EP0321807B1 - Verfahren zum Aufarbeiten von Abfallmaterial - Google Patents

Verfahren zum Aufarbeiten von Abfallmaterial Download PDF

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Publication number
EP0321807B1
EP0321807B1 EP88120665A EP88120665A EP0321807B1 EP 0321807 B1 EP0321807 B1 EP 0321807B1 EP 88120665 A EP88120665 A EP 88120665A EP 88120665 A EP88120665 A EP 88120665A EP 0321807 B1 EP0321807 B1 EP 0321807B1
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EP
European Patent Office
Prior art keywords
gas
fraction
benzene
line
catalyst
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Expired - Lifetime
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EP88120665A
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German (de)
English (en)
French (fr)
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EP0321807A2 (de
EP0321807A3 (en
Inventor
Hans Prof. Dr. Lechert
Volkert Woebs
Qun Sung
Walter Prof. Dr. Kaminsky
Hansjörg Prof. Dr. Sinn
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ABB AG Germany
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Asea Brown Boveri AG Germany
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Priority to AT88120665T priority Critical patent/ATE74617T1/de
Publication of EP0321807A2 publication Critical patent/EP0321807A2/de
Publication of EP0321807A3 publication Critical patent/EP0321807A3/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—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

Definitions

  • the invention relates to a process for working up waste material containing hydrocarbon compounds, in particular waste material containing plastic or rubber waste, the waste material being pyrolytically decomposed and the pyrolysis gas formed being converted into a liquid fraction and a gas fraction by cooling.
  • the gas fraction which is mainly hydrogen, methane, ethane, ethene, propane and in small quantities - contains a total of approximately 5% by volume - higher saturated and unsaturated hydrocarbons, approximately 15 to 30% by weight is used to carry out the pyrolysis process. This is preferably done by using the gas fraction as heating gas and / or in the case of pyrolysis in a fluidized bed by using it as a fluidizing gas.
  • the remaining gas fraction despite its interesting components, can hardly be sold on the market, and storage, transport and processing are complex and difficult to carry out.
  • the recycling or further processing of the liquid fraction which contains valuable components such as benzene, toluene and xylene (BTX aromatics), is completely unproblematic.
  • the invention is therefore based on the object of increasing the liquid fraction in a simple manner in a method of the type mentioned at the outset.
  • One solution is that the pyrolysis gas is cooled until the gaseous benzene contained therein and the higher-boiling gaseous pyrolysis gas components pass into the liquid phase, and a benzene-containing liquid fraction is formed, so that a gas mixture containing benzene and toluene is obtained from the benzene-containing liquid fraction that the gas mixture together with the gas fraction is brought into contact with a zeolitic catalyst at a temperature of 300 to 450 ° Celsius, and that the catalytically treated mixture is separated by cooling into a fraction which is liquid at ambient temperature and a residual gas fraction.
  • the pyrolysis gas is therefore cooled to such an extent that the gaseous benzene it contains, including the constituents, which have a higher boiling point than benzene, pass into the liquid phase and a liquid fraction containing benzene is formed. Since the benzene has a boiling point of 80 ° Celsius at ambient pressure and the cooling is carried out approximately at ambient pressure, the pyrolysis gas must be cooled to approximately 75 to 80 ° Celsius in order to obtain the liquid fraction containing benzene.
  • This benzene-containing liquid fraction is then heated to a temperature above the boiling point of the toluene and a gas mixture is expelled which, together with the gas fraction remaining after the benzene-containing liquid fraction has been obtained, is passed over a zeolitic catalyst at elevated temperature.
  • the olefins present in the gas fraction react with the lower-boiling and gaseous fractions of the liquid fraction, in particular benzene and toluene, to form condensable products.
  • benzene and ethene form ethylbenzene.
