 and / or heating coils at a higher level than in the melting tank 7 in a reduced amount of plastic, whereby a reduction in the amount of energy is given at a high temperature level.
  • the evaporation vessel 20 has a motor-driven agitator 22 for homogenizing the molten recyclable material. Within the evaporation vessel 20, the formation of a second liquid phase and a second gas phase takes place.
  • a Nachflower constituer 23 is connected by line, which has its own heater 24, which may be an electric heater E.
  • the Nachflower capableer 23 is used for further reheating and vaporizing an even smaller amount of recyclables than in the evaporation vessel 20 with the highest evaporation temperatures of the recyclables, so that in him a third gas phase is formed.
  • the evaporation tank 20 is down by means of a residue discharge fitting 25, for example of the type ball valve, closed to discharge residues.
  • the Nachflower constituer 23 has in turn at its lower end an emptying valve 26 for emptying the Nachflower mattersers 23.
  • a cracking tower 27 which serves to break up the long-chain molecules into short-chain molecules; in Crackturm 27 there is a separation of the resulting oil gas from high-boiling components.
  • the Nachflower concerninger 23 is connected in line with the cracking tower 27, so that in the same both the second gas phase from the evaporation tank 20 and the third gas phase is introduced from the Nachloom electer 23.
  • a product gas line 28, namely a pipe 28 the discharge of the product gas formed in the cracking tower in a pre-condenser 29 can be carried out, which works as a heat exchanger to recover heat at a high temperature level, so that this pre-cooling of the product gas with the possibility of heat recovery in the Heating system is done.
  • the oil gas is then supplied to the main condenser 30, in which the oil gas is condensed to liquid oil.
  • the main condenser 30 has two cooling circuits, namely a sump cooling condenser 31 and a head cooling condenser 32.
  • the main condenser 30 has an incoming and outgoing line with a circulating pump 35 for circulating the oil. Also located in the line are two automatic valves with a throttle function for switching and dividing the recirculation flow to the main condenser 30 or into a transfer line 37 to a separator (not shown).
  • the conduit further has a metering point 40 as an injection site for delivery of additives, for example, to condition, stabilize and adjust product properties of the product oil.
  • Addition of an additive can also be made in the line between cracking tower and main condenser.
  • the main condenser 30 is conductively connected via a residual gas outlet 39 to a heating system 38 of the process plant, via the residual gas outlet 39, a derivation of the non-condensable portion of the product gas in the heating system 38 of the process plant for thermal utilization in the heating system.
  • the main condenser achieves a very rapid cooling and condensation of the hot product gas (shock cooling) to an average temperature level of 80-200 ° C by applying the process principle quenching.
  • the quench medium used is cooled condensate (product oil).
  • the quenching can be done in two different ways: The hot gas stream is sucked into the liquid recycle stream of cooled condensate, where due to the high turbulence intensive heat exchange and immediate condensation of the product gas occurs. Or alternatively, the quench can be carried out as a packed column, wherein a liquid recycle stream of cooled condensate is trickled over the packing and hot product gas flows in countercurrent from bottom to top and thereby condenses. Due to the large surface of the packing, an intensive heat exchange between cold condensate and hot product gas is achieved, so that the latter condenses immediately.
  • the one can be regenerated while the other is operating normally, with the regeneration of the recycle stream in the packed column to be regenerated being shut off and the hot gas stream coming from the cracking tower being passed through the packed column to be regenerated, thereby causing the bed to fill is heated and deposits are replaced.
  • the regeneration of the packed columns thus happens alternately.
