EP3247775A1 - Procédé et installation pour la transformation des déchets de matières plastiques en un combustible ayant les propriétés du diesel/du fioul - Google Patents

Procédé et installation pour la transformation des déchets de matières plastiques en un combustible ayant les propriétés du diesel/du fioul

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Publication number
EP3247775A1
EP3247775A1 EP15707270.3A EP15707270A EP3247775A1 EP 3247775 A1 EP3247775 A1 EP 3247775A1 EP 15707270 A EP15707270 A EP 15707270A EP 3247775 A1 EP3247775 A1 EP 3247775A1
Authority
EP
European Patent Office
Prior art keywords
cracking reactor
heating device
cracking
plastic materials
plastic
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.)
Granted
Application number
EP15707270.3A
Other languages
German (de)
English (en)
Other versions
EP3247775B1 (fr
Inventor
Gerold Weser
Teunis Christiaan VAN DER REE
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.)
Bluealp Innovations BV
Original Assignee
Bluealp Innovations BV
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 Bluealp Innovations BV filed Critical Bluealp Innovations BV
Priority to PL15707270T priority Critical patent/PL3247775T3/pl
Publication of EP3247775A1 publication Critical patent/EP3247775A1/fr
Application granted granted Critical
Publication of EP3247775B1 publication Critical patent/EP3247775B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • C10G7/00—Distillation of hydrocarbon oils
    • 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
    • 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
    • C10G9/40—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by indirect contact with preheated fluid other than hot combustion gases
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4081—Recycling aspects
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil

Definitions

  • the invention relates to a method and a plant for processing plastic waste, in particular plastic waste based on (i) the basis of polyolefins and / or (ii) organic oil-based fluids, by converting such waste plastics into hydrocarbons with 1 C atom ( Methane) to hydrocarbons with more than 22 C atoms.
  • WO 2005/071043 A1 discloses a processing method in which plastic waste is processed into oil.
  • WO 2008/022790 describes a process for the treatment of plastic-containing wastes and organic liquids based on crude oil, cooking oil, fats or the like, with the following steps:
  • the gas phase present after the cracking zone of the reactor is fed, for example, to a distillation device which is operated in such a way that long-chain polymers condense and are returned to the cracking zone of the reactor.
  • a distillation device which is operated in such a way that long-chain polymers condense and are returned to the cracking zone of the reactor.
  • Relatively short chain, after the distillation device and a subsequent condenser are gaseous hydrocarbons (C1-C4) can be energetically ge ⁇ uses as fuel.
  • the aim of the present invention was to provide an improved process for the treatment of plastic waste (hereinafter also referred to as plastic materials) and a plant for carrying out this process.
  • the improvements include reduction of slag formation and / or more flexible product control and / or optimized product purity.
  • This object has been achieved by providing a process for recovering hydrocarbons from preferably polyolefin waste by means of purely thermolytic cracking in a cracking reactor, preceded by a first heating device and a second heating device, without the use of catalysts
  • the molten plastics materials together with hydrocarbonaceous vapors already formed from the second heating device, are fed to the cracking reactor in which the molten plastic materials are further cracked (cracked) at about 400 ° C, the gaseous hydrocarbons being fed to a partial condenser condense long-chain hydrocarbons and be recycled to the cracking reactor, preferably a condenser, which is preceded by a packed column,
  • (B4) emerge short-chain hydrocarbons from the cracking reactor and fed to a distillation apparatus in which they are decomposed into a gaseous and a liquid fraction and from which the liquid fraction is withdrawn as product diesel, and passed the gas ⁇ shaped fraction through a cooler in which it is split into low boilers (C5-C7), which are gela ⁇ siege, and in the non-condensed gases (C1-C4), which are preferably used as fuel for heating the thermal oil,
  • the withdrawn liquids may be purified in special adsorption and / or filtration systems prior to transfer to storage tanks and any interfering components (e.g., organic acids) that may have been formed removed.
  • interfering components e.g., organic acids
  • a feed system which is preferred for the system according to the invention but which can also be used together with other systems comprises the feeding of the plastic waste to the first heating device via a delivery system in which
  • These acidic exhaust gases are preferably one
  • the compression in the first stage (a2) is suitably carried out by means of a screw compressor and the second stage (a3) by means of an extruder, wherein the compressor as well as the extruder should be heatable.
  • a preferred heating medium is thermal oil.
  • ge ⁇ is enough, via a system of at least two and preferably two buffer tanks, which are preferably supplied with stick ⁇ material and / or rinsed, and of which the one is filled while the other is being emptied, and both of which are connected to a weighing system which permits metered filling of the plastic waste introduction system.
  • the recycle stream mentioned in (b5) above is obtained by pumping plastic melted down from the cracking reactor by means of a high-temperature pump, high-energy but non-gaseous pitch and tar-like substances, and carbon excess resulting from the cracking of polymers, and a separator System is supplied.
  • separator system is preferably a cyclone separator, optionally and preferably connected to a sedimentation (settling).
  • the gaseous hydrocarbons from the cracking reactor are preferably fed to the partial condenser via a packed column, so that the route for the separation of the still insufficiently cracked hydrocarbons (usually more than 22 C atoms) becomes longer.
  • This has the positive effect that the partial condenser can be operated at a higher temperature, without a significant proportion of excessively long hydrocarbons can leave the cracking reactor, or that the temperature in the partial condenser must not be set so low that a significant An ⁇ part of Hydrocarbons with 22 or fewer carbon atoms in the cracking reactor is recycled and further cracked there, which would reduce the proportion of longer-chain hydrocarbons in the product diesel.
  • the gases / vapors are decomposed into a gaseous and a liquid fraction.
  • the liquid fraction is withdrawn at the intermediate bottom as product diesel and the gaseous fraction at the top of the distillation column.
  • the gaseous fraction is cooled so that low-boiling components (C5-C7 / C8) condense and can be withdrawn as a liquid fraction.
  • the Uncondensed gases (C1-C4) are preferably used as fuel for heating the thermal oil.
  • the lengths of the hydrocarbons in the individual fractions can be well controlled, on the one hand by the temperature of the partial condenser, then by the length of the distillation column and the temperature in this and in the cooler.
  • the system can be operated continuously.
  • Preferred first and second heaters in the context of this invention are tube heat exchangers surrounded by thermal oil.
  • the temperature of the partial condenser is adjustable, for example in a range from 150 ° C. to 350 ° C., for chain lengths of a maximum of 22 C atoms, preferably to 300 ° C.
  • Crack reactor emerging gas takes place, preferably by means of countercurrent distillation, in which a portion of the Pro ⁇ dukt diesel recycled above the sampling point in the distillation column, in particular sprayed.
  • the temperature in this column can be varied or adjusted, for example in such a way that, depending on the setting, hydrocarbons having 8-9 to 20-22 C atoms are withdrawn at the intermediate bottom as product diesel become.
