EP3247775A1 - Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizöl - Google Patents
Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizölInfo
- 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
Links
- 238000010438 heat treatment Methods 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000013502 plastic waste Substances 0.000 title claims abstract description 18
- 239000000446 fuel Substances 0.000 title claims description 8
- 238000005336 cracking Methods 0.000 claims abstract description 90
- 239000004033 plastic Substances 0.000 claims abstract description 76
- 229920003023 plastic Polymers 0.000 claims abstract description 76
- 238000004821 distillation Methods 0.000 claims abstract description 54
- 239000007789 gas Substances 0.000 claims abstract description 49
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 49
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 49
- 239000000463 material Substances 0.000 claims abstract description 42
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000002699 waste material Substances 0.000 claims abstract description 13
- 238000002844 melting Methods 0.000 claims abstract description 10
- 230000008018 melting Effects 0.000 claims abstract description 10
- 230000002378 acidificating effect Effects 0.000 claims abstract description 7
- 229920000098 polyolefin Polymers 0.000 claims abstract description 7
- 239000011261 inert gas Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 34
- 230000008569 process Effects 0.000 claims description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 239000000872 buffer Substances 0.000 claims description 12
- 239000004215 Carbon black (E152) Substances 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 11
- 238000004062 sedimentation Methods 0.000 claims description 10
- 238000001179 sorption measurement Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 229920000642 polymer Polymers 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 238000011049 filling Methods 0.000 claims description 8
- 239000003112 inhibitor Substances 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 238000009835 boiling Methods 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 4
- 239000007924 injection Substances 0.000 claims description 4
- 150000007524 organic acids Chemical class 0.000 claims description 4
- 235000005985 organic acids Nutrition 0.000 claims description 4
- 239000003990 capacitor Substances 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 238000001035 drying Methods 0.000 claims description 2
- 229910052736 halogen Inorganic materials 0.000 claims description 2
- -1 halogen acids Chemical class 0.000 claims description 2
- 230000008929 regeneration Effects 0.000 claims description 2
- 238000011069 regeneration method Methods 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims description 2
- 238000005303 weighing Methods 0.000 claims description 2
- 239000003208 petroleum Substances 0.000 claims 3
- 238000004080 punching Methods 0.000 claims 1
- 230000000630 rising effect Effects 0.000 claims 1
- 150000003464 sulfur compounds Chemical class 0.000 claims 1
- 239000000047 product Substances 0.000 description 29
- 239000003921 oil Substances 0.000 description 22
- 239000012071 phase Substances 0.000 description 14
- 239000002245 particle Substances 0.000 description 10
- 125000004432 carbon atom Chemical group C* 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 8
- 230000008901 benefit Effects 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 239000000155 melt Substances 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 150000003254 radicals Chemical class 0.000 description 5
- 239000002893 slag Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000010791 quenching Methods 0.000 description 4
- 239000003381 stabilizer Substances 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000003963 antioxidant agent Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 230000003078 antioxidant effect Effects 0.000 description 2
- 239000007853 buffer solution Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 230000002452 interceptive effect Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- XURIQWBLYMJSLS-UHFFFAOYSA-N 1,4,7,10-tetrazacyclododecan-2-one Chemical compound O=C1CNCCNCCNCCN1 XURIQWBLYMJSLS-UHFFFAOYSA-N 0.000 description 1