  • the heat exchangers of the main capacitor do not necessarily have to be inside the condenser, for example be arranged as bottom and head cooling, but it is sufficient a heat exchanger in the line of the circulating flow.
  • the heating system is preferably multi-circuit for generating the necessary process heat at this optimized temperature levels.
  • a heat carrier oil or salt or gas can be used for heat transfer with adjustable maximum heating temperature.
  • the efficiency of the heating system is thereby maximized by providing heat recovery to the system using the residual gas to fire the heating system.
  • the method according to the invention does not require the separate gas combustion, gas flare, required in the prior art.
  • the maximum energy utilization is also given because flexible heating of the heating system is possible by means of several optimized temperature levels, namely by the product oil, by the product gas and by the oil-water emulsion, as well as electrically or by a combination of the various aforementioned energy sources. In order to record and monitor the amounts of energy, the resulting temperature differences, the different pressures as well as the different flow rates of the heat transfer medium circuits can be used.
  • FIG. 2 shows a modified registration system over that of FIG. 1 ,
  • the connecting tube of the melting container 7 for connecting the screw conveyor 4 or Stopftechniks is here formed at an acute angle to the melting vessel; otherwise the design is the same.
  • FIG. 3 shows a process plant, which of those of FIGS. 1a . 1B and 1c is very similar and in which the heat transfer and cooling circuits are fully illustrated.
  • the heating system 38 is divided into five heat carrier circuits WT 1 to WT 5.
  • WT 1 is connected via lines to the melting tank 7 and supplies it with heat energy;
  • WT2 is connected to the evaporation vessel 20.
  • WT 3 or WT 4 or WT 5 is connected to the heat removal with the precondensator 29 or with the cooling system 34 or with the residue precooling container 15.
  • FIGS. 4 and 5 show two more examples of different registration systems of a process plant according to the invention.
  • the reflow containers 39 shown here have an upper filler neck 40, through which a feed tube 41 is guided, whose opening is below the liquid level 42 of the liquid melt.
  • the feed tube 41 and the screw plug additionally surrounded by a cooling jacket 43, which is traversed by cooling water.
  • FIG. 6 shows another example of a main capacitor 44 of the process plant according to the invention.
  • the hot gas enters through the opening 45 in the main condenser 44 and flows through packed columns 46, in which there are Rail Energy concept, such as rings made of stainless steel.
  • Liquefied condensate is withdrawn from the sump 54 via a line 47 and fed via a pump 48 two series-connected heat exchangers 49, 50 and further cooled, which are connected to a cooling system 55 with two cooling circuits, cooling circuit I and cooling circuit II. Via a return line 51 to the second heat exchanger 50, cooled condensate is fed back into the main condenser 44 in countercurrent, as in FIG. 6 seen.
  • non-condensed residual gas is either used as combustion gas or it may follow another condenser to be condensed by means of the same existing portions of HCs within the residual gas via a branch line 52 to the second heat exchanger 50 and before the return line 51 is the liquid oil, the target product of the process plant, taken.
  • FIG. 7 is different from the FIG. 3 essentially only in that in the melting vessel 7 and in the evaporation vessel 20 in addition heating coils 56, 57 are installed in order to increase the introduction of heat into the masses.
  • These heating coils 56, 57 are for their supply according to the FIG. 7 connected to own heat transfer medium circuits WT circuit 1 and WT circuit 2 of the heat transfer heating system 58, which either gas-fired oil - for example, with the residual gas from the main capacitors 30 and 44 - or electrically heated.
  • the outer heating jacket can also be omitted.
  • the inventive method or cracking method and the device are industrially applicable in the industries of hygienic workup for the recovery of plastic materials and / or oily residues or plastic waste and / or oily waste.

