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WO2003016435A2 - Condensation sans pression de substances residuelles - Google Patents

Condensation sans pression de substances residuelles Download PDF

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Publication number
WO2003016435A2
WO2003016435A2 PCT/DE2002/002819 DE0202819W WO03016435A2 WO 2003016435 A2 WO2003016435 A2 WO 2003016435A2 DE 0202819 W DE0202819 W DE 0202819W WO 03016435 A2 WO03016435 A2 WO 03016435A2
Authority
WO
WIPO (PCT)
Prior art keywords
container
temperature
oil
product
evaporator
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.)
Ceased
Application number
PCT/DE2002/002819
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German (de)
English (en)
Other versions
WO2003016435A3 (fr
Inventor
Wolfgang Hornig
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Evk-Lux Sa
Original Assignee
Evk-Lux Sa
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Evk-Lux Sa filed Critical Evk-Lux Sa
Priority to BR0205841-3A priority Critical patent/BR0205841A/pt
Priority to JP2003521745A priority patent/JP2004521184A/ja
Priority to HU0400598A priority patent/HUP0400598A3/hu
Priority to AU2002325803A priority patent/AU2002325803A1/en
Publication of WO2003016435A2 publication Critical patent/WO2003016435A2/fr
Priority to NO20031542A priority patent/NO20031542L/no
Publication of WO2003016435A3 publication Critical patent/WO2003016435A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
    • 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
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation

Definitions

  • the aim of the invention is to carry out this process in seconds instead of in the long historical periods and in a form which ensures high product quality despite all impurities and additives, such as foaming agents, of the residues.
  • the process should also be suitable for mineral hydrocarbon products, such as waste oils with the phosphate component as foaming agents, plastics with chlorine and fluorine-containing substances, such as PVC and Teflon, and for the waste greases and complex hydrocarbons, such as distillation residues.
  • mineral hydrocarbon products such as waste oils with the phosphate component as foaming agents, plastics with chlorine and fluorine-containing substances, such as PVC and Teflon, and for the waste greases and complex hydrocarbons, such as distillation residues.
  • the essential object of the present invention is therefore to demonstrate a method in which the residues are converted into a usable form in material form without combustion and gasification.
  • the circulation evaporator 1 has a honeycomb ceramic layer 5 on both sides, which ensures that the combustion chamber burns stably and the heating of the evaporator tubes works optimally due to the increased radiation portion of the heat transfer.
  • the hydrocarbon vaporized with the aid of the splitting action of the calcium-aluminum-silicate added collects in a safety steam container 6. This is designed to be large in order to prevent foams which may arise from foaming agents from entering the product.
  • the non-evaporated parts collect at the bottom of the containment and from there back into the circulation evaporator, which creates a cycle.
  • the two evaporators, the circulation evaporator 1 and the distillation evaporator 2 are connected to a discharge 7 which disposes of the settled solids from the two evaporators 1 and 2.
  • the vaporized substances that condense in the distillation column are discharged via the two product containers .8 and 9.
  • the container 8 is an intermediate product tank for the temporary storage of oils for maintaining the liquid level in the circulation evaporator and the container 9 is the product tank for the storage of the end product.
  • the intermediate product tank 8 is the actual product tank and the product tank 9 is used to extract the water content.
  • the gaseous product from the product tank 9 and the safety container 6 is sucked off into the combustion chamber via the vacuum pumps 10.
  • a stirrer 17 is used to supplement the mobilization of the solid which is being introduced and is formed. Care must be taken to ensure that the amount of solid in the reactor does not become too large in order not to impede the circulation.
  • the solid is conveyed via a discharge screw into a riser pipe which is connected to an entry into the safety container above the liquid level of the circulating liquid. Below this entry is a separating sieve, on which the solid drips and from which the solid is periodically discharged to the outside through an opening and scratches.
  • the low boilers are formed at the upper end of the column and are removed on a line 25.
  • the product arises in the underlying floors and is taken from the lines 26.
  • the distillation column is expediently a bubble tray column.
  • the product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products. This is done by a condenser 27 and a solenoid valve 29. A backwash 30 is activated to lower the product evaporation temperature. At the end of the condenser 27, a vacuum line 28 is attached, which opens into the product container 9.
  • the values to be set as the mean boiling point of the product hood are 270 ° C for diesel oil, 280 ° C heating oil, 250 ° C kerosene and 160 ° C for petrol in the case of high aromatics.
  • the input substances which are introduced into the system at the entry 20 via a metering are the residual substances 35, a catalyst 36 and the lime 37.
  • the catalyst is introduced in the form of a fine powder in order to be homogeneously suspended in the circulation evaporator.
  • Sodium aluminum silicate is used instead of calcium magnesium silicate.
  • the lime then converts this sodium aluminum silicate into calcium silicate by ion exchange. This makes the calcium-magnesium silicate the effective substance even when sodium magnesium silicate is input.
  • the still liquid components are released in a high-speed cyclone 38.
  • This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle.
  • the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and an expanding part with a 6 ° extension from a 3 to 6 -fold diameter.
  • the stabilized flow separates the liquids much better.
  • the oil components pressed out at the discharge are pumped back into the safety container 6 by a heavy oil pump 39.
  • the oil pumped by the heavy oil pump 39 serves, like the oil from the intermediate product container 9, to maintain the liquid level in the circulation evaporator 1, the liquid circulation of which and therefore reliable operation depends on it, that the circulation of the oil between the circulation evaporator and the safety container is maintained with a sufficient liquid level.
  • the solids deposited in the evaporators at the lower end of the evaporators are discharged via flaps or metering screws, the solenoid valves 40.
