EP0879273B1 - Verfahren und vorrichtung zur aufarbeitung von altöl - Google Patents

Verfahren und vorrichtung zur aufarbeitung von altöl Download PDF

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EP0879273B1
EP0879273B1 EP97900905A EP97900905A EP0879273B1 EP 0879273 B1 EP0879273 B1 EP 0879273B1 EP 97900905 A EP97900905 A EP 97900905A EP 97900905 A EP97900905 A EP 97900905A EP 0879273 B1 EP0879273 B1 EP 0879273B1
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EP
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Prior art keywords
waste oil
temperature
mixture
feed mixture
volatile components
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EP97900905A
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English (en)
French (fr)
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EP0879273A1 (de
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Heshui Yu
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • 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

Definitions

  • This invention relates to a process and apparatus for reclaiming waste oils from various sources.
  • Used oil represents a major environmental problem.
  • the U.S. Environmental Protection Agency estimated that of the 4.9 million cubic meters (1.3 billion gallons) of used oil produced annually in the United States, only about 2% was being re-refined, despite the existence of a large number of physical and chemical processes developed for reclaiming or re-refining industrial and automotive lubricants. The remainder of the waste oil, presumably, was being dumped or discarded into the environment in various ways.
  • Sulfuric acid acts as an extraction medium for the removal of unsaturates, dirt, additives and colored materials from the waste oil.
  • the clay is used as an adsorbent to remove impurities.
  • large quantities of spent acid sludge and clay are produced and must be disposed of as a process waste.
  • U.S. Patent No. 5,271,808 discloses a process for reclaiming waste oil wherein a vessel heater is used. In this process, because a large volume of feedstock is held in a heater vessel under high temperature for a long residence time, undesired polymerization, oxidation and dehydrogenation take place, resulting in the production of an unstable diesel fuel and a large volume of ash cake residue. Additionally, the run length of the process is quite short.
  • DE-A-3,224,114 discloses a process and apparatus for cracking used motor vehicle engine oil by heating with microwaves.
  • the used oil cracks on heating to the distillation point.
  • the volatile products are removed in a condenser.
  • JP-56 082886 discloses a process to suppress local coking and to improve the yield of light oil, by mixing a catalyst with a heavy oil to form a uniform slurry. The slurry is cracked in the liquid phase catalytically.
  • EP-0 308669 discloses processing materials containing halogenated hydrocarbons by pyrolysis in a fluidised bed of basic substance.
  • US-5,143,597 describes a used lubricant oil recycling process in which a used lubricating oil is injected to a delayed coker downstream of the coker furnace whereby the used oil is thermally cracked into hydrocarbon fuel products.
  • An object of the present invention is to overcome some or all of the disadvantages of prior waste cil reclaiming techniques by providing an effective, low cost process and apparatus for reclaiming waste cil.
  • Another object of the present invention is to provide a process for reclaiming waste oil that results in the production of an acceptably stable and valuable #2 diesel fuel or gasoline.
  • Still another object of the invention is to provide a process for reclaiming waste oil that can result in the formation of less residue than any prior process while enabling longer run times between shutdowns.
  • a process for treating waste oil containing heavy hydrocarbons and contaminants which comprises: raising the temperature of a feed mixture of fresh waste oil and a recycled non-volatile residue to a range of 400°C to 490°C (measured at the output of the heating unit) under a pressure of 276 kPa to 1034 kPa (40 to 150 p.s.i.g.) for a period of time from 1 to 15 seconds, preferably 3 to 10 seconds, sufficient to cause pyrolysis of the heavy hydrocarbons contained in the feed mixture, but insufficient to permit substantial undesired polymerization, oxidation and dehydrogenation reactions to take place in the feed mixture; cooling the resulting pyrolyzed waste oil mixture to a temperature in the range of 300°C to 455°C, preferably 300°C to 425°C and most preferably 300°C to 375°C, and maintaining this temperature while allowing volatile components in the pyrolyzed waste oil mixture to evaporate, leaving
  • the process temperature to which the waste oil is heated for pyrolyzation depends on the designed conversion. That is to say, higher temperatures will be used for higher percentage gasoline yields, and lower temperatures for higher percentage diesel oil yields.
