EP2061859A2 - Procédé et dispositif pour le traitement de déchets à teneur en matière plastique - Google Patents

Procédé et dispositif pour le traitement de déchets à teneur en matière plastique

Info

Publication number
EP2061859A2
EP2061859A2 EP07801847A EP07801847A EP2061859A2 EP 2061859 A2 EP2061859 A2 EP 2061859A2 EP 07801847 A EP07801847 A EP 07801847A EP 07801847 A EP07801847 A EP 07801847A EP 2061859 A2 EP2061859 A2 EP 2061859A2
Authority
EP
European Patent Office
Prior art keywords
reactor
zone
cooling
cracking
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP07801847A
Other languages
German (de)
English (en)
Inventor
Christian Widmer
Rudolf Hartmann
Gerold Weser
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.)
Grt Operations SA
Original Assignee
Granit Systems S A
Granit Systems SA
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 Granit Systems S A, Granit Systems SA filed Critical Granit Systems S A
Publication of EP2061859A2 publication Critical patent/EP2061859A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to a method and an apparatus for treating plastic-containing wastes and organic liquids based on petroleum, cooking oil, fats or the like.
  • the sorted plastic materials are first compressed under exclusion of air and fed to a melting vessel. In this, a separation into a first liquid phase, a first gas phase and a residue fraction takes place.
  • the liquid phase and the first gas phase are fed to an evaporator in which a second liquid phase and a second gas phase are formed.
  • the second liquid phase is further heated in a reheater.
  • the resulting third gas phase is fed together with the second gas phase from the evaporation vessel to a cracking tower in which long-chain hydrocarbons are cracked.
  • the resulting gas is then condensed in a condenser to give light weight.
  • the invention has for its object to provide a method and an apparatus with which plastic-containing waste can be treated with minimal device complexity.
  • the melting, evaporation and cracking takes place in a single common reactor, which is subdivided into a melting and a cracking zone or in two reactors connected in series, so that the technical equipment expense compared to the solution described above is considerably reduced.
  • the gas phase present after the cracking zone of the reactor is fed, for example, to a distillation column 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 column and an adjoining cooler gaseous hydrocarbons present can be used as fuel energetically.
  • the inventive method can be used particularly effectively realized, when the temperature is as low as possible in the melting zone - about 250 0 C to a maximum of 350 0 C - and in the cracking zone at about 420 ° C to 450 0 C.
  • condensation still existing in the light liquid impurities can be removed by a separate treatment step, for example by absorption from the light liquid.
  • the reactor with the melting zone and / or the cracking zone is provided with a conveyor through which the melt is conveyed continuously from the material entry path.
  • This conveyor may for example be formed by a screw conveyor, which is assigned to one of the said zones.
  • the mixture of substances to be treated is fed symmetrically to the reactor via at least two material entries. It is particularly preferred if this material is compacted before being fed to the reactor.
  • the reactor is preferably designed as a horizontal container.
  • a portion of the liquid product is passed after cooling and quenching as circulating cooling liquid over a cooler and used as a quench liquid in the cooler for cooling and condensing the gas stream.
  • the heating of the melt in the melting or cracking zone is preferably carried out in each case by guided in the interior of the reactor tubes, so that practically a tube heat exchanger is formed.
  • the number of tubes or, more precisely, their heat exchange surface is adapted to the heat output to be applied.
  • a single reactor with a melting and a cracking zone can be provided.
  • two reactors can be connected in series.
  • To heat the suspension heating tubes are provided in the reactor.
  • the Schuffeneintrag and the distribution of the heating means on the individual tubes is the front side at one end of the reactor.
  • the outlet distributor and the Schuffenaustrag are then located on the opposite side of the reactor.
  • the heating tubes together with the associated distributors and the spiral, via which incrustations on the inner circumferential wall of the relevant reactor can be removed, rotate together.
  • the only reactor with melting and cracking zone or the two reactors connected in series is in each case assigned a heat exchanger in which the suspension or melt can be heated.
  • these heat exchangers are designed as a tube heat exchanger, wherein in a flowed through by the suspension / melt inner tube, a spiral is arranged, which rotates together with the suspension and substantially improves the heat exchange, so that the heat exchanger can be built shorter than conventional constructions , - A -