  • the type of hydrocarbon mixture of the low boilers or noncondensed gases can also be varied or determined via the temperature setting during cooling.
  • the product diesel and / or the low boilers are withdrawn and stored for later use, while the uncondensed gases (Cl-C4) are used directly as fuel for heating the thermal oil.
  • the uncondensed gases Cl-C4
  • An apparatus for treating plastic-containing wastes and organic liquids based on crude oil which is particularly suitable for carrying out the method described above, comprises a first heating device, a second heating device, a cracking reactor, and a recirculation flow line, which of a Lower region of the cracking reactor via a separator system in the feed line of the molten plastic waste from the first heater into the second heater leads.
  • the first and the second heating device are each a tube heat exchanger flushed with thermal oil.
  • the first and / or the second heating device may also consist of a plurality of series-connected or parallel-connected heating devices, but as a whole have the characteristics of the first and second heating devices.
  • the first and second heaters and the cracking reactor have independently controllable heaters.
  • Preferred heaters are heat exchangers, which are designed as a tube heat exchanger, wherein the tubes are filled with the melt and are lapped by thermal oil. This ensures the largest possible heat transfer surface, which offers the advantage that it is possible to work with a small temperature difference (usually at most 20 ° C.) between the desired temperature in the melt and the temperature of the heat transfer medium, the thermal oil.
  • the recycle stream comprises carbon-rich particles as well as non-melting contaminants that accumulate in the bottom of the cracking reactor.
  • This recycle stream is pumped out of the cracking reactor continuously and passed through a Separator- system in which particles are deposited, whereupon the residual stream is supplied to the plastic melt before the second heater again.
  • a preferred separator system comprises a cyclone separator.
  • This cyclone separator comprises a cylindrical part with centrally arranged pipe.
  • the separator system in addition to the cyclone separator, has a sedimentation tank arranged outside the recycle stream line but connected to the cyclone separator, which, however, may optionally be connected to the recycle stream line via the heater side by-pass and preferably connected.
  • the cracking reactor is equipped with a partial condenser which has a cooling / heating device which is designed in such a way that a defined temperature can be set in the partial condenser.
  • a ⁇ be ferred cooler / heater comprises, as heat transfer medium in a heat transfer medium, which can be brought to a temperature by means of a temperature control that is required to set the required temperature inside the partial condenser.
  • a preferred heat transfer medium is a thermal oil.
  • the partial condenser in particular in combination with a packed column, has the effect that only-or at least predominantly-molecules of defined chain length emerge from the cracking reactor.
  • a distillation device Connected downstream of the cracking reactor or the partial condenser is a distillation device which can be operated in such a way that long-chain molecules condense (product-diesel) and escape from the short-chain molecules as gas phase.
  • This gas phase can be partially condensed in a condenser downstream of the distillation column (low boilers and non-condensed gases).
  • the distillation device comprises a reboiler and a distillation column, which preferably has a region designed as a packed column and also preferably an intermediate bottom, to which the liquid fraction, e.g. condensed product diesel, is withdrawn. A portion of this liquid fraction, this product diesel, can be recycled to optimize the temperature above the sampling point in the distillation column, which serves to better separation of the hydrocarbon fractions.
  • a reboiler and a distillation column which preferably has a region designed as a packed column and also preferably an intermediate bottom, to which the liquid fraction, e.g. condensed product diesel, is withdrawn.
  • the liquid fraction e.g. condensed product diesel
  • the cooler intended for further separation of the gas phase into low boilers and noncondensed gases has a heating / cooling device with which a defined temperature in the cooler - and thus the composition of the hydrocarbon fractions - can be set.
  • adsorption and / or filter units for adsorbing impurities from the light liquid and / or the product diesel can be provided.
  • These adsorption or filter units can comprise a plurality of adsorbers or filters, which alternately can be switched on or off for adsorption or regeneration.
  • Purified and presorted polyolefin-rich wastes are stored in a bunker.
  • the presorting can be carried out by means of common methods.
  • the plastics e.g. PVC, PET by their IR spectra or other features recognized and foreign substances such. removed by means of a punctually placeable air flow.
  • the plastic materials may still contain small amounts of impurities, such as e.g. chlorine- and / or sulfur-containing compounds, rubber, metals, sand, etc., which are removed later in the process.
  • the plastic materials of the plant are preferably supplied by means of the injection system described below.
  • This system has the advantage that it is possible to dispense with a permanent flushing with inert gas (nitrogen) during the filling of the melting zones and the cracking reactor, since the introduction system filled with at least partially molten plastic material constitutes an airtight seal .
  • the system can also be filled with another injection system.
  • the exact and reproducible dosage in the inventive delivery system is done with the help of two buffer containers, which are weighed. These buffer containers may optionally be charged or purged with nitrogen. From the respective buffer container, the filling of the system is done by means of a mechanical injection system. This introduction system itself is divided into at least two zones that perform different tasks.