  • the signals for this are given by the thermocouples 43 which, in the case of deposits at the lower end, bring about the lowering of the temperature compared to the evaporator contents as a signal for the discharge. So if solids settle, they ensure a temperature reduction on the thermocouple compared to the circulating liquid. If this temperature drop has exceeded a value, the discharge is activated until the value falls below again. This automates the periodic, continuous discharge.
  • the temperature sensor in the circulation evaporator above the tube bundle increases the amount of catalyst with increasing temperature, since the reaction is then increased and the temperature is lowered.
  • the additional burner is started.
  • the vacuum pump has reached a sufficient speed, i.e. the required minimum speed for the gas supply has been reached, the start burner is switched off. If the temperature then drops, the vacuum is increased and only when the temperature drops further does the burner again ignited.
  • the amount of entry that cools the system is increased.
  • the temperature is controlled with the amount of the entry.
  • the amount of gas to the burner is reduced by metered opening of the gas flow to the torch.
  • An energy supply can also result from the suction of the water vapor generated in the safety container.
  • the water vapor and low boiler components that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at a water separator 44 and are introduced into the combustion chamber in a dried state by the liquid components via the high-speed cyclone 38.
  • the vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum.
  • the amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas, based on the input material or the product, is generated.
  • the control ensures that the gas volume is always adapted to the energy requirements of the system.
  • a safety line 46 to the torch is therefore only open in the event of a sudden overproduction.
  • the evaporator tubes in the rear part are equipped with ribs, coated with a metal sponge or with an improved flow with the flame deflection plates 47. These baffles increase the flue gas path and thus ensure better heat transfer to the evaporators.
  • FIG. 2 shows the inventive device.
  • a circulation evaporator 51 consists of a cylindrical container with a tube bundle. The tubes seen in the direction of the flames are not finned. The pipes lying to the rear in the radiation shadow of the pipes have ribs, surface-enlarging structures, such as foam metal casting or baffle plates.
  • the circulation evaporator 51 has collecting chambers below and above the tubes, which are connected to an adjacent safety steam container 56 with tubes and thus form a circuit.
  • distillation evaporator 52 To the right of the circulation evaporator 51 is a distillation evaporator 52 connected downstream on the flue gas side, via which the distillation column is arranged. To the left is the starting burner in the form of an oil burner 53, which is mounted on a ceramic-lined combustion chamber 54. The gas line, which is connected to the vacuum pumps 60, opens into this.
  • the burner 53 has a separate circuit for the air and the oil supply, which is temporarily blocked during operation, while the combustion air fan is always switched on during operation.
  • the circulation evaporator 51 has a honeycomb ceramic layer on both sides, which is constructed from honeycomb ceramic blocks of 50 to 100 mm in thickness.
  • the material is preferably magnesium aluminum silicate (cordierite).
  • the safety steam container 56 is arranged above the oil burner 53.
  • the two evaporators, the circulation evaporator 51 and the distillation evaporator 52 are connected to a discharge 57 which is arranged underneath. It is connected to the two evaporators 51 and 52.
  • the distillation column which preferably consists of a bubble cap column. This has outlets on the floors, which are connected to pipes and drainage containers. These are the two product containers 58 and 59.
  • the solids discharge is carried out by a screw press 61 with a press cylinder 62.
  • the conically tapered press cylinder 62 increases the solids concentration by squeezing oil.
  • the safety technology for the handling of such a system with combustible oil is ensured by a control technology and in the event of an accident via a pressurized water extinguishing tank 63 with the contents of the extinguishing water 64 and the compressed air 65 located above it.
  • extinguishing with the pressurized water 64 causes the groundwater to become contaminated an extinguishing water retention basin 66 prevented.
  • a stirrer 67 is used to supplement the mobilization of the solid that is being formed and is formed. This is arranged on the circulation evaporator in such a way that the stirrer protrudes through one of the pipes to below the pipes and thus reaches the liquid below the pipes.
  • the solid that is then discharged is conveyed into a discharge screw 68 after a pressing screw 62 and is further dried there by indirect heating. From there, the expelled oil vapor reaches the safety container.
  • An entry screw 69 is also located in the chimney or exhaust pipe arranged at the end. It has a double wall, in the intermediate wall the flue gas is guided separately from the contents of the screw.
  • the screw has a connecting line to an entry 70.
  • the flue gas line merges into a flue gas pipe 71.
  • a foam brake 73 is arranged in the distillation evaporator 52. It consists of sieves or metallic sponge castings arranged one above the other and is located below a distillation column 74. In the distillation zone 74, the low boiler fraction is removed via a line 75. The product arises in the underlying floors and is removed from the lines 76 by connecting the raw line attached to the floor to the product container.