  • the Antriebsag regate the pumps and conveyors are exposed to a special wear.
  • magnetic coupling motors can be used in a variant according to the invention, so that no coupling elements of the drives come into contact with the suspension.
  • the wear of pumps can be reduced if the pump is operated magnetically, wherein the drive magnet is arranged outside the suspension area.
  • a double-acting piston pump is used with two pressure chambers, which are separated by a piston which is actuated by the magnetic drive.
  • This magnetic drive can, for example, have an outer magnet which encompasses the pump cylinder and can be driven by a linear drive, so that the stroke of the piston is predetermined by the actuating movement of the linear drive.
  • Shown in Figure 1 is a continuous processing plant for mixed plastics and contaminated plastics, which are sorted out of residual waste, while PVC, PET and rubber is sorted out as foreign matter.
  • the following processes have been brought to market, but only the process (according to WO 2005/071043 A1) has been designed for continuous operation.
  • the other two processes are batch-operated plants and can be used for min. three units are called quasi-continuous operation. These methods are described in JP 08 034978A (Patent Abstracts), US 4 584 421 A and CN 1 284 537 A.
  • a difference between the aforementioned methods and the new method according to FIG. 1 lies in the continuous feed via at least two feed devices, 20/22 into a horizontal reactor 1 in which the following six process steps take place simultaneously and which has a common unseparated gas space.
  • the distillation tower 23 is thus designed so that longer-chain hydrocarbons condense as C24 and run back into the cracking reactor 1.2 and remain there until they are shorter than C24.
  • the cracking bandwidth ranges from C1 to C22 with the majority at C12 to C16.
  • C1 (predominantly methane) to C4 (predominantly propane) remain in the gaseous state 32.1 at the selected temperature in the distillation tower 23.
  • These highly calorific, combustible gases are used in the multi-fuel burner 32.4 for thermal salt heating.
  • sulfur compounds especially sulfuric acids, halogen acids, such as hydrochloric acid (HC2) and possibly interfering organic acids are proposed devices according to FIGS. 7, 8 and 9 sorption to remove the aforementioned Use pollutants.
  • HC2 hydrochloric acid
  • basic reactive molecular sieves in the form of silica gel beds are suitable, which can be reused after regeneration. After the aforementioned pollutants are removed, the light liquid meets the quality requirements of low sulfur light fuel oil.
  • FIG. 6.1 shows a further embodiment variant for the formation of a melt reactor 1.1 and a downstream cracking reactor 1.2 in which the heating agent inlet 9 via the pipe distributor 9.3 lies opposite the heating outlet distributor 9.4 and the outlet 9.2.
  • the tubes 9 rotate with the delivery spiral 2.
  • FIG. 6.2 shows a variant embodiment of the melt reactor 1.1 in which preferably all drive elements for conveyors and pumps via magnetic drive motors 34 occur, in which neither content liquid can escape to the outside, or atmospheric oxygen comes into contact with the contents liquid 10.3.
  • the magnets are made of a special cobalt-containing alloy.
  • FIG. 11 shows a cracking reactor 1.2 in standing configuration with a tube bundle heat exchanger 9.5 arranged vertically.
  • the suspension is then driven in the circuit 37.
  • FIG. 11.1 shows a variant (39) to the circulating pump (35).
  • the circulation substrate (37) is pumped by the motor drive (39.5) in the direction of the reference numeral (39.1).
  • the jacket tube (39.4) has a jacket heating, not shown here.
  • the main cracking process takes place in the dynamic part of the heat exchanger 9.5 at 420 to 450 0 C.
  • This heat exchanger 9.5 has 3 parallel flow paths, in each of which a cleaning coil 9.6 is provided.
  • the non-cracked, long-chain carbon compounds 8 settled.
  • FIG. 12 shows a coil 9.6 of the heat exchanger which swirls in direct current with suspension 37 directly (about 1 to 20 rpm) and through the contact surface 9.6 swirls the suspension stream 9.10.
  • FIG. 13 shows how the spiral 9.6 standing under slight tension (against the outer surface of the pipe wall) scrapes off the incrustations of the deposited carbon compounds 8 and is removed from the heating surfaces with the product feedstream 37, 9.7. This ensures that the heat transfer is constantly maintained. Since the product consists of a lubricious, oily mass, the abrasion is classified as very low.
  • FIG. 14 shows an overall concept of an alternative plant for carrying out the process according to the invention, wherein instead of the single reactor with melting and cracking zone according to FIG. 1, two reactors 8, 10 connected in series are used. Similar to the above-described embodiment, the mixed plastics are fed to the melt reactor via some conveyors and melted there. This melting takes place at about 250 to 350 0 C, wherein the reactor 8 is heated by the liquid salt heater 20 and the melt is heated by means of a heat exchanger 9 according to Figures 12 and 13, wherein this heat exchanger is integrated into the liquid salt circuit. The molten suspension then passes through an overflow in the cracking reactor 10, in which the long-chain hydrocarbons are cracked at 420 to 45O 0 C. The structure of this cracking reactor is shown in FIG.