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  • 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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Processing Of Solid Wastes (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)

Claims (23)

  1. Procédé d'extraction d'hydrocarbures fractionnés à partir de matériaux synthétiques valorisables et/ou de résidus huileux, dans lequel les matériaux synthétiques et/ou les résidus sont triés en fonction de leur sorte et sont comprimés à l'abri de l'air en utilisant un système d'alimentation (1,2,3,4) et la masse comprimée est amenée à un récipient de fusion (7), de préférence en dessous du niveau de liquide, et chauffée là-dedans, de sorte qu'il se produit une séparation entre une première phase liquide, une première phase gazeuse et une part de résidus, caractérisé en ce que
    la phase liquide et la première phase gazeuse sont transportées dans un récipient d'évaporation (20) dans lequel il se produit, sous un nouvel apport de chaleur, une deuxième phase liquide et une deuxième phase gazeuse, la deuxième phase liquide étant conduite à un réchauffeur (23) où elle continue d'être chauffée sous un nouvel apport de chaleur, de sorte qu'il se produit une troisième phase gazeuse, ce après quoi la deuxième phase gazeuse provenant du récipient d'évaporation (20) et la troisième phase gazeuse provenant du réchauffeur (23) sont amenées à une tour de craquage (27) où il se produit un nouveau fractionnement (craquage) des hydrocarbures à longue chaîne en hydrocarbures à courte chaîne et le gaz d'huile produit est conduit ensuite à un condensateur (30) dans lequel le gaz d'huile est condensé en huile liquide, l'huile représentant le produit cible, et le procédé se pratique en utilisant un système de chauffage (38) à plusieurs circuits, afin de générer la chaleur nécessaire au process pour le récipient de fusion (7), le récipient d'évaporation (20) et le réchauffeur (23), l'agent caloporteur utilisé étant de l'huile, ou du sel, ou du gaz.
  2. Procédé selon la revendication 1, caractérisé en ce que pour charger les matériaux synthétiques et/ou les résidus huileux dans le récipient de fusion (7), on utilise à l'intérieur du système d'alimentation une vis de gavage (4) ou un mécanisme de gavage qui comprime les résidus pour l'extraction de l'oxygène et alimente le récipient de fusion en dessous du niveau de liquide de ce dernier.
  3. Procédé selon la revendication 1, caractérisé en ce que la fraction moyenne et la fraction lourde du gaz d'huile ou gaz de craquage chaud est refroidi brusquement par injection d'un condensat froid à un niveau de température moyen et est ce faisant condensé, de sorte que les hydrocarbures à chaînes moyennes et longues se condensent en même temps.
  4. Procédé selon la revendication 3, caractérisé en ce que pour pratiquer le principe du refroidissement brusque, le flux de gaz est ou bien aspiré dans le flux de circulation liquide froid, ou passe par deux lits de garnissage à l'intérieur de colonnes à corps de remplissage qui ponctionnent à contre-courant, le condensat froid étant répandu par ruissellement sur les corps de remplissage.
  5. Procédé selon la revendication 3, caractérisé en ce que du fait de la disposition de deux colonnes à corps de remplissage, l'une d'elles peut être régénérée tandis que l'autre fonctionne en régime normal, le flux de circulation étant coupé pour la régénération dans la colonne à corps de remplissage devant être régénérée et le flux de gaz chaud provenant de la tour de craquage étant conduit à travers la colonne à corps de remplissage devant être régénérée, ce par quoi le garnissage est chauffé dans cette dernière et les dépôts se détachent.
  6. Procédé selon l'une des revendications précédentes, caractérisé en ce que, pour la génération de la chaleur de processus primaire, une part non condensable du gaz d'huile est amenée dans le système de chauffage pour l'alimentation de ce dernier à des fins de valorisation thermique.
  7. Procédé selon l'une des revendications précédentes, caractérisé en ce que l'émulsion huile/eau est amenée dans le système de chauffage (38) pour chauffer de ce dernier à des fins de valorisation thermique.
  8. Procédé selon la revendication 1, caractérisé en ce que
    le condensateur utilisé est un précondensateur (29) et un condensateur principal (30) et la chaleur excédentaire provenant du précondensateur (29), du condensateur principal (30) et du récipient de pré-refroidissement des résidus (15) est amenée au système de chauffage (38), le condensateur principal étant raccordé à un système de condensation à plusieurs circuits.
  9. Procédé selon la revendication 1, caractérisé en ce que
    les matériaux synthétiques et/ou les résidus huileux sont réduits en petits morceaux après le triage et sont le cas échéant séchés avant le process de craquage.
  10. Procédé selon la revendication 1, caractérisé en ce que
    la part de résidus à l'intérieur du récipient de fusion (7) est transportée dans un compartiment de sédimentation (10) en dessous du récipient de fusion, compartiment dans lequel la part de résidus est concentrée et ensuite transférée vers un récipient de pré-refroidissement des résidus (15) dans lequel la part de résidus est refroidie à l'aide d'un agent de refroidissement provenant d'un système de refroidissement (34), à une température de préférence inférieure à 120°C.