  • the remaining residual gas fraction in which very little olefins are still present (approximately 3% by weight), contains essentially hydrogen, methane, ethane, propane and traces of unsaturated and saturated higher hydrocarbons. Although this residual gas fraction is now only 30 to 35% by weight of the feed, it is still completely sufficient to operate the pyrolysis process independently.
  • the residual gas fraction still contains sufficient proportions of saturated C1 to C3 hydrocarbon compounds and is therefore very suitable and sufficient for use, for example, as heating gas and fluidizing gas for carrying out the pyrolysis process.
  • the second way to achieve the object according to the invention is that the cooling of the pyrolysis gas is carried out to a temperature at which a special gas fraction is formed, the proportions of C2 and C3 olefins and C6 and C7 aromatics in a molar ratio of approximately 1 have that the special gas fraction is brought into contact with a zeolitic catalyst at a temperature of 300 to 450 ° Celsius, and that the catalytically treated special gas fraction is separated by cooling into a fraction liquid at atmospheric pressure and a residual gas fraction.
  • the pyrolysis gas is only cooled to a temperature at which a special gas fraction is formed, which contains fractions of C2 and C3 olefins and C6 and C7 aromatics, the molar ratio of the C2 and C3 olefins to the C6 and C7 aromatics is about 0.8 to 1.2, preferably about 1.
  • the pyrolysis gas must be cooled to a temperature of approximately 80 to 100 ° Celsius. The special gas fraction is then treated just like the first solution and with the same end result.
  • the cooling of the special gas fraction is carried out to a temperature above the boiling point of the benzene, preferably to a temperature which is at most 10 to 20 ° C. above the boiling point. Since the process is carried out at approximately ambient pressure, the information about the boiling point is based on ambient pressure. If the cooling is carried out at a pressure that deviates from the ambient pressure, the cooling temperature must be changed according to the pressure.
  • the catalyst is designed as a fixed bed catalyst and the contact time of the gas mixture or the special gas fraction with the catalyst is 0.3 to 2 Seconds, preferably 0.7 to 1.5 seconds.
  • the catalyst is used in fine-grained form and used to form a fluidized bed, and that the contact time of the gas mixture or the special gas fraction with the fluidized bed is 0.4 to 1, 5 seconds, preferably 0.5 to 1.1 seconds.
  • the gas mixture or the special gas fraction is brought into contact with the catalyst at a temperature of 350 to 410 ° Celsius according to a preferred embodiment of the invention.
  • the commercially available catalyst ZSM5 is used as the catalyst.
  • the system according to FIG. 1 has a standing pyrolysis reactor 10, the upper area 12 of which is circular-cylindrical.
  • the lower region 14 adjoining at the bottom tapers downward in a circular cone shape and is provided at its end with a discharge line 16.
  • the fluidized bed 18 which forms in the pyrolysis reactor during operation has a vertical height which is approximately 80 to 90% of the clear height of the pyrolysis reactor, so that a gas space 20 remains free above the fluidized bed.
  • a supply line 22, which opens into the fluidized bed 18, is provided for introducing the waste material into the pyrolysis reactor.
  • Eddy gas lines 24 are connected to the pyrolysis reactor in the lower region 14 and are connected to the gas line 28 with the interposition of a control and shut-off element 26.
  • the gas-fired heating pipes 30 are used for indirect heating of the fluidized bed.
  • the heating pipes 30 are connected to the gas line 28 through a line 32 with an inserted control and shut-off device 34, in which the combustible residual gas fraction, which is generated in the system and is used as heating gas and fluidizing gas, is guided.
  • the combustion air required for the combustion is supplied to each heating tube through a line 36, and the exhaust gases are each discharged into the environment 40 through an exhaust line 38.
  • the gas space 20 of the pyrolysis reactor is connected by a line 42 to a cooling stage 46, a cyclone separator 44 being inserted in the line 42.
  • the line 42 is connected to the upper end of a cylindrical, standing cooler 48 of the cooling stage, the lower end of the cooler opens into a separating container 50.