  • the temperature of the feed mixture is raised, to above the range of 400°C to 490°C, to promote "deep cracking" of the heavy hydrocarbons, and a resulting pyrolyzed waste oil mixture is then subjected to further cooling, evaporation and mixing steps.
  • the non-volatile residue containing the contaminants is heated to a temperature in the range of 470°C to 590°C for a short time, and is then brought to a temperature in the range of 440°C to 570°C and is maintained at that temperature under a pressure of 21 kPA to 172 kPa (3 to 25 p.s.i.g.) to cause the residue to undergo a further pyrolysis and a coking reaction, creating further volatile components and a solid coke, whereupon the further volatile components are removed and condensed, and the solid coke is collected and discarded.
  • the feed material is mixed with steam before being raised in temperature.
  • an apparatus for treating waste oil containing heavy hydrocarbons and contaminants comprising: a heating unit for raising a temperature of a feed mixture of fresh waste oil and a recycled non-volatile residue to a range of 400°C to 490°C for a time sufficient to cause pyrolysis of the heavy hydrocarbons contained in the feed mixture, depending on the designed conversion of the cylindrical reactor, but insufficient to permit substantial undesired polymerization, oxidation and dehydrogenation reactions to take place in the feed mixture; two substantially identical containers, and pipes and valves allowing said containers to be used alternately, for receiving the resulting pyrolyzed waste oil mixture and for holding and maintaining the pyrolyzed waste oil mixture at a temperature in the range of 300°C to 455°C, preferably 300°C to 425°C, most preferably 300°C to 375°C, while allowing volatile components in the pyrolyzed waste oil mixture to evaporate, leaving a non-volatile residue containing
  • the heating unit conveniently includes at least one heating tube, which may be straight and which may be set in the heating unit in a vertical, oblique or horizontal orientation.
  • the heating of the feed material is preferably carried out in a tubular heating unit capable of operating at a high liquid velocity (e.g. a velocity in the range of about 0.6 m to 4.5 m/s (2 to 15 feet/second), and more preferably 1.2 m to 3.0 m/s (4 to 10 feet/second)), and the pyrolyzed mixture is preferably cooled and the volatile components evaporated in a preferably cylindrical reactor acting as a container mentioned above.
  • the temperature of a cylindrical reactor is controlled by adjusting the volume of preheated feedstock introduced into the cylindrical reactor. Due to a short residence time in the tubular heating unit (i.e. 1 to 30 seconds, preferably 1 to 15 seconds and most preferably 3 to 10 seconds), and relatively low temperatures in the cylindrical reactor, undesired side reactions are minimized.
  • the light fuel vapors with any accompanying steam emanating from a cylindrical reactor are preferably introduced into a heat exchanger to preheat the fresh waste oil feedstock (e.g. to a temperature in the range of 110°C to 150°C).
  • the remainder heavier oil in a cylindrical reactor with fresh waste oil feedstock is pumped into the tubular heating unit again for a second heating and pyrolysis reaction, and this procedure is repeated continuously.
  • high boiling point oil in a cylindrical reactor accumulates to such an extent that process production decreases, the temperature in the tubular heater is increased for deep cracking. After that, the temperature is returned to normal.
  • steam injection into the tubular heater for steam cracking can be used. This improves oil stability and decreases coke formation.
  • the steam may be produced by the tubular heating unit.
  • the preheated feedstock is normally introduced into the upper part of a cylindrical reactor and is sprayed downwardly at the center.
  • the heated pyrolyzed mixture from the heated tubes in the tubular heating unit is introduced near the bottom of a cylindrical reactor.
  • the feedstock lines for the heating tubes are introduced from the bottom of a cylindrical reactor, then pass a pump into the tubular heater.
  • the feedstock from a cylindrical reactor can enter the tubular heater from either the top or the bottom. If desired, the preheated feedstock can be pumped directly to the tubular heater without passing through, or only partially passing through, a cylindrical reactor depending on the temperature of the fluid within the cylindrical reactor.