  • the plastic mixture to be processed is fed continuously to the introduction system from the buffer containers, which are alternately filled or emptied, first into a compressor in which it is homogenized and heated substantially by friction. If necessary, the heating can be supported by additional heating, in particular on the outer wall of the compressor, which can be heated, for example with thermal oil. In the compressor, the material should be heated to a temperature of 120 to 150 ° C., So that steam evaporated in this stage and, in particular by applying a slight vacuum, can be sucked off.
  • the material is conveyed to a preferably heated with thermal oil extruder and heated there to about 250 - 300 ° C. At these temperatures, sulfur-containing and chlorine-containing plastic components are destroyed. HCl and H2S are withdrawn from the extruder with a vacuum pump.
  • the acidic pollutants are preferably neutralized with sodium hydroxide solution as part of a gas scrubber and disposed of. At max.
  • this technique also has the advantage that during filling of the heaters (Schmelzzo ⁇ NEN) and the cracking reactor to a permanent purging with inert gas (nitrogen) can be dispensed with, since the filling system filled with already partially molten plastic or the extruder forms an airtight seal.
  • the extruder compresses and conveys the plastic recyclable materials in a first heating device, in which the plastic ⁇ valuable materials flow through the pipes which are flushed with thermal oil as a heating medium a first tube heat exchanger.
  • the entire heating surface of Tubes is chosen so large that with the smallest possible temperature difference between heating medium and
  • Plastic recyclables can be worked. This minimizes the deposition of coke by cracking processes on the tube walls.
  • An added benefit of tube heat exchangers is that they are easy to clean. In order to completely melt the plastics, they are heated to approx. 380 ° C.
  • the output of the first heater, the first heat exchanger, is connected to a recirculation flow line.
  • recycle stream which was passed from the cracking reactor via a cyclone separator acting as a slag discharge system is added to the plastic melt from the first heater.
  • the mixed stream flows into a second heater, a second tube heat exchanger in which the plastic melt is heated to 400 ° C. From this second heat exchanger, the molten plastic materials, together with the cracking gases already produced at this temperature, reach the cracking reactor. In this reactor at about 400 ° C, the plastic molecules purely thermolytically, ie without the use of catalysts, decomposed into a substantially gaseous hydrocarbon mixture (cracked).
  • the heat transfer in the cracking reactor is preferably carried out to avoid pyrolytic decomposition reactions not or not only by the reactor wall (boiler principle).
  • a suitable heating means are a plurality of tube heat exchangers arranged within the crack reactor or bundles of heating tubes which are filled with heat transfer medium, in particular thermal oil, or through which heat transfer medium flows.
  • the tubular heat exchanger or heating tubes can be easily arranged within the cracking reactor so that even in their presence can be dispensed with a conventional, centrally arranged agitator, i. that due to the continuously pumped and recirculated return flow sufficient mixing of the melt is achieved.
  • the heat transfer medium which is used for heating the plastic melt in the cracking reactor, be maintained at a relatively low temperature of preferably 405 ° C to a maximum of 420 ° C.
  • a high temperature liquid pump At the bottom of the cracking reactor is an outlet leading to a high temperature liquid pump.
  • This pump is able to pump fluids at a temperature of 400 ° C and is not affected by possible abrasive components in the plastic melt.
  • High-energy but not in the gaseous state passing pitch and tar-like substances as well as the cracking of polymers resulting carbon excess are pumped through a Separator ⁇ system, in particular a cylindrical cyclone separator with associated sedimentation.
  • the tangenti ⁇ ale velocity of the fluid is increased due to the dimensions of the cyclone separator.
  • the heavier parts flow down the cyclone separator, preferably into a settling tank, as these still contain larger quantities of molten plastic.
  • the flow velocity in the sedimentation tank is very low, so that an additional separation between see parts high and. low density, or solid particles and molten plastic can be achieved.
  • a obtained in the sedimentation tank phase which is rich in molten plastic can be fed back via the bypass in the recycle stream line from ⁇ divorced phase of higher density, which comprises the solids, is removed and can be used as high-energy fuel.
  • This partial condenser is preferably ak ⁇ tiv heatable and / or coolable, in particular, be cooled and also preferably adjusted so that hydrocarbon ⁇ substances which do not correspond to the desired character of the product, such as diesel / fuel oil character, condense and flow back to the cracking reactor where they further are cracks overall until they are shorter than, for example, hydrocarbons with a maximum of 22 carbon atoms and the capacitor passie ⁇ ren can.
  • this technology it is possible to largely or even completely avoid the formation of long-chain hydrocarbons (wax / paraffins).
  • the lower boiling part (for example, less than C20 or C22) is not retained by the condenser and sent from it to a quench / distillation apparatus which separates the low boilers and gases (C1-C7 / C8) from the middle distillate (C8 / C8). C9 - C20 / C22).
  • This quench / distillation device comprises a
  • Reboiler evaporator
  • a distillation column evaporator
  • the bottom temperature in the quench / Destil- lations is preferably controlled by an evaporation ⁇ fer, a so-called reboiler, which up to 400 ° C can be heated. Hydrocarbons containing more than 22 C atoms are accumulated in the reboiler and pumped back from the reboiler to the cracking reactor.
  • the distillation column is at least in part ⁇ be designed as a packed column.
  • a bottom is preferably provided, in which at least a portion of the liquid hydrocarbons is collected.
  • These hydrocarbon liquids ⁇ the withdrawn and - preferably in a heat exchanger - cooled.
  • a portion of the cooled liquid is returned as a recycle stream (reflux) for temperature control at the top of the distillation column, preferably after addition of a free radical inhibitor, which acts as a stabilizer ⁇ gate and prevents the formation of paraffins in the product diesel.