  • the condenser receives its cooling water through a cooling water inlet 81. In countercurrent, the cooling water passes through the condenser and then passes into a cooling water outlet 82. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas passes through a pressure relief valve 83 in the torch.
  • the input material input 70 is connected via a metering to the input of the residual materials 85, a catalyst 86 and the lime 87.
  • the residual material contains hydrocarbons and has the form of animal meal, fat, waste oils, vacuum residue, plastics, wood meal or rubber.
  • the catalyst is entered in the form of a fine powder and has the chemical structure of powdered calcium magnesium silicate or sodium aluminum silicate. This sodium-aluminum-silicate is then converted into calcium-magnesium-silicate by ion exchange. This makes the calcium-magnesium silicate the effective substance even when sodium magnesium silicate is input.
  • This conversion is always given, in particular when using plastic waste, since the PVC contained in the plastic waste removes the catalyst from the catalyst by ion exchange by salt formation or replaces it with hydrogen.
  • the catalyst will then always take the form of calcium magnesium silicate and act as an active substance.
  • the lime is dosed via the pH measurement in the gas after the vacuum pump by switching the dosing on until the pH drops again until pH 7 is reached again. Soda or caustic soda can be used instead of lime.
  • the burner gas line is connected to a high-speed cyclone 88. This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle.
  • the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and a widening part with a 6 ° widening and a 3 to 6 -fold diameter.
  • the stabilized flow separates the liquids much better.
  • a heavy oil pump 89 is arranged in the discharge 57 and is connected to the safety container 56.
  • a connecting line is also arranged between the intermediate product container 59 and the circulation evaporator 51.
  • the circulation evaporator 51 is a hard-to-evaporate water-poor oil, a kind of thermal oil, as it is used for the heat exchanger with thermal oil.
  • the solids deposited in the evaporators at the lower end of the evaporators are discharged via flaps or metering screws, the solenoid valves 90. These are electronically connected to the thermocouples 93 via a controller in the electronics and the frequency-converted motor of the flaps.
  • the heavy oil connection lines from the intermediate product container 59, residual oil container and the heavy oil pump 89 are given by a float switch 91 in the safety container.
  • the signal for the addition of the lime 87 is given by a pH sensor 92 in the vacuum line.
  • the signals for the temperature controls are given by the temperature and measuring sensors 93. In this way, they not only control the flaps on the discharge, but also the elements of the system's heat generation and the amount of catalyst added.
  • the amount of entry that cools the system is increased. With the The amount of the entry is controlled by the temperature. In the event of a further increase, the amount of gas to the burner is reduced by metered opening of the gas flow to the torch.
  • An energy supply can also result from the suction of the water vapor generated in the safety container. The water vapor and low boiler parts that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at a water separator 94 and are dried and introduced into the combustion chamber by the liquid parts via the high-speed cyclone 88.
  • the vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum.
  • the amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas is generated, based on the input material or the product.
  • the safety line is connected outside the building with an overpressure pot, which is designed as a cyclone. At the bottom of this pot there is a liquid separator and condensate container.
  • the gas discharge of the overpressure pot may be designed as a torch. To do this, an ignition device must be installed depending on the flow switch.
  • a circulation evaporator 1 has a volume of 500 liters and the distillation evaporator 2 located next to it also has 500 liters.
  • the evaporator contains 100 tubes with a diameter of 2 inches and fins with a thickness of 2 cm.
  • the first 3 rows of pipes facing the burner have no fins.
  • the start burner in the form of oil burner 3, with an output of 200 kW, is used to reach the reaction temperature of 390 ° C, in which the oil produced for the starting process is burned. This takes place in the combustion chamber 4 with a volume of 100 liters, which in the operating state is heated with the gas from the vacuum pumps 10 with a maximum output of 16 m 3 / h at 0.2 bar negative pressure. In the operating state, there is no operation from the burner 3, which only supplies the combustion air of 200 m 3 / h during operation.
  • the circulation evaporator 1 has a honeycomb ceramic layer 5 of 4 x 4 honeycombs 100 mm thick and 150 x 150 mm surface on both sides, which ensures that the combustion chamber burns stably and the heating of the evaporator tubes works optimally due to the increased radiation portion of the heat transfer.
  • the hydrocarbon vaporized with the aid of the splitting action of the calcium-aluminum silicate added collects in the safety steam container 6 with a volume of 5 m 3 .