  11. Procédé selon l'une des revendications précédentes, caractérisé en ce que
    la part de résidus refroidis est amenée à une unité d'émulsionnement (16) dans laquelle une émulsion huile/eau est produite.
  12. Procédé selon l'une des revendications précédentes, caractérisé en ce que
    entre la tour de craquage (27) et le condensateur principal (30) est disposé un précondensateur (29) qui refroidit le gaz d'huile à un niveau de température élevé pour la récupération d'énergie réduisant ainsi la chute de température entre la tour de craquage (27) et le condensateur principal (30).
  13. Procédé selon l'une des revendications précédentes, caractérisé en ce que
    le condensateur principal (30) et le cas échéant le précondensateur (29) sont raccordés à un système de refroidissement (34) à plusieurs circuits.
  14. Procédé selon la revendication 1, caractérisé en ce que
    le rendement thermique du système de chauffage est maximisé par remise en circulation de la chaleur dans le système en utilisant le gaz résiduel pour chauffer le système de chauffage.
  15. Procédé selon la revendication 1, caractérisé en ce que
    grâce à plusieurs niveaux de température optimisés, un chauffage flexible du système de chauffage est rendu possible, à savoir par l'huile produite, par le gaz produit, ainsi que par l'émulsion huile/eau, tout comme par voie électrique ou par la combinaison des différentes sources d'énergie pré-citées, en assurant ainsi une exploitation maximale de l'énergie.
  16. Dispositif d'extraction d'hydrocarbures fractionnés à partir de matériaux synthétiques et/ou de résidus huileux dans lequel les matériaux synthétiques et/ou les résidus sont triés en fonction de leur sorte, comportant un système d'alimentation (1,2,3,4) pour la compression à l'abri de l'air des matériaux synthétiques et/ou des résidus huileux, ainsi qu'un récipient de fusion (7) raccordé en aval pour le chauffage et la fusion de la masse comprimée afin de générer une première phase liquide, une première phase gazeuse et une part de résidus, caractérisé en ce que
    en aval du récipient de fusion (7) est disposé un récipient d'évaporation (20) pour générer sous un nouvel apport de chaleur une deuxième phase liquide et une deuxième phase gazeuse, récipient d'évaporation auquel succède, pour démarrer et pursuivre la chauffe de la deuxième phase liquide, un réchauffeur (23) pour la production d'une troisième phase gazeuse, et une tour de craquage (27) est raccordée au récipient d'évaporation (20) et au réchauffeur (23) pour le fractionnement (craquage) des hydrocarbures à longue chaîne en hydrocarbures à courte chaîne, tour de craquage à laquelle est raccordé un condensateur (30) pour la condensation du gaz d'huile en une huile liquide qui est le produit cible, ledit dispositif présentant un système de chauffage (38) à plusieurs circuits pour générer la chaleur nécessaire au process pour le récipient de fusion (7), le récipient d'évaporation (20) et le réchauffeur (23) à des niveaux de température optimisés à cet effet, avec de l'huile, du sel ou du gaz comme agent caloporteur.
  17. Dispositif selon la revendication 16, caractérisé en ce que pour charger les matériaux synthétiques et/ou les résidus huileux dans le récipient de fusion (7), une vis de gavage (4) ou un mécanisme de gavage pour la compression du matériau synthétique ou des résidus huileux est disposée à l'intérieur du système d'alimentation, en amont de laquelle se trouve si besoin est un récipient de transfert (3) sphérique pour le transfert dans la vis de gavage (4) ou le mécanisme de gavage.
  18. Dispositif selon la revendication 17, caractérisé en ce que la sortie de la vis de gavage (4) ou du mécanisme de gavage débouche à l'intérieur du récipient de fusion (7) en dessous du niveau de liquide de la masse fondue.
  19. Dispositif selon la revendication 16, caractérisé en ce que au-dessous du récipient de fusion (7) est disposé un compartiment de sédimentation (10) pour recueillir la part de résidus.
  20. Dispositif selon la revendication 19, caractérisé en ce que un récipient de pré-refroidissement des résidus (15) ainsi qu'une unité d'émulsionnement (16) qui lui est agencée, est agencé au compartiment de sédimentation (10) pour la production d'une émulsion huile/eau à partir de la part de résidus.
  21. Dispositif selon la revendication 16, caractérisé en ce que
    le condensateur est constitué par un condensateur principal (30) et un précondensateur (29) et le précondensateur (29) est disposé entre la tour de craquage (27) et le condensateur principal (30) pour le pré-refroidissement du gaz d'huile.
  22. Dispositif selon la revendication 16, caractérisé en ce que
    un système de refroidissement (34) à plusieurs circuits est raccordé au condensateur principal (30).
  23. Dispositif selon la revendication 16, caractérisé en ce que
    le récipient de fusion (7) et le récipient d'évaporation (20), ainsi que, le cas échéant, le récipient de post-chauffage (23) présentent une enveloppe chauffane extérieure (8,21) et/ou des serpentins (56,57), ledites enveloppes chauffantes (8,21) pouvant être chauffées via le système de chauffage commun (38) des agents caloporteurs.
EP05701145A 2004-01-24 2005-01-24 Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux Expired - Lifetime EP1745115B1 (fr)