  • the products generated from reclaiming waste oil using the process and apparatus of the present invention include #2 diesel fuel, gasoline and coke.
  • the process and apparatus can be operated without causing significant waste disposal problems.
  • the process feedstock can be any type of waste oil, such as motor oil, industrial lubricants, vegetable oil, fish oil, industrial oil sludge and spilled waste crude oil.
  • a heat exchange column 14 (more than one such column may be provided, if required), where it flows downwardly and is pre-heated (generally to a temperature in the range of 110°C to 150°C) by heat exchange with product vapor (derived in a manner to be described later).
  • the preheated feedstock is then pumped from the bottom of the heat exchange column 14 via line 16 into a cylindrical reactor 18 which forms a container for receiving and holding a pyrolyzed waste oil mixture from a tubular heating unit 20.
  • the pyrolyzed mixture is held within the reactor 18 at a predetermined temperature within the range of 300°C to 455°C, preferably 300°C to 425°C, most preferably 300°C to 375°C, while volatile components are evaporated therefrom, as will be described more fully later.
  • the preheated waste oil from line 16 is sprayed downwardly into the pyrolyzed waste oil mixture held at the bottom of the cylindrical reactor 18 to create a mixture of the fresh preheated waste oil and the pyrolyzed waste oil mixture for further treatment.
  • the spraying of the fresh waste oil also has the effect of cooling the pyrolyzed waste oil mixture to the desired temperature range of 300°C to 455°C.
  • the mixture of fresh waste oil and the non-volatile residue of the pyrolyzed waste oil mixture formed in the cylindrical reactor 18 in the manner stated, is pumped by pump 24 as a feed mixture via pipe 25 to a series of heating tubes 26 (only one of which is shown in Fig. 1, but see Fig. 2) within the tubular heating unit 20.
  • the unit 20 acts as an apparatus for rapidly raising the temperature of the feed mixture to a desired range of 400°C to 490°C for a short period of time (usually 1 to 30 seconds, preferably 1 to 15 seconds and most preferably 3 to 10 seconds).
  • Heat is created within the unit 20 by means of burners 28, turning the interior of the unit into a fire chamber.
  • the burners may burn a conventional fuel or a fuel or a gas from the reclamation process itself.
  • the feed mixture passing through the tubes 26 is heated rapidly by virtue of the large surface area of the tubes and the relatively small volume of feed mixture within the tubes.
  • the tubes 26 are preferably straight, with a length of preferably from 1.8 m to 6.0 m (6 to 20 feet), although the number and length of heating tubes depends on the per day volume of feedstock to be processed and the velocity of the feed mixture through the tubes (preferably 0.6 m to 4.5 m/s (2 to 15 feet/second), and ideally 1.2 m to 3.0 m/s (4 to 10 feet/second)).
  • the heating tubes 26 could be coils.
  • the heat consumption in the tubular heating unit is normally quite low, thus minimizing the size of the tubular heating unit 20.
  • the diameter of the heating tubes 26 is most preferably in the range of 1.25 cm-12.5 cm (0.5-5 inches) for efficient heating of the feed mixture within the heating tubes.
  • the feed mixture is heated to the desired temperature of 400°C to 490°C in the tubes 26 for a period of time sufficient to cause pyrolysis of heavy hydrocarbons in the feed mixture, but insufficient to permit substantial undesired polymerization, oxidation and dehydrogenation reactions to take place.
  • This time period depends to a certain extent on the type of feed mixture, but is generally in the range of 1 to 30 seconds, preferably 1 to 15 seconds and most preferably 3 to 10 seconds.
  • the resulting hot streams of pyrolyzed waste oil mixture from tubes 26 are passed to the bottom of the cylindrical reactor 18 via a pipe 30.
  • the temperature of the fluid in the cylindrical reactor 18 decreases from bottom to top due to an endothermic pyrolysis reaction that continues to take place in the reactor 18 and due to cooling caused by the spray of fresh waste oil feedstock from pipe 16.