  • the non-evaporated parts collect at the bottom of the safety container and are separated in a hydrocyclone on the underside under the safety container and from there they get back into the circulation evaporator via a liquid and sludge separator container with a volume of 500 l and a connecting pipe with DN 200 forms a cycle.
  • the two evaporators, the circulation evaporator 1 and the distillation evaporator 2 are connected to the discharge 7 with a content of 0.5 m 3 , which disposes of the settled solids from the two evaporators 1 and 2.
  • the container 8 is an intermediate product tank for the temporary storage of oils for maintaining the liquid level in the circulation evaporator and the container 9 is the product tank for the storage of the end product.
  • the intermediate product tank 8 is the actual product tank and the product tank 9 is used to extract the water component.
  • the gaseous product from the product tank 9 and the safety container 6 is sucked off into the combustion chamber via the vacuum pumps 10.
  • the right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment.
  • the safety technology for the handling of such a system with combustible oil is guaranteed by a control technology and in the event of an accident via the pressurized water extinguishing container 13 with a total content of 10 m 3 with the contents of the extinguishing water 14 and the compressed air 15 above With the extinguishing water 14, the amount of extinguishing water is collected below the system, thus preventing the groundwater from being contaminated by the extinguishing water retention basin 16 with a total volume of 20 m 3 .
  • the flue gases cooled in this way reach the outside through the flue gas pipe 21 with a diameter of 250 mm.
  • condensate arises that condenses in the flue gas pipe 21 and is discharged to the outside by the condensate drain with neutralization 22.
  • the flue gas is cooled to 450 ° C in the circulation evaporator stage, to 350 ° C in the distillation evaporator to 250 ° C in the after-dryer and to 150 ° C in the input material dryer.
  • the dryers are provided with additional burners, which ensure the necessary minimum temperature.
  • the product specification is given by the boiling temperature of the respective column section and the trays and thus ensures the control of the products. This is done by the condenser 27 and the solenoid valve 29.
  • the backwash 30 is activated to lower the product evaporation temperature.
  • the vacuum line 28 is attached, which opens into the product container 9.
  • the values to be set as the average boiling point of the product fume cupboard are 270 ° C for diesel oil, since the raw material is plastic with predominantly PE and PP.
  • the condenser has a cooling capacity with water of up to 200 kW. He receives his cooling water through the cooling water inlet 31 with a diameter of 1.5 inches. In countercurrent, the cooling water passes through the condenser and then reaches the cooling water outlet 32. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas reaches the torch via a pressure relief valve 33.
  • the pressurized water openings for a water flow rate of 100 l / min are also used for 1 and 2 minutes through the extinguishing water pressure nozzles 34.
  • the temperature of the hottest zone of the system is raised to 390 ° C in the event of an accident or critical operating state the uncritical lower ignition temperature has cooled down to below 320 ° C.
  • the input materials which are introduced into the system at entry 20 via a metering are the residual materials 35, the catalyst 36 and the lime 37.
  • the catalyst is introduced in the form of a fine powder in order to. to be present homogeneously suspended in the circulation evaporator. 6 kg / h calcium aluminum silicate are used. 15 kg of lime are added per hour controlled by the pH probe. This means that even if you enter sodium magnesium silicate calcium-magnesium-silicate is the effective substance.
  • a high-speed cyclone 38 This consists of a cyclone, the inlet nozzle of which is extended in the form of a Venturi nozzle. As an extension to the inlet, the nozzle has a narrowing part in which the speed is increased to values of approx. 100 m / s, a parallel part with at least 5 times the diameter and an expanding part with a 6 ° extension and a 3 to 6 -fold diameter. The stabilized flow separates the liquids much better.
  • the cyclone has a diameter of 300 mm and a narrowest diameter in the venturi inlet of 15 x 25 mm.
  • the oil components pressed out at the discharge are pumped back into the safety container 6 by the heavy oil pump 39 with a pumping capacity of 50 l / h. They serve, like the oil from the intermediate product container 9, to maintain the liquid level in the circulation evaporator 1, the liquid circulation of which and therefore reliable operation depends on the circulation of the oil between the circulation evaporator and the safety container being maintained with a sufficient liquid level.
  • Heavy oils are important in the cycle, since the reaction should take place with the substances entered and not with the circulating liquid. These should be largely preserved in order to maintain the liquid cycle.
  • the system is therefore being started for the first time with a hard-to-evaporate water-poor oil, a type of thermal oil, as is used for heat exchangers with thermal oil.
  • thermal oil a type of thermal oil, as is used for heat exchangers with thermal oil.
  • These oils are continually supplemented by the more difficult-to-split fractions of the feedstocks, such as the asphaltenes of the residual oils, which, however, are also split at elevated catalyst temperatures.