- 206010053567 Coagulopathies Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000035602 clotting Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000008162 cooking oil Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000002329 infrared spectrum Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Combustion & Propulsion (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
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 (de) | 2015-01-19 | 2015-01-19 | Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizöl |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3247775A1 true EP3247775A1 (de) | 2017-11-29 |
EP3247775B1 EP3247775B1 (de) | 2020-07-08 |
Family
ID=52596923
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP15707270.3A Active EP3247775B1 (de) | 2015-01-19 | 2015-01-19 | Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizöl |
Country Status (5)
Country | Link |
---|---|
US (2) | US20180010050A1 (de) |
EP (1) | EP3247775B1 (de) |
ES (1) | ES2822597T3 (de) |
PL (1) | PL3247775T3 (de) |
WO (1) | WO2016116114A1 (de) |
Families Citing this family (27)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA2972505A1 (en) | 2017-07-05 | 2019-01-05 | Decide Nv | Process and system for treating municipal solid waste materials and producing multiple products |
PL422780A1 (pl) * | 2017-09-07 | 2019-03-11 | Polymer Energy Polska Spółka Z Ograniczoną Odpowiedzialnością | Sposób ciągłego przetwarzania odpadów organicznych, zwłaszcza oczyszczonych lub zanieczyszczonych odpadowych tworzyw sztucznych, na regranulaty oraz woski polimerowe |
CN109289225B (zh) * | 2018-09-12 | 2021-02-19 | 国宏中晶集团有限公司 | 一种冷凝回收热解气的装置及方法和应用 |
DE102019001702A1 (de) * | 2019-03-11 | 2020-09-17 | Olaf Heimbürge | Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien |
DE102019001696A1 (de) * | 2019-03-11 | 2020-09-17 | Olaf Heimbürge | Anlage und Verfahren zur katalytischen Herstellung von Dieselölen aus organischen Materialien |
NL2023870B1 (en) | 2019-09-20 | 2021-05-27 | Bluealp Innovations B V | Cracking long chained hydrocarbons from plastic-containing waste and organic liquids |
ES2759939B2 (es) * | 2019-11-21 | 2021-06-14 | Urbaser Sa | Procedimiento para convertir residuos plasticos en productos liquidos utiles en la industria petroquimica |
US11639472B2 (en) * | 2020-04-22 | 2023-05-02 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polyethylene via oil refinery with filtering and metal oxide treatment of pyrolysis oil |
WO2021216873A1 (en) * | 2020-04-22 | 2021-10-28 | Chevron U.S.A. Inc. | Circular economy for plastic waste to polypropylene via oil refinery with filtering and metal oxide treatment of pyrolysis oil |
WO2022056212A1 (en) | 2020-09-14 | 2022-03-17 | Ecolab Usa Inc. | Cold flow additives for plastic-derived synthetic feedstock |
JP2024503111A (ja) * | 2021-01-15 | 2024-01-24 | ルーマス テクノロジー エルエルシー | 廃プラスチックの石油化学製品への変換 |
JP2024509805A (ja) * | 2021-03-10 | 2024-03-05 | エコラボ ユーエスエー インコーポレイティド | プラスチック由来の合成原料のための安定添加剤 |
US20220315841A1 (en) * | 2021-03-31 | 2022-10-06 | Ecolab Usa Inc. | Extraction solvents for plastic-derived synthetic feedstock |
US20230114094A1 (en) * | 2021-10-12 | 2023-04-13 | Republic Services, Inc. | Integrated center and process for recycling both polyolefin and polyester |
KR20240088863A (ko) | 2021-10-14 | 2024-06-20 | 에코랍 유에스에이 인코퍼레이티드 | 플라스틱-유래 합성 공급원료를 위한 방오제 |
EP4202017A1 (de) * | 2021-12-27 | 2023-06-28 | Achileas Poulios | Anlage und verfahren zur umwandlung von kunststoffrohstoffen in brennstoff |
NL2032929B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | System for separation of gas, liquid, and solid particles in a material |
NL2032928B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | System for separation of gas, liquid, and solid particles in a material |
WO2024046896A1 (en) | 2022-08-31 | 2024-03-07 | Bluealp Innovations B.V. | System for separation of gas, liquid, and solid particles in a material |
NL2032925B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | System for separation of gas, liquid, and solid particles in a material |