  • a cooling coil 52 is arranged in the cooler itself, which is connected to a cooling medium, preferably cooling water or Cooling brine, is supplied.
  • the cooling medium is discharged through line 56.
  • a three-way valve 58 is inserted into line 54, the third connection of which is connected to line 56 by a line 60.
  • a temperature sensor 62 is provided in the cooler 48 below the cooling coil 52 and is connected to the three-way valve 58 by a control line 64 shown in broken lines. If necessary, a power amplifier, not shown, is inserted into the control line.
  • the lower region of the separating container 50 serves as a liquid space 66, the free space 68 above it serves as a gas space.
  • the liquid chamber 66 is connected at the bottom by a line 70 with an inserted shut-off and control element 72 to the upper region 74 of a standing, circular cylindrical and closed evaporation container 76.
  • a heating coil 80 is arranged in the lower region 78 of the evaporation container and is connected to a heating boiler 86 by a feed line 82 and a return line 84.
  • a three-way mixing valve 88 is inserted into the flow line 82 and connected to the return line 84 with a mixing line 90.
  • a temperature sensor 92 is arranged in the lower region 78 of the evaporation container 76 and acts on the three-way mixing valve 88 through a control line 94 shown in broken lines.
  • a line 96 is also provided, into which a shut-off device, not shown in the drawing, is inserted.
  • the boiler 86 is provided with a gas burner 98, which is connected to the gas line 28 by a line 100 with an inserted control and shut-off device 102.
  • the exhaust gas from the boiler 86 is discharged to the environment through the exhaust pipe 104.
  • the free space 68 of the separating tank 50 and the upper region 74 of the evaporation tank 76 are each connected by a line 106 or 108 to the inlet of a gas conveyor or compressor 110.
  • the outlet of the compressor 110 is connected by the line 112 to the lower end of a standing, cylindrical container 114, in which the catalyst is in the form of lumpy zeolites 116, and is therefore a fixed-bed catalyst.
  • the container 114 is surrounded by a jacket 120 for heating the catalytic converter to form a space 118 on all sides.
  • a gas burner 122 is arranged below the container 114 in the intermediate space 118 and is connected to the gas line 28 by a line 124 with an inserted control and shut-off element 126.
  • an exhaust gas line 128 is connected to the upper area of the intermediate space 118 and opens into the environment 40.
  • the piece size of the zeolites is approximately 3 to 20 mm.
  • the upper end of the container 114 is connected to a further cooling stage 132 by a line 130.
  • the line 130 opens into the upper end of a standing, circular-cylindrical cooler 134, the lower end of which opens into a further separating container 136.
  • a cooling coil 138 is arranged in the cooler 134, the cooling water or cooling brine supply thereof being provided by the lines 140.
  • the standing, circular-cylindrical further separating container 136 has a lower region 142, which is provided for the absorption of liquid, whereas the upper region 144, which is above it, is intended for the reception of gases.
  • a line 146 is connected, which is provided with a shut-off element 148.
  • the gas line 28 is connected to the upper region 144 of the further separating container 136 with the interposition of a gas conveyor or compressor 150. Downstream of the compressor 150, the line 152 is also connected to the gas line 28, through which excess gas is removed and supplied to consumers, for example for space heating. The consumers are not shown in Fig. 1.
  • gas which serves here as a fluidizing gas
  • gas line 28 flows from the gas line 28 through the fluidizing gas lines 24 into the pyrolysis reactor 10.
  • the fine-grained fluidizing medium present there preferably sand with a grain size of less than 0.5 mm, is swirled and the fluidized bed is formed 18.
  • the mass flow of gas, which is required for the production of the fluidized bed is adjusted by the control and shut-off device 26.
  • gas, which serves as heating gas is supplied to the heating tube 30 through line 32 and combustion air through line 36, and the heating tube is heated by gas combustion to such an extent that it is able to raise the fluidized bed 18 to a temperature of 400 to 1000 ° Celsius, preferably 600 to 900 ° Celsius.