  • the solids deposited in the evaporators are discharged at the lower end of the evaporators via flaps or metering screws with a diameter of 25 mm, the solenoid valves 40.
  • the signals for this are given by the thermocouples 43 which, in the case of deposits at the lower end, bring about the lowering of the temperature compared to the evaporator contents as a signal for the discharge.
  • thermocouple compared to the circulating liquid. If this temperature drop has exceeded a value, the discharge is activated until the value falls below it again. This automates the periodic, continuous discharge.
  • the supply of the heavy oils from the intermediate product container 9, additional waste oil containers for waste oils and waste oils to be processed and the heavy oil pump 39 is given by the float switch 41 in the safety container. If the required liquid level drops below a value, the oils are added until the level is reached again.
  • the signal for the addition of lime 36 is given by the pH sensor 42 in the vacuum line.
  • the signals for the temperature controls are given by the temperature and measuring sensors 43. Not only are these used to control the flaps on the discharge, but the temperature sensors also serve as measuring sensors for the elements of the system's heat generation and the quantity of the added catalyst quantity.
  • the temperature sensor in the circulation evaporator above the tube bundle increases the amount of catalyst with increasing temperature, since the reaction is then increased and the temperature is lowered.
  • the auxiliary burner is started. After reaching the reaction temperature and at a sufficient speed of the vacuum pump, d. H. the required minimum speed of the vacuum pump for the gas supply is reached, the start burner is switched off. When the temperature drops, the vacuum is increased and only when the temperature drops further, the burner is ignited again.
  • the limit temperature for the self-sufficiency of the reaction with the gas is 410 ° C with this feed.
  • the temperature in the containment then being about 100 ° C. lower than in the circulation evaporator.
  • the temperature is controlled with the amount of the entry.
  • the amount of gas to the burner is reduced by metered opening of the gas flow to the torch.
  • An energy supply can also result from the suction of the water vapor generated in the safety container.
  • the water vapor and low boiler parts which occur when the entry is wet at lower temperatures are discharged at the upper end of the safety container at the water separator 44 and, after being dried, are introduced into the combustion chamber via the high-speed cyclone 38.
  • the hydrocyclone with a tangential inflow pipe opening of DN 150 is located below the safety steam container and at the lower end of the safety steam container is a liquid container with a diameter of 600 mm and a height of 1 m. In the upper part there is a connection line from DN 250 to the circulation evaporator.
  • distillation evaporator 52 To the right of the circulation evaporator is the distillation evaporator 52 connected downstream on the flue gas side, via which the distillation zone is arranged.
  • the gas line with a 2.5 inch diameter and a vacuum pump 60 with 16 m 3 / h gas suction capacity at 0.2 bar negative pressure opens into this.
  • the burner 53 has a separate circuit for the air of 200 m 3 / h and the oil supply of 20 l / h, which is temporarily blocked during operation, while the combustion air fan is always switched on during operation.
  • the circulation evaporator 51 has a honeycomb ceramic layer on both sides, which is constructed from honeycomb ceramic blocks of 50 to 100 mm in thickness.
  • the honeycombs are 4 x 4 honeycombs with a cross-sectional area of 150 x 150 mm.
  • the material is preferably magnesium Aluminum silicate (cordierite).
  • a safety steam container 56 with a diameter of 2 m and a height of 3 m is arranged above the burner 53. This is large and has foam-reducing fittings. It has the connecting lines to the circulation evaporator 51 and forms a liquid circuit with it.
  • the two evaporators, the circulation evaporator 51 and the distillation evaporator 52, both of which are of identical design, are connected to the discharge 57, which is arranged underneath. It is connected to the two evaporators 51 and 52.
  • the distillation column which consists of a bubble-cap column with a diameter of 400 mm, the base distance of 300 mm and 6 x 5 shots, ie. H. 6 floors are processed per shot. This has outlets on the floors, which are connected to pipes and drainage containers.
  • the container 58 is an intermediate product tank, preferably a cylindrical unpressurized container, which is approved for the storage of oils. It is connected to the safety steam tank by a line and a feed pump with a capacity of 1000 l / h, which is switched via the level switch.
  • the container 59 is the product tank for storing the final product, i. H. the product containers are connected to different lines.
  • the intermediate product container 58 is connected to the safety container via a pump at 500 l / h.
  • the product container 58 is connected to the consumer or a tank.
  • the intermediate product tank 58 is the actual product tank and the product tank 59 is used to extract the water content.
  • the gaseous product from the product tank 59 and the safety container 56 is sucked off into the combustion chamber via the vacuum pumps 60.