NL2032930B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | Methods and apparatuses for plastics pyrolysis |
NL2032926B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | System for separation of gas, liquid, and solid particles in a material |
NL2032927B1 (en) | 2022-08-31 | 2024-03-15 | Bluealp Innovations B V | System for separation of gas, liquid, and solid particles in a material |
NL2033241B1 (en) | 2022-10-05 | 2024-04-18 | Bluealp Innovations B V | Staggered heat exchangers for cracking hydrocarbons |
NL2033249B1 (en) | 2022-10-06 | 2024-04-19 | Bluealp Innovations B V | Method of heating plastics for the production of oil |
NL2033250B1 (en) | 2022-10-06 | 2024-04-19 | Bluealp Innovations B V | Method of heating plastics for the production of oil |
WO2024141608A1 (en) | 2022-12-28 | 2024-07-04 | Bluealp Innovations B.V. | System and process for degassing of pyrolysis plastics |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1423420A (en) * | 1973-08-16 | 1976-02-04 | Mitsubishi Heavy Ind Ltd | Processing synthetic polymer waste |
BE830379A (fr) * | 1975-06-18 | 1975-10-16 | Procede pour recuperer des constituants utiles de dechets en polymeres synthetiques | |
BE830380A (fr) * | 1975-06-18 | 1975-10-16 | Appareil de decomposition thermique | |
CH592275A5 (en) * | 1975-06-20 | 1977-10-14 | Mitsubishi Heavy Ind Ltd | Thermal decomposition and recovery of scrap polymers - by selective distillation via plate and coil reflux systems |
US4367121A (en) * | 1980-05-01 | 1983-01-04 | Phillips Petroleum Company | Fractional distillation column control |
CN1127519A (zh) * | 1993-07-20 | 1996-07-24 | Basf公司 | 蒸汽裂化器中回收塑料的方法 |
DE4344311A1 (de) * | 1993-12-23 | 1995-06-29 | Linde Ag | Verfahren und Vorrichtung zur thermischen Depolymerisation von Kunststoffen |
FR2735460B1 (fr) * | 1995-06-15 | 1997-07-25 | Inst Francais Du Petrole | Procede et dispositif de traitement d'un gaz contenant de l'hydrogene sulfure, comportant une etape d'elimination du soufre cristallise par refroidissement |
US6011187A (en) * | 1996-02-27 | 2000-01-04 | Mitsubishi Heavy Industries, Ltd. | Method and apparatus for reclaiming oil from waste plastic |
DE19722585B4 (de) * | 1997-05-30 | 2006-06-08 | Mitteldeutsches Bitumenwerk Gmbh | Verfahren zur Gewinnung von Paraffinen und/oder Mikrowachsen aus Altkunststoffen |
WO2001018152A1 (fr) * | 1999-09-06 | 2001-03-15 | Bright Co Ltd. | Procede de degradation par pyrolyse de dechets de matieres plastiques en vue de leur transformation en melange d'hydrocarbures utilisables comme combustibles |
KR100322663B1 (ko) * | 2000-03-20 | 2002-02-07 | 곽호준 | 폐플라스틱을 이용한 휘발유, 등유 및 경유의 연속식제조방법 및 그 시스템 |
CN1223650C (zh) * | 2003-09-25 | 2005-10-19 | 北京帅更新能源技术有限公司 | 工业化用废塑料生产汽油、柴油的方法 |
PT1745115E (pt) | 2004-01-24 | 2011-03-23 | Wolfgang Nick | Dispositivo e processo para a extracção e hidrocarbonetos fraccionados a partir de materiais plásticos recicláveis e/ou de resíduos de óleo |
WO2008022790A2 (de) | 2006-08-25 | 2008-02-28 | Granit Systems S.A. | Verfahren und vorrichtung zum aufbereiten von kunststoffhaltigen abfällen |
EP2516592B1 (de) * | 2009-12-22 | 2018-06-13 | Cynar Plastics Recycling Limited | Umwandlung von kunststoffabfallmaterial in kraftstoff |
AT511772B1 (de) * | 2011-05-05 | 2018-03-15 | Omv Refining & Marketing Gmbh | Verfahren und vorrichtung zur energieeffizienten aufbereitung sekundärer lagerstätten |
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 |
-
2015
- 2015-01-19 EP EP15707270.3A patent/EP3247775B1/de active Active
- 2015-01-19 WO PCT/EP2015/000081 patent/WO2016116114A1/de active Application Filing
- 2015-01-19 ES ES15707270T patent/ES2822597T3/es active Active
- 2015-01-19 US US15/544,260 patent/US20180010050A1/en not_active Abandoned
- 2015-01-19 PL PL15707270T patent/PL3247775T3/pl unknown
-
2022
- 2022-08-03 US US17/879,944 patent/US20230059944A1/en active Pending
Also Published As
Publication number | Publication date |
---|---|
US20180010050A1 (en) | 2018-01-11 |
WO2016116114A1 (de) | 2016-07-28 |
US20230059944A1 (en) | 2023-02-23 |
PL3247775T3 (pl) | 2020-12-14 |
WO2016116114A8 (de) | 2017-03-16 |
EP3247775B1 (de) | 2020-07-08 |