  • this cracking reactor 10 is associated with a heat exchanger 10.1, which is formed for example by two or three or more parallel tubes, in each of which a cleaning coil 9.6 is arranged, each associated with its own drive, such as a magnetic motor drive.
  • the gas formed during cracking is then condensed in a condenser 10.2 and enters a Venturi cooler 11 and a downstream tube bundle cooler 11.1, in which the condensate is cooled. This cooled to about 30 ° C condensate / vapor mixture is then passed into an intermediate container 15.
  • the high calorific gas may be used to operate a steam generator 19 or the liquid salt heater 20.
  • the intermediate product withdrawn from the intermediate product container 15 can then be fed to a plurality of purification stages 22.1, 22.2, 22.3, in which - as in the method according to FIG. 1 - contaminants are removed by absorption. At the end of the process, light liquid is present with the quality of light heating oil.
  • the cracking reactor 10 In the cracking reactor 10 remaining long-chain hydrocarbons are discharged and emulsified in an emulsifier 16 - for example by means of ultrasound and then also in the units 19, 20 (steam generator, liquid salt water heater) used, this thermal energy used to heat the suspension in the melt reactor 8 and cracking reactor 10 becomes.
  • the processes described above are preferably carried out in a nitrogen atmosphere, wherein the nitrogen originates, for example, from an air separation 25.
  • FIGS. 15 / 15.1 / 15.2 and 16 show a further embodiment in which plastic chips are melted in a melting tube (9.5) and the melt is conveyed directly into the screw conveyor pump by means of conveying spirals (9.6), which are surrounded by a heating medium (9) and heated. 39) are pumped into it.
  • the plastic chips (20) are placed in the feeding hopper (21.1) of the entry screw.
  • the feed screw (21.1) conveys the plastics into the compressor screw (22.2). Here, the plastics are compressed and the air is expelled by means of nitrogen.
  • the compressor screw (22.2) conveys the plastics into the melt reactor (9.5).
  • the feed from the melt reactor can be interrupted by means of slide (18).
  • the compacted plastic parts are pressed into the molten plastic (10.3) by means of the conveying spirals (9.6), while the liquefaction of the plastic parts is accelerated by the solvent effect of the already previously tainted plastic.
  • the plastics are heated to a maximum of 12O 0 C.
  • the registered with the plastics moisture (water) will evaporate and also the volatile components such as plasticizers are escaping and withdrawn through the bell (9.10) via line (11).
  • the plastic is heated further until it melts.
  • the melt is conveyed from here with the screw pump (39) into the cracking reactor (9.5).
  • a larger tube from the cracking reactor is equipped with a closed spiral, which conveys the melt down into the sump (10.4).
  • the melt is further heated until the boiling point is reached.
  • the melt from the sump is transported upwards (9.7 / 9.10) and also heated so that the boiling temperature is not exceeded.
  • the plastic melt is thus continuously circulated, in this case the outer screws (9.6) convey the melt into the upper pot (10.4) of the cracking reactor, from where it is conveyed downwards again by means of a closed spiral (39) in the middle tube and thereby with fresh melt (10.3) from the melt reactor (9.6 / 9.7) is mixed.
  • Part of the ascending vapors (10.6 / 23) are recondensed in the distillation column, which is mounted directly above the cracking reactor (10.6) and flow back into the cracking reactor.
  • the following partial condenser (40) will only pass vapors which do not condense at the set temperature.
  • This fraction is subsequently cooled with product (27.1.1) in a steel washing tube (50.1) and condensed.
  • a cyclone is used for the separation of the vapor / liquid phases.
  • the quantity of liquid product (27.1.1) required for the steel tube cooler (50.1) is provided by the pump (27.8).
  • This pump sucks the product from the product reservoir (27) and conveys it through the heat exchanger (24.6) so that it is cooled to a temperature of 20 to 90 0 C before it is fed to the steel washing pipe (50.1).
  • a cooling unit For cooling the compressor screw (27.1.1) and the product via the heat exchanger (24.6) a cooling unit is used.
  • a temperature control unit (40.5) is used to set the temperature in the partial condenser (40).
  • the vapors (10.6) originating from the cracking reactor (9.5) consist of short-chain and long-chain hydrocarbon atoms and rise in the rectification column (40).
  • rectification countercurrent distillation
  • the vapors (10.5) rise and the liquid mixture (10.6) flows downwards a first thermal fine separation is carried out.