  • the product diesel taken from the distillation step and preferably (as a result of the reflux added with such an inhibitor) containing a free radical inhibitor is preferably finally cooled in a further heat exchanger and optionally filtered by adsorption and / or filtration means and edited.
  • an antioxidant is preferably added to prevent the degradation of the product diesel.
  • the vapor exiting the upper part of the distillation means comprises the lower boiling components (gasoline-type hydrocarbons, for example Cl to C8).
  • This steam is cooled in an actively coolable condenser.
  • the condensate, a low boiler (e.g., C5-C8), is discharged into a reservoir.
  • the uncondensed at room temperature part, Cl to C4 or methane to butane - optionally after purification, e.g. by adsorption / desorption - either spent by a compressor in a reservoir, from which it can be used at a later time in a burner for heating the heat transfer medium, or it is fed directly to such a burner.
  • the partial condenser in particular with an upstream filler column, prevents hydrocarbons exceeding a desired length from entering the distillation system.
  • the distillation apparatus allows a very accurate separation of the hydrocarbon fractions into a liquid fraction, e.g. Product diesel, and a gaseous fraction, e.g. Low boilers / noncondensed gases.
  • a liquid fraction e.g. Product diesel
  • a gaseous fraction e.g. Low boilers / noncondensed gases.
  • the filling of the compressor 1 is preferably carried out by means of two buffer systems (not shown), which are charged or purged with nitrogen, and which can be weighed by the amount introduced
  • the system can be operated continuously, as one buffer system is filled while the other buffer system is being emptied.
  • the plastic materials are homogenized, compressed and heated substantially by friction, if necessary supported by a thermal oil heating, preferably in the outer wall of the compressor, in particular a screw compressor.
  • the heating in this compressor to 120-150 ° C, allows the removal of most of the water contained. Water removal can be by applying a vacuum un ⁇ terology and is preferably assisted by applying ei ⁇ nes vacuum.
  • the dried, compacted plastic materials are conveyed into an extruder 2, preferably heated with thermal oil, and further heated to about 250-300 ° C., so that at least part of the plastics material is melted.
  • an extruder 2 preferably heated with thermal oil, and further heated to about 250-300 ° C., so that at least part of the plastics material is melted.
  • a vacuum pump sucks the noxious gases, in particular the acidic gases HCl and H2S.
  • a technique has the additional advantage that during the loading ⁇ filling of the melting zones of the cracking reactor and to Permanent flushing with inert gas (nitrogen) can be dispensed with, since the system filled with molten plastic is an airtight seal.
  • the at least partially molten plastic enters a first heating device, a first tubular heat exchanger, 3 in which the plastic materials are heated to a temperature of 300 ° C to 380 ° C, so that all plastic is molten ,
  • This recirculation flow is taken from the cracking reactor 5 by means of the high-temperature pump 7 and conducted in the recirculation flow line 10 via the cyclone separator 8 into the stream of plastic materials emerging from the heat exchanger 3.
  • the liquid phase formed from the melted KunststoffStoffwertstoffen derived from heat exchanger 3 and the recycle stream, in a second Schuvorrich- device, a second heat exchanger, 4 at a temperature of 380 ° C to 400 ° C - if still necessary - further melted, already can use a thermal cracking.
  • the molten plastic recyclable materials, to ⁇ together with already-formed hydrocarbon-containing vapors are then the cracking reactor 5, respectively ⁇ leads, which can optionally be heated by means of heat exchanger 6 and in which the molten hydrocarbons split at about 400 ° C (cracked) are.
  • the entire plastic melt which is located in the cracking reactor 5 and in the second heat exchanger 4, is permanently circulated by means of the high-temperature pump 7.
  • the gaseous hydrocarbons leaving the cracking reactor are fed to a filler column with subsequent partial condenser 10, in which long-chain hydrocarbons (longer than, for example, C22) condense, are returned to the cracking reactor 5 and cracked until they have a chain length of, depending on the setting, a maximum of C20 to C22 have.
  • the gases which do not condense in the usually unheated packed column 12 or in the partial condenser 11 are fed to a distillation device 13, 14, 15, 16 in which they are decomposed into a gaseous and a liquid fraction and from which the liquid fraction as middle distillate, the gaseous fraction as low boilers and uncondensed gases from the distillation unit
  • the distillation device 13, 14, 15, 16 comprises a reboiler 13 and a distillation column 14.
  • the distillation column 14 preferably has a region designed as a packed column 15 and, where appropriate, within this region containing filler or preferably above this range a Zwi ⁇ ash floor 16, on the liquid fraction (product diesel) is collected and can be derived.
  • the product diesel derived from the distillation device 13, 14, 15, 16 is preferably cooled off by means of a heat exchanger, and part of this cooled product diesel can be returned to the distillation device via recycle stream line 17 to set optimum temperature conditions.
  • the return, the reflux takes place at the top of the distillation device, but in any case above the intermediate bottom 16, the removal point of the product diesel.
  • Diesel a radical inhibitor term paraffin is preferably added, the langket the origin 'etc. prevented. This ⁇ addition is suitably carried out after the heat exchanger and after the branching of the reflux stream.
  • the withdrawn liquid may be purified in ad sorption and / or filter systems and the alternative ⁇ ell interfering components (eg, organic acids) are removed before the hydrocarbons are converted into a laser gertank.
  • ⁇ ell interfering components eg, organic acids
  • At least one stabilizer Before storing the product diesel, it is preferable to add at least one stabilizer to it.
  • Radical inhibitors as well as stabilizers and antioxidants are familiar to the person skilled in the art.
  • a suitable radical inhibitor is e.g. BHT (butylhydroxitoluene)
  • suitable stabilizers are e.g. strong basic amines
  • a suitable antioxidant is e.g. Phenyldi- min.