ES2822597T3 (es) | 2021-05-04 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP3247775B1 (de) | Verfahren und anlage zum überführen von kunststoffabfällen in einen brennstoff mit eigenschaften von diesel/heizöl | |
EP2876146B1 (de) | Verfahren und anlage zum aufbereiten von kunststoffwertstoffen | |
EP2981572B1 (de) | Verfahren zum abbau von synthetischen polymeren und eine vorrichtung zu dessen durchführung | |
DE878830C (de) | Verfahren und Vorrichtung zur Herstellung fluechtiger Kohlenwasserstoffe aus kohlenwasserstoffhaltigen festen Stoffen | |
DE68908205T2 (de) | Wiederverwertung von ölhaltigen Raffinierrückständen. | |
DE10049377C2 (de) | Katalytische Erzeugung von Dieselöl und Benzinen aus kohlenwasserstoffhaltigen Abfällen und Ölen | |
EP1745115B1 (de) | Vorrichtung und verfahren zum gewinnen von fraktionierten kohlenwasserstoffen aus kunststoffwertstoffen und/oder aus ölhaltigen reststoffen | |
DE102007039887A1 (de) | Verfahren und Vorrichtung zum Aufbereiten von kunststoffhaltigen Abfällen | |
DE102004003667A1 (de) | Verfahren zum Gewinnen von fraktionierten Kohlenwasserstoffen aus Kunststoffwertstoffen und/oder ölhaltigen Reststoffen sowie Vorrichtung hierzu | |
DE69615089T2 (de) | Verbessertes Verfahren und Vorrichtung zum Aufarbeiten von Öl | |
DE202015009755U1 (de) | Anlage zum Überführen von Kunststoffabfällen in einen Brennstoff mit Eigenschaften von Diesel/Heizöl | |
DE3401840A1 (de) | Verfahren und anlage zur aufbereitung schwerer rohoele insbesondere zur herstellung von koksen fuer metallurgische zwecke | |
DE2415412A1 (de) | Verfahren und vorrichtung zur behandlung hochmolekularer hydrocarbonate oder altoele | |
DE3224114A1 (de) | Verfahren zum erwaermen von fluessigkeiten mit dabei zur bildung von ablagerungen neigenden bestandteilen | |
DE102008051058B4 (de) | Verfahren zur Abtrennung von festen Partikeln aus einer Wasserphase in einer Anlage zur Erzeugung von Kohlenwasserstoffen | |
DE937723C (de) | Verfahren und Vorrichtung zur Umwandlung von Kohlenwasserstoffen in leichtere Produkte | |
WO2010086092A1 (de) | Verfahren und vorrichtung zur abtrennung von festen partikeln aus einer wasserphase | |
DE964086C (de) | Verfahren zur Umwandlung von schweren Kohlenwasserstoffoelen | |
DE102019102528A1 (de) | Verfahren und Vorrichtung zum Behandeln von Altöl | |
DE102018106311A1 (de) | Verfahren und Vorrichtung zum Behandeln von Öl | |
DE19708384B4 (de) | Vorrichtung zum Recycling von Altölen und anderen Stoffen, die gemeinsam mit dem Altöl recycelt, destilliert und gecrackt werden können | |
DE957326C (de) | Verfahren zum Raffinieren von Rohoel | |
AT86433B (de) | Verfahren und Vorrichtung zur Herstellung von Petroleum aus Rohöl. | |
DE102021133899A1 (de) | Pyrolyseverfahren und Pyrolysevorrichtung zur Herstellung von Pyrolysegas und Pyrolysekoks | |
CH660021A5 (de) | Verfahren und anlage zur aufbereitung schwerer rohoele, insbesondere fuer eine nutzung derer kokse fuer metallurgische zwecke. |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE |
|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE |
|
17P | Request for examination filed |
Effective date: 20170818 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
AX | Request for extension of the european patent |
Extension state: BA ME |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: VAN DER REE , TEUNIS CHRISTIAAN Inventor name: WESER, GEROLD |
|
DAX | Request for extension of the european patent (deleted) | ||
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
17Q | First examination report despatched |
Effective date: 20180827 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R079 Ref document number: 502015012954 Country of ref document: DE Free format text: PREVIOUS MAIN CLASS: C10G0001100000 Ipc: C10G0009000000 |
|
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: GRANT OF PATENT IS INTENDED |
|
RIC1 | Information provided on ipc code assigned before grant |
Ipc: C10G 1/10 20060101ALI20200116BHEP Ipc: C10G 7/00 20060101ALI20200116BHEP Ipc: C10G 9/00 20060101AFI20200116BHEP Ipc: C10G 9/40 20060101ALI20200116BHEP |
|
INTG | Intention to grant announced |