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PL05701145T PL1745115T3 (pl) 2004-01-24 2005-01-24 Sposób i urządzenie do odzyskiwania frakcjonowanych węglowodorów z surowców wtórnych zawierających tworzywa sztuczne i/lub z części odpadowych zawierających olej
EP05701145A EP1745115B1 (fr) 2004-01-24 2005-01-24 Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux
SI200531238T SI1745115T1 (sl) 2004-01-24 2005-01-24 Naprava in postopek za pridobivanje frakcioniranih oglikovodikov iz recikliranih plastičnih frakcij in/ali olje vsebujočih ostankov

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DE102004003667A DE102004003667A1 (de) 2004-01-24 2004-01-24 Verfahren zum Gewinnen von fraktionierten Kohlenwasserstoffen aus Kunststoffwertstoffen und/oder ölhaltigen Reststoffen sowie Vorrichtung hierzu
EP2005000504 2005-01-20
PCT/EP2005/000661 WO2005071043A1 (fr) 2004-01-24 2005-01-24 Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux
EP05701145A EP1745115B1 (fr) 2004-01-24 2005-01-24 Dispositif et procede d'extraction d'hydrocarbures fractionnes a partir de materiaux synthetiques et/ou de residus huileux

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EP1745115B1 true EP1745115B1 (fr) 2010-12-15

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PT (1) PT1745115E (fr)
SI (1) SI1745115T1 (fr)
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WO2014161767A2 (fr) 2013-04-04 2014-10-09 Achim Methling Josef Ranftl Gbr Procédé de décomposition de polymères synthétiques et dispositif permettant la mise en œuvre dudit procédé

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DE102005059856A1 (de) 2005-12-15 2007-06-28 Nill-Tech Gmbh Förder- und Schleusensystem
EP2061859A2 (fr) * 2006-08-25 2009-05-27 Granit Systems S.A. Procédé et dispositif pour le traitement de déchets à teneur en matière plastique
FR2931482A1 (fr) * 2008-05-23 2009-11-27 Sylvie Lestrade Procede de craquage en continu de dechets de polyolefines
CH708681A1 (de) * 2013-10-14 2015-04-15 Gerold Weser Dr Verfahren und Anlage zum Aufbereiten von Kunststoffwertstoffen.
US20180010050A1 (en) 2015-01-19 2018-01-11 Bluealp Innovations B.V. Method and system for transferring plastic waste into a fuel having properties of diesel/heating oil
DE102019001696B4 (de) 2019-03-11 2026-05-07 Olaf Heimbürge Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien
DE102019001702A1 (de) 2019-03-11 2020-09-17 Olaf Heimbürge Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien
DE102019001697A1 (de) 2019-03-11 2020-09-17 Olaf Heimbürge Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien
WO2020225219A1 (fr) * 2019-05-03 2020-11-12 Biofabrik White Refinery Gmbh Procédé et dispositif de valorisation de déchets ou résidus plastiques contenant de préférence des polyoléfines
CN111111575A (zh) * 2019-12-27 2020-05-08 北京英惠尔生物技术有限公司 一种提高Vc酯反应釜效率的方法及其简易冷水供给系统
DE102020004964A1 (de) 2020-08-14 2022-02-17 Timon Kasielke Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien
NO348031B1 (en) 2021-12-31 2024-06-24 Inrigo As Method and device for pyrolysis-based production of hydrocarbon oils based on plastic containing raw material
DE102022116573B4 (de) 2022-07-04 2026-04-30 adeamus GmbH Reaktoreneinheit zur Kunststoffthermolyse, Kunststoffthermolyseanlage sowie Verfahren zu deren Betrieb

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JPH0834978A (ja) 1994-07-21 1996-02-06 Kubota Corp 低沸点炭化水素油の製造方法および製造装置
CN2435146Y (zh) 2000-06-01 2001-06-20 北京乐意环保技术有限公司 连续大规模工业化生产的反应釜
CN1127554C (zh) 2000-07-12 2003-11-12 北京乐意环保技术有限公司 利用废塑料生产汽油、柴油和液化气的工艺方法及设备

Cited By (3)

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Publication number Priority date Publication date Assignee Title
WO2014161767A2 (fr) 2013-04-04 2014-10-09 Achim Methling Josef Ranftl Gbr Procédé de décomposition de polymères synthétiques et dispositif permettant la mise en œuvre dudit procédé
DE102013205996A1 (de) 2013-04-04 2014-10-09 Achim Methling Josef Ranftl GbR (vertretungsberechtigte Gesellschafter: Achim Methling, A-1110 Wien, Josef Ranftl, 82256 Fürstenfeldbruck) Verfahren zum Abbau von synthetischen Polymeren und eine Vorrichtung zu dessen Durchführung
US10494572B2 (en) 2013-04-04 2019-12-03 Achim Methling Joesef Ranftl GbR Method for the degrading of synthetic polymers and device for carrying out said method

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PL1745115T3 (pl) 2011-05-31
CA2558347A1 (fr) 2005-08-04
EP1745115A1 (fr) 2007-01-24
ATE491771T1 (de) 2011-01-15
CA2558347C (fr) 2013-07-30
SI1745115T1 (sl) 2011-05-31
DK1745115T3 (da) 2011-04-04
WO2005071043A1 (fr) 2005-08-04
DE502005010684D1 (de) 2011-01-27
PT1745115E (pt) 2011-03-23

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