  • a column (23.2) with an ordered packing is used.
  • the column (23.3) and the subsequent partial condenser (40) are designed for the relevant key separations of hydrocarbon compounds C10 to C24 carbon atoms per molecule.
  • the pre-fractionated vapors exiting the column pass through a special distributor through which the condensate flows out of the column Partial condenser is distributed to the packing of the column, in the partial condenser (40.1).
  • a precise temperature is set by means of cooling coils. This temperature can be between 150 0 C and 300 0 C.
  • thermal oil 40.2 and 40.3 is used.
  • the temperature control unit (40.4), as a cold or heat dispenser, ensures that the exact temperature of the required thermal oil is maintained.
  • the unique feature is that the selectability of the temperature in the partial condenser allows to set the maximum chain length of the gases leaving the cracking reactor exactly. If, for example, the partial condenser (40) is operated at about 300 ° C., more than 95% of the condenser (50) condenses only those molecules which consist of a chain length between about 10 ° C. to about 24 ° C. Atoms are focused on C12 to C16. This is because the gases leaving the partial condenser at a temperature of about 300 ° C. in the partial condenser only comprise molecules which have a maximum chain length of C24. If the temperature is increased / decreased, the chain length of the molecules in gas phase is correspondingly increased / decreased.
  • adjusting the temperature in the condenser following the partial condenser is crucial to producing fuel of a particular type. If, for example, a temperature of about 70 ° C. is prevailing in the cooler instead of 30 ° C., then the hydrocarbons C 1 to C 9 remain gaseous, while longer-chain hydrocarbons condense. The so-called low boilers remaining in the gas phase can be withdrawn and used to generate process energy. This separation of the low boilers C1 - C9 can thus be used to produce pure diesel fuel directly.
  • the vapors from the partial condenser (10.5.1) are fed into a quencher (50.1) with a motive nozzle where they are condensed by means of product (27.1.1) (to diesel).
  • the drive nozzle may be supplied with diesel fuel, having a temperature between 20 0 C and 9O 0 C.
  • the biphasic mixture from the quencher is subsequently separated in a cyclone (50).
  • the vapors or gases leaving the cyclone can be used as fuel gas.
  • the separated liquid (Diesel) is passed into a water separator (phase separator) (60), from where it then flows into a storage tank (27.10).
  • the product first flows into a buffer container (27), the so-called storage container for the quencher.
  • a pump (27.8) delivers the product from here through a heat exchanger (24.6) into the motive nozzle of the quencher.
  • heat exchanger (24.6) By means of heat exchanger (24.6), the required temperature for the quenches can be set.
  • An industrial cooling unit (25) supplies the necessary cooling water.
  • the excess amount of product in the phase separator (60) is derived.
  • 6.1 discharge device shown here as a conveyor spiral
  • Level level maximum corresponds to the overflow height of the partition wall 10.1 (also baffle wall)
  • Feed device shown here as a spiral conveyor
  • bunker discharge device here shown as spiral conveyor
  • compression unit shown here as a piston pump
  • Jacket heaters shown here with four sub-wires. If necessary, the number of elements can be reduced, or increased by additional heating elements.
  • the circulating product consists of the final product in the form of light fuel oil and / or diesel fuel, ie with the product produced is cooled in the circuit.
  • the circulation product 27.1 with a temperature of about 3O 0 C is cooled down in the radiator 24.6 to about 1O 0 C and with the sprayers 24.7 in over the in-more and more cooling and condensate 27.1 over the individual Qunchezonen 24.10 gas stream 10.5 as a liquid Mixture of fresh product and recycled product 27.1 emerges in the output of the column as product 27.2.
  • the separation zone between the light liquid 27.1 and the water 27.7 can be determined with millimeter precision. Is the max. Level reaches 27.2, the engine valve 27.5 opens until the lower water level 27.3 is reached.
  • FIG. 7 Shown here (FIG. 7) are two groups 28.5 u. 28.6, which are driven in alternating operation. If one group is loaded, the system switches to the other group. If a group is emptied or replaced individual containers, the inflow is 27.6 bringsschiebert 18 and nitrogen 18.5 fed through the open slide 18.1 and then the outflow slide (18) open and via the connection 18.7 u. 28.8 pumped back the remaining liquid in the container 27 via the pump 28.9.
  • the container contents 28.4 are blanketed with nitrogen and rendered inert. Thereafter, all slides are closed and the container is decoupled via the quick release 18.7, superimposed with nitrogen 18.5 and then set by opening the slide 18 in operation.
  • Absorbent packing materials such as e.g. Silicate gel etc. which absorbs and binds the interfering compounds from the product 27.1.
  • N2 nitrogen