  • the volatile oil and water components from the reactor 18, on being removed from the reactor through pipe 22, are first passed upwardly through heat exchange column 14 to pre-heat the fresh waste oil feedstock, as already described, and are then fed to a distillation column 32 via pipe 34 to form reclaimed oil fractions, the desired product, and water that may be re-used, as will be described later.
  • the feed mixture being delivered to the heating unit 20 from the cylindrical reactor 18 is admixed with steam from a steam heater 48, in amounts ranging from 3 to 50 mole percent, preferably 10 to 50 mole percent, steam, prior to entry of the feed mixture into the heating tubes 26.
  • the steam heater 48 is a tube coil or a steam boiler which may be set in the upper portion of the tubular heater 20.
  • the mixed stream is heated in heating tubes 26 and enters cylindrical reactor 18, as before.
  • the added steam, in conjunction with light fuel vapor passes through the heat exchanger 14 via pipe 22, is then separated in distillation column 32 into storage tank 40.
  • the hot water in tank 40 may then be pumped to steam heater 48 for re-use.
  • the pressure can be controlled by suitable adjustment of a valve (not shown) in the tubular heater outlet line 30.
  • the amount of fresh waste oil added from tank 10 may be balanced with the amount of product produced by the system so that the process may be operated on a continuous basis indefinitely.
  • the yield of the desired reclaimed oil product declines as the content of contaminants increases within the recirculating pyrolyzed mixture.
  • the yield may decline to 75% of the desired yield.
  • the temperature of the fluid within the tubular heating unit 20 may be raised to the range of 460°C to 520°C, to effect "deep pyrolysis" of the heavy hydrocarbons within the fluid, i.e. a greater degree of hydrocarbon cracking than is normally achieved.
  • the heavy residue and sludge in the cylindrical reactor which contains metals from waste oil additives and dirt, accumulates to an unacceptable level and a coking process must be carried out.
  • the residue is heated in tubes 26 or a separate set of coking tubes (not shown) to a temperature in the range of 470°C to 590°C measured at the outlet of the tubes.
  • the heated stream is fed back into the cylindrical reactor where it undergoes a pyrolysis reaction with the help of its entrained heat, under pressure of 21 kPa to 172 kPa (3 to 25 p.s.i.g.) and at a temperature of 440°C to 570°C, the pressure being controlled by means of a control valve 50.
  • the oil vapors produced thereby are distilled off in the normal way to form the desired product, and the coke containing metals and the like is deposited in the cylindrical reactor.
  • the system is shut down for decoking.
  • the ultimate residue of the process of the invention is therefore a coke in relatively small amounts that can be disposed of using conventional means to avoid environmental pollution, or can be used as an industrial fuel.
  • FIG. 2 this shows in more detail a preferred form of the tubular heating unit 20.
  • the heating tubes 26 are straight and contain no coils. When steam is used, coiled tubes could alternatively be provided in order to increase the residence time of the heavier feedstock.
  • the tubes may be set vertically, obliquely or horizontally.
  • the hot feedstock and steam enter the heating tubes 26 via valves 52, then leave via valves 54 for the cylindrical reactor 18. Plugs 56 at the bottom of each reaction tube are used for decoking and cleaning.
  • the temperature of the pyrolyzed mixture leaving the tubular heating unit 20 may be measured by temperature measuring devices 57, e.g. remotely monitored thermocouples.
  • Each reaction tube can be isolated by the indicated valves, so that failure of one tube does not affect the operation of the entire system and it can be replaced while the system continues to operate.
  • a different set of coking tubes (not shown) may be provided, if desired, for the coking reaction in order to avoid undue deposition within the heating tubes 26.
  • Such tubes would be much the same as tubes 26, but would have diameters in the range of 5 cm to 12.5 cm (2 to 5 inches), and would be arranged within the heating unit 20 parallel to tubes 26, but would only be fed with fluid when required for coking by the operation of appropriate valves (not shown).