  • the right-hand vacuum pump only switches on in the event that the temperature in the safety container at the suction point drops due to the formation of water vapor. This removes water vapor from the atmosphere in the containment.
  • the agitator 67 serves to supplement the mobilization of the solid which is being formed and is formed. This is arranged on the circulation evaporator in such a way that the agitator projects through one of the tubes to below the tubes and thus reaches the liquid below the tubes.
  • the solid that is then discharged is conveyed into the discharge screw 68 after the extrusion screw 62 and is further dried there by indirect heating. From there, the expelled oil vapor reaches the safety container.
  • the feed screw 69 with a diameter of 250 mm. It has a double wall with a 50 mm cavity.
  • the flue gas is guided in the partition wall separately from the screw content.
  • the screw has a connecting line to the entry 70.
  • the flue gas line merges into the flue gas pipe 71.
  • the condensate drain with neutralization 72 with a condensate drain to the outside.
  • the foam brake 73 is arranged in the distillation evaporator 52. It consists of 6 sieves arranged one above the other and is located below the distillation zone 74. In the distillation zone 74, the low boiler fraction is removed via line 75 with a 1 inch diameter. The product arises in the underlying floors and is removed from the lines 76 by connecting the raw line attached to the floor to the product container.
  • the condenser with 20 cooling water pipes with 1 inch diameter and a cooling capacity of Its cooling water receives 200 kW through the cooling water inlet 81.
  • the cooling water passes through the condenser and then passes into the cooling water outlet 82. If, despite the cooling and the vacuum pump, the pressure of the system rises above a set value, the excess gas passes through a pressure relief valve 83 in the torch.
  • the extinguishing water pressure nozzles 84 are also connected to solenoid valves which are electrically connected to flame and flue gas detectors and receive their opening impulse from there.
  • the temperature of the hottest zone of the system is cooled from 390 ° C to the uncritical lower ignition temperature of below 320 ° C.
  • the input material input 70 with a capacity of 600 kg / h plastic is connected via a metering with the input of the residual materials 85, the catalyst 86 with 6 kg / h and the lime 87 with 15 kg / h.
  • the residue contains hydrocarbons and is in the form of plastics.
  • the catalyst is entered in the form of a fine powder and has the chemical structure of powdered calcium magnesium silicate.
  • the burner gas line is connected to a high-speed cyclone 88.
  • This consists of a cyclone with a diameter of 300 mm, the inlet nozzle of which is extended in the form of a Venturi nozzle.
  • the nozzle has a constricting part at a height of 15 x 25 mm, a parallel part with a length of 75 mm and an expanding part with a 6 ° extension of 60 mm length. The stabilized flow separates the liquids much better.
  • the heavy oil pump 89 with a delivery capacity of 100 l / h which is connected to the safety container 56, is arranged in the discharge 57.
  • a connecting line is also arranged between the intermediate product container 59 and the circulation evaporator 51.
  • the circulation evaporator 51 is a hard-to-evaporate water-poor oil, a kind of thermal oil, as it is used for the heat exchanger with thermal oil.
  • the solids deposited in the evaporators are discharged at the lower end of the evaporators via flaps or metering screws with a diameter of 250 mm, the solenoid valves 90. These are electronically connected to the thermocouples 93 via a controller in the electronics and the frequency-converted motor of the flaps.
  • the signals for the temperature controls are given by the temperature and measuring sensors 93. In this way, they not only control the flaps on the discharge, but also the elements of the system's heat generation and the amount of catalyst added.
  • the temperature sensor in the circulation evaporator above the tube bundle is electrically interconnected with the metering device for the amount of catalyst. As the temperature rises, the dosing device is regulated for larger additions. When the temperature drops, the auxiliary burner is started. If it reaches the reaction temperature and the vacuum pump reaches the minimum speed required for the gas supply, it switches off. When the temperature drops, the vacuum is increased and only when the temperature drops further, the burner is ignited again.
  • the amount of entry that cools the system is increased.
  • the temperature is controlled with the amount of the entry.
  • the amount of gas to the burner is reduced by metered opening of the gas flow to the torch.
  • An energy supply can also result from the suction of the water vapor generated in the safety container.
  • the water vapor and low boiler parts that occur when the temperature is wet at lower temperatures are discharged at the upper end of the safety container at the water separator 94 and, after being dried, are introduced into the combustion chamber by the high-speed cyclone 88 via the high-speed cyclone.
  • the vacuum pump connected to this circuit is separated by a solenoid valve during the non-operation phase in order not to endanger the vacuum.
  • the amount of gas in the total amount of product is approximately 3 to 7% in terms of energy. On average, 4.5% gas is generated, based on the input material or the product.