  • the exhaust gas emerging from the heating pipe is discharged through the exhaust pipe 38, preferably to a chimney, not shown.
  • the heating power of the heating tube is set by the control and shut-off device 34, with which the gas supply can be regulated.
  • the waste material with a piece size of appropriately approximately a maximum of 10 cm is introduced through the feed line 22 into the lower region of the fluidized bed and there thermally decomposed in a reducing atmosphere, i.e. in the absence of oxygen.
  • the combustible pyrolysis gases formed in this way collect in the gas space 20 of the pyrolysis reactor 10, whereas the pyrolysis residue is discharged through the discharge line 16 from the pyrolysis reactor.
  • the pyrolysis gas flows from the gas space 20 through the line 42 to the cooling stage 46, solid particles carried by the pyrolysis gas being separated off in the cyclone separator 44.
  • the pyrolysis gas enters the standing cooler 48 at the top and is cooled by the cooling coil 48.
  • cooling coil 52 is supplied with cooling water through line 54, which is discharged through line 56 after the heat absorption.
  • a three-way mixing valve 58 is installed in line 54 and is connected to line 56 via line 60. The three-way mixing valve adjusts the temperature and the inflow of the cooling water to the cooling coil so that the gaseous benzene contained in the pyrolysis gas and the higher-boiling gaseous constituents condense and are separated off as a liquid fraction.
  • the boiling point of the benzene at ambient pressure is 80 ° Celsius
  • the pyrolysis gas must therefore be cooled in the cooler 48 to a temperature of approximately 75 to 79 ° Celsius.
  • a temperature sensor 62 is arranged in the cooler 48 below the cooling coil 52, which acts on the three-way mixing valve 58 through the control line 64.
  • the three-way mixing valve is adjusted such that a cooling water flow is established in the cooling coil 52, which achieves the desired cooling.
  • the benzene condense in the cooler 48 but also those components of the pyrolysis gas condense, whose boiling points are higher than that of benzene.
  • the toluene contained in the pyrolysis gas condenses, which has a boiling point of approximately 111 ° Celsius.
  • the condensation in cooling stage 46 takes place at ambient pressure.
  • the control and shut-off device 72 is set in such a way that part of the benzene-containing liquid fraction is always contained in the liquid space 66 and gas transfer from the upper region 74 of the evaporation container to the free space 68 of the separating container is thus avoided.
  • a heating coil 80 is provided, which is connected to the water boiler 86 through the feed line 82 and the return line 84. This boiler is heated by a schematically indicated gas burner 98, which is supplied with heating gas from the gas line 28 through the line 100 with the shut-off and control element 102 inserted.
  • the exhaust gas is released to the environment through the exhaust pipe 104.
  • the three-way mixing valve 88 is arranged in the flow line 82 and is connected to the temperature sensor 92 by the control line 74.
  • This temperature sensor 92 is arranged in the lower region 78 of the evaporation container 76 and regulates the mass flow and the temperature of the heating water in the heating coil 80.
  • the control is set here so that the benzene-containing liquid fraction collected in the lower region 78 so it is heated to such an extent that the benzene and the toluene are expelled in gaseous form and a gas mixture containing benzene and toluene is formed which collects in the upper region 74.
  • the benzene-containing liquid fraction is heated at ambient pressure to a temperature above 111 ° C., preferably from 120 to 140 ° C.
  • the gas mixture is fed through line 108 to the compressor 110.
  • the gas fraction accumulating in the cooler 48 and remaining after the recovery of the benzene-containing liquid fraction flows to the compressor 110 and mixes with the gas mixture containing benzene and toluene, so that a total gas flow is produced.
  • This total gas flow is introduced through line 112 into the container 118 below and flows through the zeolitic catalyst upwards.
  • the container 114 and thus the catalyst 116 is heated by the schematically indicated gas burner 122, which is supplied with heating gas from the gas line 28 through the line 124 and the control and shut-off device 126.
