KR19990082068A - Waste oil treatment method and device - Google Patents

Abstract

The present invention is directed to a process and apparatus for the reclaiming and re-refining of waste oils. The process comprises raising a temperature of a feed mixture of fresh waste oil and a recycled non-volatile residue to a range of 400 DEG C to 490 DEG C for a time sufficient to cause pyrolysis of said heavy hydrocarbons contained in the feed mixture, but insufficient to permit substantial undesired polymerization, oxidation and dehydrogenation reactions to take place in said feed mixture; cooling the resulting pyrolized waste oil mixture to a temperature in the range of 300 DEG C to 425 DEG C, and maintaining said temperature while allowing volatile components in the pyrolyzed waste oil mixture to evaporate, leaving a non-volatile residue containing said contaminants; condensing the evaporated volatile components to form a reclaimed oil product; and mixing the non-volatile residue with fresh waste oil to form more of said feed mixture and repeating said temperature raising, cooling, evaporation and mixing steps on a continuous basis, while continuing to condense volatile components evaporated from said pyrolyzed waste oil mixture. The apparatus comprises a heating unit, a container, a condenser and pumping equipment and piping. The process and apparatus of the present invention generate #2 diesel fuel, gasoline and coke from waste oil.

Description

Waste oil treatment method and device

The oil used represents a major environmental problem. For example, in 1992 the U.S. Environmental Protection Agency reported that 4.9 million square meters (1.3 billion) of used oil produced annually in the United States, despite the many physical and chemical methods developed to recycle and refine industrial and automotive lubricants. Only about 2% of the gallons were estimated to be refinanced. The surplus of waste oil was probably thrown into the environment or disposed of in various ways.

Early major treatment methods include refining the waste oil with sulfuric acid and clay. Sulfuric acid acts as an extraction medium to remove the unsaturated, dirt, additives and coloring substances from the waste oil. Clay is used as an absorbent to remove impurities. Discomfort is that in this method, large amounts of spent acid sludge and clay are produced, which must be treated as treated waste.

In order to avoid waste disposal problems from acid-clay treatment, other forms of distillation have been developed, which are described, for example, in US Pat. No. 3,625,881 and US Pat. No. 4,071,438. The treatment produces a recycled lubricant as the main product and a carbon-black slurry as the treatment waste.

Recently, development of a method for regenerating useful fuels has produced diesel fuel from waste oil as described in US Pat. Nos. 5,271,808 and 5,286,349. U.S. Patent 5,271,808 describes a waste oil regeneration process in which a vessel heater is used. In this process, undesired polymerization, oxidation and dehydrogenation occurs because large volumes of raw material are stored in the heater vessel for long residence times at high temperatures resulting in unstable diesel fuel and large volumes of ash cake surplus. In addition, the processing length is very short.

Summary of the Invention

It is an object of the present invention to overcome some or all of the disadvantages of conventional waste oil recycling techniques by providing an effective and inexpensive treatment and apparatus for recycling waste oil.

It is a further object of the present invention to provide, in at least preferred form, a waste oil regeneration process for producing an acceptable, stable and useful # 2 diesel fuel or gasoline.

It is still another object of the present invention to provide a waste oil regeneration method which allows longer running time between shutdowns and forms less surplus than conventional methods.

Another object of the present invention is to provide a pyrolysis unit and a cylindrical reactor for use in the process of the invention.

According to one aspect of the present invention, a method of treating waste oil containing heavy hydrocarbons and impurities is provided. The method is sufficient to cause pyrolysis of the heavy hydrocarbons contained in the mixed fuel, but the mixed fuel of the regenerated non-volatile surplus and the newly produced waste oil for a time sufficient to cause the undesirable polymerization, oxidation and dehydrogenation reactions occurring in the mixed fuel. It raises the temperature of to the range of 400-490 degreeC (measured at the time of release of a heating unit). The pyrolysis waste oil mixture obtained is then cooled to a temperature in the range of 300 ° C. to 455 ° C., preferably 300 ° C. to 425 ° C., more preferably 300 ° C. to 375 ° C., to evaporate the volatile components in the pyrolysis waste oil mixture, It is maintained at this temperature while leaving a non-volatile surplus containing it. The evaporated volatile components are condensed to form a regenerated oil product, and the nonvolatile surplus is mixed with the newly generated waste oil to form a mixed fuel. The step of raising the temperature, cooling, evaporating and mixing is repeated on a continuous basis while the volatile components evaporated from the pyrolyzed waste oil mixture continue to condense.

The treatment temperature at which the waste oil is heated for pyrolysis depends on the conversion. That is, high temperatures will be used to further increase gasoline yields and low temperatures will be used to increase diesel oil yields.

In a preferred form of treatment, when the yield of regenerated oil product drops below a predetermined level, the temperature of the mixed fuel rises above the range of 400 ° C. to 490 ° C. to promote “deep cracking” of bicarbonate, and The waste oil mixture thus obtained is subjected to further cooling, evaporation and mixing steps.

In another preferred form of treatment, when the impurities in the pyrolyzed waste oil mixture increase to a predetermined level, the nonvolatile surplus containing impurities is heated to a temperature in the range of 470 ° C to 590 ° C for a short time to a temperature of 440 ° C to 570 ° C. In the range, maintained at this temperature under a pressure of 21 kPa to 172 kPa (3 to 25 psig), and the surplus undergoes additional pyrolysis and coking reactions to produce additional volatile components and solid coke, as a result Other volatile components are removed and condensed to collect and discard solid goggles.