  • the reaction tubes 26 may themselves be used for the coking reaction since coke deposition is kept to a minimum by using high liquid velocities (e.g. from 0.6 m to 4.5 m/s (2 to 15 feet/second)), straight heating tubes and, optionally, steam injection, as already indicated.
  • Fig. 3 shows in more detail a preferred embodiment of the cylindrical reactor 18.
  • Fig. 6 shows an alternative cylindrical reactor.
  • the pipe 16 introduces preheated feedstock into the cylindrical reactor 18 and the pipe 25 is a line for delivering mixture to the tubular heating unit 20.
  • the pipe 25 may be a series of tubes with inlets at different levels within the cylindrical reactor.
  • the heated fluid from the heating tubes 26 is recirculated to the cylindrical reactor 18 by pipe 30, which can be one tube or a number of tubes depending on the size of the tubular heating unit 20.
  • Oil and steam vapors are transferred to the heat exchange column 14 by tube 22, which is located at the top of the cylindrical reactor 18.
  • a flange 58 is provided for coke cleaning, and a line 60 is for sampling.
  • the reactor is made cylindrical for economy and for better containment of the usual reaction pressures, however, other shapes could be provided, if required.
  • the top and bottom of the cylindrical reactor may be flat or cone-shaped, as desired.
  • the coke formation in the cylindrical reactor 18 is limited by the high turbulence of the fluid within the reactor caused by the entrance of the high velocity oil and steam from the tubular heating unit 20, as well as the low reaction temperature of the cylindrical reactor where it is below 455°C. Therefore long run lengths can be achieved in this process. Decoking is normally required after the coking process has been carried out, and this may be achieved by steam decoking, water decoking, mechanical decoking or other methods.
  • FIG. 4 shows in more detail a preferred embodiment of an apparatus having two cylindrical reactors 18a and 18b.
  • the feedstock from the heat exchanger 14 and heated effluent from the tubular heating unit 20 can be switched to the other cylindrical reactor 18b by valves 62 and 64.
  • the apparatus of Fig. 4 is otherwise the same as that of Fig. 1.
  • the heavy residue and sludge in the cylindrical reactor 18a can be pumped to the tubular heating unit 20 and heated to a heater outlet temperature of 470°C to 590°C.
  • the heated effluent from the tubular heating unit 20 is switched to the other cylindrical reactor 18b to undergo a coking reaction under 21 kPa to 172 kPa (3 to 25 p.s.i.g.) pressure and at a temperature of 440°C to 570°C.
  • cylindrical reactor 18a When the heavy residue and sludge in cylindrical reactor 18a is pumped out to the tubular heating unit 20, fresh waste oil is pumped into the cylindrical reactor 18a to be subjected to normal cooling, evaporation, mixing and temperature raising steps. The cylindrical reactor 18b is then subjected to the decoking process. After completing the decoking process, the heated effluent from the tubular heating unit 20 is switched to the cylindrical reactor 18b and the fresh feedstock supply for the cylindrical reactor 18a is stopped. The cylindrical reactor 18b is subjected to normal cooling, evaporation, mixing and temperature raising steps. The cylindrical reactor 18a is ready for the next coking and decoking processes.
  • the process may be performed to make most efficient use of the equipment and to recycle and use contained heat for preheating and various process steps.
  • an alternative operation is shown in Figure 5.
  • Waste oil feedstock from tank 10 is pumped via pump 65 to heat exchanger 14 to preheat the feedstock to a temperature of about 115°C with steam.
  • the preheated feedstock is passed via line 66 to a flash drum 67 where water is evaporated from the feedstock and passed via line 68 to a heat exchanger 69 for cooling. The evaporated water is removed.
  • the heated feedstock from flash drum 67 is pumped via pump 70 through line 71 to distillation column 32 for further preheating with the hot vapour stream from cylindrical reactors 18a and 18b.
  • the heavy oil fraction from the bottom of distillation column 32 is mixed with 3% to 10% steam and is pumped by pump 72 through line 73 to tubular heater 20 where the temperature is raised to 450°C to 530°C.