  • the catalyst is heated to a temperature of preferably 350 to 410 ° Celsius by the flue gases flowing in the space 118 to the exhaust pipe 128.
  • the cross section of the container and thus of the fixed catalyst bed is selected so that the gas flowing through remains in contact with the catalyst for 0.3 to 2 seconds, preferably 0.7 to 1.5 seconds.
  • the gaseous olefins present in the gas fraction react with the gaseous benzene and toluene to form gaseous products which are obtained as a liquid fraction when cooled. This reduces the proportion of the gas fraction in favor of the liquid fraction.
  • the catalytically treated which emerges from the container 114 is treated Total gas flow through line 130 to the further cooling stage 132 and introduced into the standing cooler 134 above.
  • the cooling coil 138 installed there which is supplied with cooling water or cooling brine through the lines 144, cools the catalytically treated total gas stream to a temperature of 20 to 60 ° Celsius.
  • the pyrolysis oil which condenses in this case forms the liquid fraction and, together with the remaining gas, which represents the residual gas fraction, flows downward to the standing, further separation container 136.
  • the liquid fraction collects in the lower region 142, the residual gas fraction is in the upper region 144 of the further separation container 136 available.
  • the liquid fraction is drawn off from the further separating container and processed further through line 146, the combustible residual gas fraction is fed to the compressor 150 and conveyed into the gas line 28.
  • the residual gas fraction is fed to the gas burners as heating gas and to the pyrolysis reactor as fluidizing gas.
  • the remaining gas not required in the system is fed through line 152 to other consumers, which are not shown in FIG. 1.
  • FIG. 2 shows an embodiment variant of the pyrolyzer according to FIG. 1.
  • the difference compared to Fig. 1 is that the cooling stage is designed differently and the boiler 86 and the associated evaporation tank 76 are missing.
  • components of FIG. 1 that appear in identical form in FIG. 2 are provided with reference numerals that are expanded by the amount 200 compared to the reference numerals in FIG. 1.
  • the system according to FIG. 2 has a cooling stage 246, which has a standing cooler 248.
  • a cooling coil 252 is provided in the cooler, just like that Cooling coil 52 of FIG. 1 can be supplied with cooling water.
  • a separating container 250 is connected to the lower end of the cooler 248, the lower space of which serves as the liquid space 266, whereas the free space 268 remaining above is provided for the reception of gas.
  • a line 306 leads from the free space 268 to the container 314 which contains the zeolitic catalyst, a compressor 310 or a gas conveyor being switched on in line 306.
  • the three-way mixing valve 258 provided in line 254 is connected to a measuring and regulating device 156 for control by the control line 154 shown in dashed lines.
  • This measuring and control device records the molar ratio of the C2 and C3 olefins to the C6 and C7 aromatics of the particular gas fraction present in the free space 268.
  • gas is removed through line 155 from the free space 268 with the aid of a gas pump (not shown), preferably a compressor, passed through the measuring and control device and then again through line 158 to the free space 268, or better the line 306 upstream of the Compressor 310 supplied so that a continuous gas flow through the measuring and control device 156 is maintained.
  • the measuring and control device is now designed so that the three-way mixing valve 258 and thus the cooling capacity of the cooler 248 is set in such a way that the particular gas fraction obtained in the free space has a molar ratio of approximately 0.8 to 1.2, preferably 1, between the C2 and C3 olefins and the C6 and C7 aromatics.
  • the waste material is fed to the pyrolysis reactor 210 and thermally decomposed in the fluidized bed 218.
  • the resulting pyrolysis gas is made the gas space 220 through the cyclone separator 244 to the upper end of the standing cooler 248, which operates at ambient pressure.
  • the pyrolysis gas is cooled, with a portion of the pyrolysis gas being condensed and collected as pyrolysis oil in the liquid space 266 of the separating container 250. This pyrolysis oil is taken from here for further processing.
