Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
  • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
  • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
• • 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 oily residues, wherein the plastic materials and / or residues are sorted by grade and compacted using a registration system and the compacted mass is fed to a melting vessel and heated therein ;
• the invention relates to an apparatus for carrying out the method for obtaining fractionated hydrocarbons from plastic materials and / or oil-containing residues.
• Plastics are used today in almost all areas of life and must be recycled after use and / or disposed of. At the same time, health-friendly disposal poses considerable problems. 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 gas resulting from the cracking process consists of a mixture of methane, ethane, ethene, propane, propylene, i-butene, i-butane, 1-butene, 1-butane, pentane and the like, as well as 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 long-chain hydrocarbons. The oil-like residue can in a further process step
• BESTATIGUNGSKOPIE be mixed with water. This produces an oil / water emulsion, which can be utilized energetically, for example as a lighting agent.
• CN 1284537A has disclosed a process for recovering hydrocarbons, such as gases or oils, from plastic materials, which has a melting and cracking process with subsequent oil gas separation and distillation of the oil mixture.
• plastic raw materials are melted and vaporized within a container (melting and cracking reactor).
• 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 clogs, which worsen the further heat input. As a result, the heat consumption is high in relation to the yield.
• CN 2435146Y has disclosed a similar method.
• the invention has for its object to further develop the aforementioned method and the device such that the energy input is improved and that in particular by an optimal and targeted use of energy and heat recovery in undersc different areas, the efficiency of the method and the device is verb essert ,
• This object is achieved according to the invention by a process for obtaining fractionated hydrocarbons from plastic materials and / or from oily residues, wherein the plastic materials and / or residues are sorted by type and compacted using an entry system with exclusion of air and the compressed mass is supplied to a melting vessel and heated therein, 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 into an evaporation vessel in which further heat input a second liquid phase and a second gas phase is formed, 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 tank and third gas phase from the reheater are fed to a cracking tower, where further breakage (cracking) of the long-chain hydrocarbons into short-chain hydrocarbons takes place and the resulting oil gas is then
• 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 are advantageously used in the heating system for generating the primary process heat.
• the capacitor can consist of a precondensator and a main capacitor, which can 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 regulations on waste recycling.
• a precondensator and a main capacitor are used as the capacitor, the excess heat from the precondensator, the main capacitor and the residual precooling vessel being supplied to the heating system, and the main capacitor being connected to a multicircular 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 stuffing 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 fraction within the melting vessel is transported to a sedimentation compartment underneath, where the residue fraction is concentrated and then the concentrated residue fraction is transferred to a residue precooling vessel, in which the residue fraction is cooled by means of a cooling medium, preferably below 120 ° C.
• 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 the extraction of fractionated ohlen hydrogen from plastic materials and / or from oil-containing residues, wherein the plastic materials and / or the residues are sorted by variety, is characterized by a registration system for the compression of the plastic material and / or the oily residues with exclusion of air, and by a downstream melting tank for heating and melting the compacted mass to produce a first liquid phase, a first gas phase and a residue portion, wherein after the AufschmelzbereheatHer for generating further heat input of a second liquid phase and a second gas phase, an evaporation tank is disposed on welc to Initiation and further heating of the second liquid phase, a reheater follows the emergence of a third gas phase, and the evaporation tank and the reheater to separate the resulting oil gas from black a cracking tower is connected to the oil and unvaporised plastic parts, to which a main condenser is connected to condense the oil to liquid oil.
• a stuffing screw or a stuffing plant for compacting the plastic substances and / or the oil-containing residues in the melting container within the registration system of the plastic material and / or the oily residues, in front of which, if necessary, a spherical transfer container for transfer into the stuffing screw or Stopftechnik is located.
• the exit of the plug screw or the stuffing machine opens below the liquid level of the molten mass into the melting container.
• 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 fraction 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 by the common heat carrier heating system.
• Figure 5 shows another registration system of a process plant with a cooling jacket around the supply pipe and plug screw shell in front of another melting tank
• Figure 6 shows another example of a main capacitor
• FIG. 7 shows a further process plant similar to FIG.
• the process plant for obtaining fractionated hydrocarbons, from plastic materials and / or oily residues shown in the figures, consists of a silo installation 1, in which the plastic materials to be treated, preferably in the shredded state, are stored. The storage can also be done in a bunker.
• a silo installation 1 in which the plastic materials to be treated, preferably in the shredded state, are stored. The storage can also be done in a bunker.
• M motor-driven trough screw conveyor 2 connected to the silo 1, which promotes 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 melting tank 7 has at its lower end a sedimentation compartment 10 for receiving and concentrating a residue fraction which precipitates out of 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.
• 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 a stirrer 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 container 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. Furthermore, 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.
• a heating of the plastic mass takes place, 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 via the outlet A are transported in a conduit in a Verdampfungs- 20, in which under further heat input into the mass a second liquid phase and a second gas phase is formed.
• 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.
• 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 is then fed 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 carried out in two different ways: The hot gas stream is sucked into the liquid recycle stream from cooled condensate, where due to the high turbulence intensive heat exchange and instantaneous 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 compared to that of FIG. 1.
• the connecting tube of the melting container 7 for connecting the screw conveyor 4 or the stuffing mechanism is here formed at an acute angle to the melting container; otherwise the design is the same.
• FIG. 3 shows a process plant which is very similar to that of FIGS. 1a, 1b and 1c and in which the heat transfer and cooling circuits are shown completely.
• the heating system 38 is divided into five heat carrier circuits WT 1 to WT 5.
• WT 1 is connected via lines to the reflow 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.
• Figures 4 and 5 show two further 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 are additionally surrounded by a cooling jacket 43, through which cooling water flows.
• FIG. 6 shows a further 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.
• cooled condensate is fed back into the main condenser 44 in countercurrent, as can be seen in FIG.
• the gas flowing through the packed columns 46 is cooled shock-like.
• the overhead outlet 53 which corresponds to the outlet 39 in FIG. 1c, non-condensed residual gas is either used as combustion gas or a further condenser can follow here, by means of which remaining portions of HCs within the residual gas are condensed.
• the liquid oil, the target product of the process plant is removed.
• FIG. 7 essentially differs from FIG. 3 only in that heating coils 56, 57 are additionally installed in the melting tank 7 and in the evaporation tank 20 in order to increase the introduction of heat into the masses. These heating coils 56, 57 are connected to their supply according to the figure 7 to own heat transfer medium circuits WT circuit 1 and WT circuit 2 of the heat transfer heating system 58, which either gas-fired ⁇ I - for example, with the residual gas from the main capacitors 30 and 44 - or electrically heated. When using heating coils, 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)

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• 2005
  • 2005-01-24 PT PT05701145T patent/PT1745115E/pt unknown
  • 2005-01-24 SI SI200531238T patent/SI1745115T1/sl unknown
  • 2005-01-24 WO PCT/EP2005/000661 patent/WO2005071043A1/fr active Application Filing
  • 2005-01-24 PL PL05701145T patent/PL1745115T3/pl unknown
  • 2005-01-24 CA CA2558347A patent/CA2558347C/fr not_active Expired - Fee Related
  • 2005-01-24 EP EP05701145A patent/EP1745115B1/fr not_active Not-in-force
  • 2005-01-24 DE DE502005010684T patent/DE502005010684D1/de active Active
  • 2005-01-24 DK DK05701145.4T patent/DK1745115T3/da active
  • 2005-01-24 AT AT05701145T patent/ATE491771T1/de active

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