  • the heated effluent from tubular reactor 20 is passed via line 74 to the bottom of one of the cylindrical reactors 18a or 18b for further reaction at 375°C to 455°C.
  • Vapour fuel from the cylindrical reactor 18a or 18b is passed via line 75 to the bottom of the distillation column 32 to preheat the feedstock from flash drum 70.
  • the vapour fuel in the distillation column 32 travels upward through the column and is separated into #2 fuel which is removed through stripper 76 which leads to heat exchanger 77, light fuel is passed via line 78 through heat exchanger 79 for cooling and recovery, and some #4 fuel is passed via line 80 through heat exchanger 81 for cooling and recovery.
  • a portion of the feedstock from the flash drum 70 can be sprayed downwardly via line 82 into the pyrolyzed waste oil mixture held at the bottom of the cylindrical reactor 18a or 18b to create a mixture of fresh preheated waste oil and the pyrolyzed waste oil mixture for further treatment.
  • the spraying of the waste oil feedstock from the flash drum 70 has the effect of cooling the pyrolyzed waste oil mixture to the desired temperature range of 375°C to 455°C.
  • the residue in the bottom of the cylindrical reactor 18a or 18b is mixed via a recycle line 83 with feedstock in the bottom of the distillation column 32 into tubular heater 20.
  • the decoking procedure can be carried out by methods such as steam decoking, water decoking and mechanical decoking.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Lubricants (AREA)
  • Electrical Discharge Machining, Electrochemical Machining, And Combined Machining (AREA)
  • Processing Of Solid Wastes (AREA)
  • Coke Industry (AREA)

Claims (11)

  1. Verfahren zur Aufbereitung von Altöl, das schwere Kohlenwasserstoffe und Verunreinigungen enthält, welches Folgendes umfasst:
    eine Temperatur einer Einspeisemischung von frischem Altöl und
    einem zurückgewonnenen nichtflüchtigen Rückstand auf einen Bereich von 400 °C bis 490 °C unter einem Druck von 276 kPa bis 1034 kPa (40 bis 150 p.s.i.g.) eine Zeitspanne von 1 bis 15 Sekunden lang zu erhöhen, die ausreicht, um Pyrolyse der in der Einspeisemischung enthaltenen schweren Kohlenwasserstoffe zu bewirken, jedoch nicht ausreicht, dass wesentliche unerwünschte Polymerisations-, Oxidations- und Dehydrierungsreaktionen in der Einspeisemischung stattfinden können;
    die entstehende pyrolysierte Altölmischung auf eine Temperatur im Bereich von 300 °C bis 455 °C abzukühlen und diese Temperatur aufrechtzuerhalten, während flüchtige Bestandteile in der pyrolysierten Altölmischung Abdampfen gelassen werden, wobei ein nichtflüchtiger Rückstand übrig bleibt, der die Verunreinigungen enthält;
    die verdampften flüchtigen Bestandteile zu kondensieren, um ein regeneriertes Ölprodukt zu bilden; und
    den nichtflüchtigen Rückstand mit frischem Altöl zu mischen, um mehr von der Einspeisemischung zu bilden und die Verfahrensschritte des Temperaturerhöhens, Abkühlens, Verdampfens und Mischens auf einer kontinuierlichen Basis zu wiederholen, während aus der pyrolysierten Altölmischung abgedampfte flüchtige Bestandteile weiter kondensiert werden.
  2. Verfahren nach Anspruch 1, bei dem, wenn eine Ausbeute des regenerierten Ölproduktes unter ein vorbestimmtes Niveau sinkt, die Temperatur der Einspeisemischung erhöht wird, um Tiefcracken der schweren Kohlenwasserstoffe zu fördern, und eine entstehende pyrolysierte Altölmischung dann weiteren Verfahrensschritten des Abkühlens, Verdampfens, Mischens und Temperaturerhöhens unterzogen wird.