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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)

Abstract

L'invention concerne un procédé et un dispositif pour le traitement de liquides à teneur en matière plastique et organiques à base de pétrole, huile de friture, graisses ou similaires, le mélange de matières étant introduit dans un réacteur, puis fondu dans une zone de fusion du réacteur et les substances étrangères étant extraites de la masse fondue. Les polymères à chaîne longue contenus en outre dans la masse fondue sont craqués dans une zone de craquage du réacteur jusqu'à ce que ces polymères passent dans un état gazeux, après quoi la phase gazeuse est extraite du réacteur et condensée dans un dispositif de refroidisssement. Finalement, les impuretés sont retirées du liquide léger présent après le refroidissement et le liquide léger est stocké.
EP07801847A 2006-08-25 2007-08-23 Procédé et dispositif pour le traitement de déchets à teneur en matière plastique Withdrawn EP2061859A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE102006039824 2006-08-25
DE102006046682 2006-09-29
DE102006055388 2006-11-22
DE102007039887A DE102007039887A1 (de) 2006-08-25 2007-08-23 Verfahren und Vorrichtung zum Aufbereiten von kunststoffhaltigen Abfällen
PCT/EP2007/007419 WO2008022790A2 (fr) 2006-08-25 2007-08-23 Procédé et dispositif pour le traitement de déchets à teneur en matière plastique

Publications (1)

Publication Number Publication Date
EP2061859A2 true EP2061859A2 (fr) 2009-05-27

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ID=39107155

Family Applications (1)

Application Number Title Priority Date Filing Date
EP07801847A Withdrawn EP2061859A2 (fr) 2006-08-25 2007-08-23 Procédé et dispositif pour le traitement de déchets à teneur en matière plastique

Country Status (4)

Country Link
US (1) US20090321317A1 (fr)
EP (1) EP2061859A2 (fr)
DE (1) DE102007039887A1 (fr)
WO (1) WO2008022790A2 (fr)

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WO2008022790A3 (fr) 2008-07-17
DE102007039887A1 (de) 2008-06-12
US20090321317A1 (en) 2009-12-31
WO2008022790A2 (fr) 2008-02-28

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