Landscapes

  • 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)
  • Processing Of Solid Wastes (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Catalysts (AREA)

Abstract

La présente invention concerne un procédé et un dispositif pour condenser sans pression des substances résiduelles contenant des hydrocarbures, qui décrivent le processus de formation de pétrole avec des catalyseurs similaires dans la plage de température allant de 330 à 430 °C. Selon cette invention, les additifs assurent également, outre le craquage, la désintoxication et la stabilisation des huiles résultantes. La qualité des produits résultant de plastique, d'huiles usées, de produits et de graisses animaux et d'autres substances contenant des hydrocarbures est similaire aux combustibles et ces produits sont purs et exempts d'agents toxiques.
PCT/DE2002/002819 2001-08-06 2002-08-01 Condensation sans pression de substances residuelles Ceased WO2003016435A2 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
BR0205841-3A BR0205841A (pt) 2001-08-06 2002-08-01 Liquefação sem pressão de resìduos
JP2003521745A JP2004521184A (ja) 2001-08-06 2002-08-01 残留物の常圧での液化処理
HU0400598A HUP0400598A3 (en) 2001-08-06 2002-08-01 Unpressurized liquefaction of residues
AU2002325803A AU2002325803A1 (en) 2001-08-06 2002-08-01 Unpressurized liquefaction of residues
NO20031542A NO20031542L (no) 2001-08-06 2003-04-04 Trykklös kondensering av reststoffer

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10138518.8 2001-08-06
DE10138518A DE10138518A1 (de) 2001-08-06 2001-08-06 Drucklose Verflüssigung von Reststoffen

Publications (2)

Publication Number Publication Date
WO2003016435A2 true WO2003016435A2 (fr) 2003-02-27
WO2003016435A3 WO2003016435A3 (fr) 2003-04-24

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/DE2002/002819 Ceased WO2003016435A2 (fr) 2001-08-06 2002-08-01 Condensation sans pression de substances residuelles

Country Status (7)

Country Link
JP (1) JP2004521184A (fr)
AU (1) AU2002325803A1 (fr)
BR (1) BR0205841A (fr)
DE (1) DE10138518A1 (fr)
HU (1) HUP0400598A3 (fr)
NO (1) NO20031542L (fr)
WO (1) WO2003016435A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004092305A1 (fr) * 2003-04-14 2004-10-28 Hornig, Wolfgang Procede et dispositif de traitement catalytique de residus dans des reacteurs tubulaires chauffes et purifies en continu

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10327059B4 (de) * 2003-06-16 2005-12-22 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zum Konvertieren von fett- oder ölhaltigen Roh- und Abfallstoffen in Gemische mit hohem Kohlenwasserstoffanteil, mit diesem Verfahren hergestellte Produkte und deren Verwendung
DE102008047563A1 (de) * 2008-09-16 2010-04-15 Zeppelin Silos & Systems Gmbh Verfahren und Vorrichtung zur Aufbereitung von kunststoffhaltigen Stoffen
RU2019140309A (ru) * 2017-06-13 2021-06-09 ТиДжиИ АйПи ЛЛК Способ и устройство для каталитической безнапорной деполимеризации углеводородсодержащих веществ
US10953381B1 (en) 2020-03-24 2021-03-23 Tge Ip Llc Chemical reactor with high speed rotary mixing, for catalytic thermal conversion of organic materials into diesel and other liquid fuels, and applications thereof

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Publication number Priority date Publication date Assignee Title
CA1093102A (fr) * 1976-05-20 1981-01-06 Bernhard G. Habicht Methode et appareil de transformation des dechets d'hydrates de carbone
DE4114434C2 (de) * 1991-05-03 1994-12-22 Rwe Entsorgung Ag Verfahren zur Herstellung von pumpbaren Gemischen durch thermische Behandlung synthetischer, organischer Abfälle unter Verminderug der Koksbildung
JPH0823021B2 (ja) * 1992-06-16 1996-03-06 東洋製罐株式会社 プラスチックの化学的再利用方法
JPH1072587A (ja) * 1996-05-10 1998-03-17 Mitsui Sekitan Ekika Kk 廃プラスチックスの処理方法
JPH1150062A (ja) * 1997-07-30 1999-02-23 Chiyoda Corp プラスチック廃棄物の処理方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004092305A1 (fr) * 2003-04-14 2004-10-28 Hornig, Wolfgang Procede et dispositif de traitement catalytique de residus dans des reacteurs tubulaires chauffes et purifies en continu

Also Published As

Publication number Publication date
BR0205841A (pt) 2003-10-21
JP2004521184A (ja) 2004-07-15
HUP0400598A2 (hu) 2004-06-28
AU2002325803A1 (en) 2003-03-03
WO2003016435A3 (fr) 2003-04-24
NO20031542D0 (no) 2003-04-04
HUP0400598A3 (en) 2005-02-28
DE10138518A1 (de) 2003-02-20
NO20031542L (no) 2003-06-05

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