  3. Verfahren nach Anspruch 1, bei dem, wenn Verunreinigungen in der pyrolysierten Altölmischung auf ein vorbestimmtes Niveau zunehmen, der nichtflüchtige Rückstand, der die Verunreinigungen enthält, auf eine Temperatur im Bereich von 470 °C bis 590 °C erwärmt wird und dann auf eine Temperatur im Bereich von 440 °C bis 570 °C gebracht wird und auf dieser Temperatur unter einem Druck von 21 kPa bis 172 kPa (3 bis 25 p.s.i.g.) gehalten wird, damit der Rückstand eine weitere Pyrolyse- und Verkokungsreaktion erfährt, die weitere flüchtige Bestandteile und festen Koks hervorbringt, woraufhin die weiteren flüchtigen Bestandteile entfernt und kondensiert werden und der feste Koks gesammelt und ausrangiert wird.
  4. Verfahren nach Anspruch 1, bei dem der Dampf in die Einspeisemischung eingeleitet wird, bevor der Verfahrensschritt des Temperaturerhöhens durchgeführt wird, und bei dem Wasser von den flüchtigen Bestandteilen getrennt wird.
  5. Verfahren nach Anspruch 1, bei dem die Zeitspanne 3 bis 10 Sekunden ist.
  6. Verfahren nach Anspruch 1, bei dem die entstehende pyrolysierte Altölmischung auf eine Temperatur im Bereich von 300 °C bis 425 °C abgekühlt wird.
  7. Verfahren nach Anspruch 1, bei dem die entstehende pyrolysierte Altölmischung auf eine Temperatur im Bereich von 300 °C bis 375 °C abgekühlt wird.
  8. Vorrichtung zur Aufbereitung von Altöl, das schwere Kohlenwasserstoffe und Verunreinigungen enthält, zur Verwendung bei dem Verfahren von Anspruch 1, welche Folgendes umfasst:
    eine Heizeinheit zur Temperaturerhöhung einer Einspeisemischung von frischem Altöl und einem zurückgewonnenen nichtflüchtigen Rückstand auf einen Bereich von 400 °C bis 490 °C eine Zeit lang, die ausreicht, um Pyrolyse der in der Einspeisemischung enthaltenen schweren Kohlenwasserstoffe zu bewirken, jedoch nicht ausreicht, dass wesentliche unerwünschte Polymerisations-, Oxidations- und Dehydrierungsreaktionen in der Einspeisemischung stattfinden können;
    zwei im wesentlichen identische Behälter und Rohre und Ventile, die es erlauben, die Behälter abwechselnd zu benutzen, zum Aufnehmen der entstehenden pyrolysierten Altölmischung und zum Speichern und Halten der pyrolysierten Altölmischung auf einer Temperatur im Bereich von 300 °C bis 455 °C, während flüchtige Bestandteile in der pyrolysierten Altölmischung Abdampfen gelassen werden, wobei ein nichtflüchtiger Rückstand übrig bleibt, der die Verunreinigungen enthält;
    einen Kondensator zum Kondensieren der verdampften flüchtigen Bestandteile, um ein regeneriertes Ölprodukt zu bilden; und
    eine Pumpanlage und Rohrleitungen zum Mischen des nichtflüchtigen Rückstandes aus den Behältern mit frischem Altöl, um mehr von der Einspeisemischung zu bilden, um die Einspeisemischung kontinuierlich durch die Heizeinheit in die Behälter umzupumpen und um die flüchtigen Bestandteile aus den Behältern in den Kondensator zu befördern.
  9. Vorrichtung zur Aufbereitung von Altöl, nach Anspruch 8, bei der die Heizeinheit mindestens ein Heizrohr enthält.
  10. Vorrichtung zur Aufbereitung von Altöl, nach Anspruch 9, bei der das mindestens eine Heizrohr gerade ist.
  11. Vorrichtung zur Aufbereitung von Altöl, nach Anspruch 9, bei der das mindestens eine Heizrohr in einer der Orientierungen vertikal, schräg und horizontal in der Heizeinheit angeordnet ist.