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  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé d'extraction d'hydrocarbures à partir de déchets de matières plastiques, en particulier de déchets riches en polyoléfine, au moyen d'un craquage purement thermolytique sans utilisation de catalyseurs, qui comprend la fusion des déchets de matières plastiques dans deux dispositifs de chauffage (3) et (4), les déchets de matières plastiques fondues provenant du dispositif de chauffage (3) étant mélangés à un flux de recirculation provenant du réacteur de craquage (5) et épuré dans un système séparateur (8, 9). Le flux de matières plastiques mélangé continue à être chauffé dans le deuxième dispositif de chauffage (4), d'où il est conduit dans le réacteur de craquage (5) pour procéder au craquage des matières plastiques et à leur séparation en diesel et en composants à bas point d'ébullition au moyen d'une distillation consécutive. Un système d'apport spécifique permet la séparation préalable de l'eau et des gaz acides ainsi que l'économie de gaz inerte. L'invention concerne également une installation permettant la réalisation du procédé.
EP15707270.3A 2015-01-19 2015-01-19 Procédé et installation pour la transformation des déchets de matières plastiques en un combustible ayant les propriétés du diesel/du fioul Active EP3247775B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL15707270T PL3247775T3 (pl) 2015-01-19 2015-01-19 Sposób i instalacja do przetwarzania odpadów zawierających tworzywa sztuczne w paliwa o właściwościach paliw do silników wysokoprężnych/oleju opałowego

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2015/000081 WO2016116114A1 (fr) 2015-01-19 2015-01-19 Procédé et installation pour la transformation des déchets de matières plastiques en un combustible ayant les propriétés du diesel/du fioul

Publications (2)

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EP3247775A1 true EP3247775A1 (fr) 2017-11-29
EP3247775B1 EP3247775B1 (fr) 2020-07-08

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US (2) US20180010050A1 (fr)
EP (1) EP3247775B1 (fr)
ES (1) ES2822597T3 (fr)
PL (1) PL3247775T3 (fr)
WO (1) WO2016116114A1 (fr)

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US20230059944A1 (en) 2023-02-23
WO2016116114A8 (fr) 2017-03-16
PL3247775T3 (pl) 2020-12-14
US12448573B2 (en) 2025-10-21
EP3247775B1 (fr) 2020-07-08
US20180010050A1 (en) 2018-01-11
WO2016116114A1 (fr) 2016-07-28
ES2822597T3 (es) 2021-05-04

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