Effective date: 20200204 |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE PATENT HAS BEEN GRANTED |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: REF Ref document number: 1288441 Country of ref document: AT Kind code of ref document: T Effective date: 20200715 Ref country code: CH Ref legal event code: EP |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R096 Ref document number: 502015012954 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: LANGUAGE OF EP DOCUMENT: GERMAN |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: NV Representative=s name: BOHEST AG, CH |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: T3 Effective date: 20200930 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: TRGR |
|
REG | Reference to a national code |
Ref country code: NO Ref legal event code: T2 Effective date: 20200708 |
|
REG | Reference to a national code |
Ref country code: LT Ref legal event code: MG4D |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: MP Effective date: 20200708 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BG Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20201008 Ref country code: FI Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: GR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20201009 Ref country code: LT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: PT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20201109 Ref country code: HR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IS Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20201108 Ref country code: LV Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: RS Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R097 Ref document number: 502015012954 Country of ref document: DE |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: EE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: RO Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: SM Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: CZ Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2822597 Country of ref document: ES Kind code of ref document: T3 Effective date: 20210504 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: AL Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
26N | No opposition filed |
Effective date: 20210409 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SK Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SI Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 Ref country code: MC Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20210119 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20210119 |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: MM01 Ref document number: 1288441 Country of ref document: AT Kind code of ref document: T Effective date: 20210119 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: AT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20210119 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: HU Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO Effective date: 20150119 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: CY Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
P01 | Opt-out of the competence of the unified patent court (upc) registered |
Effective date: 20230530 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: ES Payment date: 20240201 Year of fee payment: 10 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: MK Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20240129 Year of fee payment: 10 Ref country code: GB Payment date: 20240129 Year of fee payment: 10 Ref country code: CH Payment date: 20240202 Year of fee payment: 10 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: SE Payment date: 20240127 Year of fee payment: 10 Ref country code: PL Payment date: 20240103 Year of fee payment: 10 Ref country code: NO Payment date: 20240129 Year of fee payment: 10 Ref country code: IT Payment date: 20240122 Year of fee payment: 10 Ref country code: FR Payment date: 20240125 Year of fee payment: 10 Ref country code: DK Payment date: 20240125 Year of fee payment: 10 Ref country code: BE Payment date: 20240129 Year of fee payment: 10 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: TR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20200708 |