  • This pyrolysis gas is called a special gas fraction. In order to obtain the special gas fraction, the pyrolysis gas must be cooled to a temperature above the boiling point of the toluene.
  • the special gas fraction is then fed through line 306 with inserted compressor 310 to container 314, in which zeolitic catalyst 316 is contained as a fixed bed.
  • zeolitic catalyst 316 is contained as a fixed bed.
  • the mode of operation of the zeolitic catalytic converter 316 and the further flow of the gas here are exactly as described in connection with FIG. 1, so that there is no need for further details here.
  • the olefins are converted into saturated C to C-5 hydrocarbons, which are obtained in the downstream further cooling stage 332 as a liquid fraction and are removed from there for further processing will.
  • the process gas steps according to the invention reduce the residual gas fraction in favor of the liquid fraction by 20 to 30% and thus increase the economy of the plant.
  • Fig. 3 shows the detail III of Figures 1 and 2 as a variant.
  • the plant according to FIG. 3 has a standing, circular fluidized bed reactor 160, in which the zeolitic catalyst material 162 forms a fluidized bed 164.
  • the zeolitic catalyst material has a grain size of at most 1 mm and is brought into the fluidized state by a fluidizing gas, preferably a part of the residual gas fraction.
  • the fluidizing gas is removed from the gas line 28 and fed through line 166 with the shut-off and regulating element 168 to the fluidizing gas lines 171, which introduce it into the lower, circular-conical area of the fluidized bed reactor 160.
  • the fluidized bed 164 is supported by gas-fired heating tubes, of which a single heating tube 170 in fig. 3 is drawn, heated indirectly.
  • the heating pipe is supplied with heating gas from the gas line 28 through the line 172 with the control and shut-off element 174 inserted.
  • the combustion air is supplied to the heating pipe through line 176, whereas the exhaust gas flows out through line 178.
  • the catalyst material is introduced through line 180 into the top of the fluidized bed reactor, and the spent catalyst material is withdrawn through line 182 from the lower end of the fluidized bed reactor.
  • the fluidized bed reactor 160 is constructed in exactly the same way as the pyrolysis reactor 10 in FIG. 1. It accordingly has an upper, circular-cylindrical region, which is followed by the circular-conical lower region, which tapers downward.
  • the heating tube 170 is inserted horizontally into the fluidized bed 164 from the outside. A vertical introduction is just as possible.
  • the gas from the cooling stage 46 or 246 is introduced into the fluidized bed 164 through the conduit 184 through the compressor 110 or 310 (see FIGS. 1 and 2).
  • the fluidized bed is generated with the aid of fluidized gas, which is led through line 166 and the sufficiently open control and shut-off device 168 to the fluidized gas lines 171 and enters the lower region of the fluidized bed reactor 160.
  • the gas supplied through line 184 comes into sufficient contact with the zeolitic catalyst material so that the reactions described above take place.
  • the required temperature of the fluidized bed 164 of preferably 350 to 410 ° Celsius is generated by the heating tube 170.
  • the catalytically treated gas mixture or the catalytically treated special gas fraction then flows through line 130 or 330 to further cooling stage 132 or 332 and is further processed there, as described above.
  • the residence time of the gas in the fluidized bed is 0.4 to 1.5 seconds, preferably 0.5 to 1.1 seconds.
  • the catalyst of FIG. 3 designed as a fluidized bed 164 has the advantage that the contacting of the gas with the catalyst material is more intensive.
  • a good contact of the gas, which is fed through line 184 to the fluidized bed reactor 160, with the zeolites of the fluidized bed is also achieved when the gas is used as the fluidizing gas.
  • line 166 is separated from gas line 28 and line 184 from fluidized bed reactor 160, and then line 184 connected to line 166.
  • the gas supplied through line 184 additionally takes on the function of the fluidizing gas. This case is not shown in the drawings.