EP97900905A 1996-01-26 1997-01-24 Verfahren und vorrichtung zur aufarbeitung von altöl Expired - Lifetime EP0879273B1 (de)

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US59247896A 1996-01-26 1996-01-26
US592478 1996-01-26
PCT/CA1997/000053 WO1997027273A1 (en) 1996-01-26 1997-01-24 Process and apparatus for the treatment of waste oils

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KR (1) KR19990082068A (de)
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AU (1) AU719165B2 (de)
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US5885444A (en) * 1992-11-17 1999-03-23 Green Oasis Environmental, Inc. Process for converting waste motor oil to diesel fuel
ES2131022B1 (es) * 1997-10-21 2000-03-01 Landa Axpe Francisco J Procedimiento para producir de una forma continua el crakeo del aceite lubricante usado.
US7976699B2 (en) 2006-06-16 2011-07-12 Kesler Michael L Distillation apparatus and method of use
JP2008169343A (ja) * 2007-01-15 2008-07-24 Orient Sokki Computer Kk 油再生方法、油再生装置、脱硫方法、および脱硫装置
CN101974363B (zh) * 2010-09-29 2013-04-03 潘校良 一种废工业油料的回收处理方法及实施该方法的设备
RU2448145C1 (ru) * 2010-12-02 2012-04-20 Общество С Ограниченной Ответственностью "Проминтех" Способ замедленного коксования
CN102140360A (zh) * 2011-02-22 2011-08-03 唐山南光实业有限公司 高温蒸汽喷射式油砂油污泥处理装置
CN102140359A (zh) * 2011-02-22 2011-08-03 唐山南光实业有限公司 裂解蒸发式油砂油污泥处理装置
CN102140358A (zh) * 2011-02-22 2011-08-03 唐山南光实业有限公司 逐级裂解蒸发式油砂油污泥处理装置
CN102517066B (zh) * 2011-12-10 2014-03-26 唐山山岛石油化学有限公司 失衡油性废料高温缓冲热解蒸馏装置及工艺
CN103013554B (zh) * 2012-12-18 2015-05-13 青岛福瑞斯生物能源科技开发有限公司 一种用地沟油和废机油制备生物柴油的装置及方法
WO2014135966A1 (en) * 2013-03-07 2014-09-12 Verolube, Inc. Method and apparatus for recovering synthetic oils from composite oil streams
CN104629796A (zh) * 2013-11-14 2015-05-20 东营争峰新能源技术有限公司 一种废机油生产柴油设备
RU2562999C1 (ru) * 2014-06-25 2015-09-10 Общество с ограниченной ответственностью "Информ-технология" (ООО "Информ-технология") Способ замедленного коксования нефтяных остатков
KR101783764B1 (ko) 2015-09-23 2017-11-06 충북대학교 산학협력단 유증기 회수부를 포함하는 폐유재생시스템
CN106984439B (zh) * 2017-04-18 2019-04-05 长春工程学院 一种废油回收装置
CN113801681A (zh) * 2021-10-14 2021-12-17 广州新奥达云科技有限公司 一种低温状态下废机油热解装置

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EP0308669A1 (de) * 1987-08-29 1989-03-29 Asea Brown Boveri Aktiengesellschaft Verfahren zum Verwerten von Halogenkohlenwasserstoffe enthaltendem Ausgangsmaterial
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IL125496A (en) 2001-05-20
CA2242742A1 (en) 1997-07-31
IL125496A0 (en) 1999-03-12
BR9707470A (pt) 2000-01-04
JP2000503336A (ja) 2000-03-21
CN1214720A (zh) 1999-04-21
AU719165B2 (en) 2000-05-04
ATE236239T1 (de) 2003-04-15
EP0879273A1 (de) 1998-11-25
CN1074454C (zh) 2001-11-07
KR19990082068A (ko) 1999-11-15
HK1019616A1 (en) 2000-02-18
DE69720427D1 (de) 2003-05-08
WO1997027273A1 (en) 1997-07-31
EA199800657A1 (ru) 1999-02-25
CA2242742C (en) 2005-06-14
NO983434D0 (no) 1998-07-24
AU1433797A (en) 1997-08-20
EA000667B1 (ru) 2000-02-28
NO983434L (no) 1998-09-21

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