  • the zeolitic catalyst was placed in a tube 4 mm wide. A free part of the tube located upstream of the catalyst served to bring the gas to the required reaction temperature of 370 ° Celsius.
  • the subsequent pipe section is also heated to 370 ° Celsius and provided with a bed of the powdery, zeolitic catalyst over a length L.
  • the residence time t is the ratio of the reaction zone to the volume velocity of the gas at the reaction temperature T.
  • the dwell time has the dimension of seconds.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Coke Industry (AREA)
EP88120665A 1987-12-23 1988-12-10 Verfahren zum Aufarbeiten von Abfallmaterial Expired - Lifetime EP0321807B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88120665T ATE74617T1 (de) 1987-12-23 1988-12-10 Verfahren zum aufarbeiten von abfallmaterial.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19873743752 DE3743752A1 (de) 1987-12-23 1987-12-23 Verfahren zum aufarbeiten von abfallmaterial
DE3743752 1987-12-23

Publications (3)

Publication Number Publication Date
EP0321807A2 EP0321807A2 (de) 1989-06-28
EP0321807A3 EP0321807A3 (en) 1990-03-07
EP0321807B1 true EP0321807B1 (de) 1992-04-08

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US (1) US4871426A (enrdf_load_stackoverflow)
EP (1) EP0321807B1 (enrdf_load_stackoverflow)
JP (1) JPH01210493A (enrdf_load_stackoverflow)
CN (1) CN1016439B (enrdf_load_stackoverflow)
AT (1) ATE74617T1 (enrdf_load_stackoverflow)
DE (2) DE3743752A1 (enrdf_load_stackoverflow)

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JPH0386791A (ja) * 1989-08-31 1991-04-11 Mobil Oil Corp 低沸点炭化水素油の製造方法
US5504267A (en) * 1992-04-06 1996-04-02 S-P Reclamation, Inc. Resource recovery by catalytic conversion of polymers
US5369215A (en) * 1992-04-06 1994-11-29 S-P Reclamation, Inc. Depolymerization method for resource recovery from polymeric wastes
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DE4311034A1 (de) * 1993-04-03 1994-10-06 Veba Oel Ag Verfahren zur Gewinnung von Chemierohstoffen und Kraftstoffkomponenten aus Alt- oder Abfallkunststoff
DE4418562A1 (de) * 1993-06-29 1995-01-12 Leybold Durferrit Gmbh Verfahren und Vorrichtung zur Behandlung von im wesentlichen aus Kunststoff oder Gummi bestehendem Gut
CN1060203C (zh) * 1995-01-17 2001-01-03 王选玉 用废旧橡胶生产炭黑、液化气、石油油品的方法
DE19517096A1 (de) * 1995-05-10 1996-11-14 Daniel Engelhardt Zeolithkatalysierte Pyrolyse von Kunststoffen
CN1055419C (zh) * 1995-07-04 2000-08-16 张庆祥 废弃塑料芳构化催化剂及其制备方法
JP3402877B2 (ja) * 1995-10-09 2003-05-06 三菱重工業株式会社 廃タイヤからのカーボンブラック製造方法及び装置
JP2002248453A (ja) * 2000-06-16 2002-09-03 Akira Shibata 不要材のリサイクルシステム
US8003833B2 (en) 2003-03-28 2011-08-23 Ab-Cwt, Llc Process for conversion of organic, waste, or low-value materials into useful products
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CN1033830A (zh) 1989-07-12
EP0321807A2 (de) 1989-06-28
DE3869930D1 (de) 1992-05-14
CN1016439B (zh) 1992-04-29
JPH01210493A (ja) 1989-08-24
DE3743752C2 (enrdf_load_stackoverflow) 1990-02-08
US4871426A (en) 1989-10-03
DE3743752A1 (de) 1989-07-13
ATE74617T1 (de) 1992-04-15
EP0321807A3 (en) 1990-03-07

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