In another preferred form of treatment, the feed is mixed with steam before the temperature rises.

According to another aspect of the present invention, an apparatus for treating waste oil containing heavy hydrocarbons and impurities is provided. The apparatus is sufficient to cause pyrolysis of the heavy hydrocarbons contained in the mixed fuel, depending on the conversion of the cylindrical reactor, but not enough to cause the undesirable polymerization, oxidation and dehydrogenation reactions occurring in the mixed fuel at temperatures between 400 ° C and 490 ° C. A heating unit for raising the temperature of the mixed fuel of the newly generated waste oil and the regenerated nonvolatile surplus in the range; The pyrolyzed waste oil mixture obtained is evaporated while evaporating the volatile components in the pyrolyzed waste oil mixture and leaving a non-volatile surplus containing impurities, and it is 300 ° C to 455 ° C, preferably 300 ° C to 425 ° C, more preferably 300 ° C. A container for holding and storing the pyrolyzed waste oil mixture at a temperature in the range of from 375 ° C .; A condenser for condensing the evaporated volatile components to form a recycled oil product; And mixing the nonvolatile surplus from the vessel with the newly generated waste oil to form the mixed fuel, continuously recycling the mixed fuel to the vessel through the heating unit, and recycling the volatile components from the vessel. It consists of a pumping device and piping for conveying to the condenser.

The heating of the feed is at high liquid velocity (speeds in the range of about 0.6 m to 4.5 m / s (2 to 15 feet / second), more preferably 1.2 m to 3.0 m / s (4 to 10 feet / second) It is preferably carried out in a tubular heating unit which can be operated, the pyrolyzed mixture is preferably cooled and the volatile components are evaporated in a cylindrical reactor which serves as the vessel. The temperature of the cylindrical reactor is controlled by adjusting the volume of the preheated feedstock injected into the cylindrical reactor. The short residence time in the tubular heating unit (ie 1 to 30 seconds, preferably 1 to 15 seconds, more preferably 3 to 10 seconds) and the relatively low temperature in the cylindrical reactor minimize unwanted side reactions.

Under the high temperatures present in the tubular heating unit, other impurities and all metal constituents of the waste oil decompose into metals, hydrocarbons and heavy surpluses. Light fuel steam along with steam from the cylindrical reactor is preferably injected into the heat exchanger to preheat (ie, to a temperature in the range of 110 ° C. to 150 ° C.) of the newly generated waste oil feedstock. The heavier excess oil in the cylindrical reactor along with the newly produced waste oil feedstock is pumped back into the tubular heating unit during a second heating and pyrolysis reaction and the process is repeated continuously. The temperature in the tubular heater increases for deep cracking when the high boiling oil in the cylindrical reactor accumulates to the extent that the treated product is reduced. The temperature then returns to normal.

Alternatively steam injection can be used with a tubular heater for steam cracking. This improves oil stability and reduces coke formation. Steam can be produced by tubular heating units.

The preheated raw material is usually injected into the top of the cylindrical reactor. Sprayed down from the center. The heat pyrolyzed mixture from the heated tube in the tubular heating unit is injected near the bottom of the cylindrical reactor. The raw material line for the heating tube is introduced from the bottom of the cylindrical reactor and then passed through the pump to the tubular heater. The raw material from the cylindrical reactor can enter the tubular heater from the top or bottom. If desired, the preheated raw material can pass through or partially pass through the cylindrical reactor and be pumped directly to the tubular heater depending on the temperature of the fluid in the cylindrical reactor.

Products produced by reclaiming waste oil using the methods and apparatus of the present invention include # 2 diesel fuel, gasoline and coke. The method and apparatus can be operated without causing significant waste disposal problems.

The raw materials for processing may be certain types of waste oils such as automotive oils, industrial lubricants, vegetable oils, fish oils, industrial oil sludges and flowing artificial waste oils.

The present invention relates to a method and apparatus for recycling waste oil from various sources.

1 is a schematic representation of an apparatus that may be used to practice the method of the present invention;

2 is a schematic representation of a preferred tubular heater used in the apparatus of FIG. 1;

3 is a schematic representation of a preferred cylindrical reactor used in the apparatus of FIG. 1;

4 is a schematic representation of an embodiment of an apparatus with two cylindrical reactors;

5 is a schematic representation of an embodiment of an optional arrangement for a device of the present invention; And

6 is a schematic representation of an optional cylindrical reactor.

An embodiment of the overall process of the present invention and a typical apparatus used are described with reference to FIG. In the described method, the newly generated waste oil processing material is pumped from the raw material tank 10 via the pipe 12 to the top of the heat exchange column 14 (one or more may be provided, if necessary). Not shown), where the raw material flows downward and is preheated (generally to a temperature in the range of 110 ° C. to 150 ° C.) by heat exchange (in the manner described below) with the product vapor. The preheated raw material is then pumped from the bottom of the heat exchange column 14 through line 16 to the cylindrical reactor 18, where the cylindrical reactor is for receiving and maintaining the pyrolyzed waste oil mixture from the tubular heating unit 20. Form a container. The pyrolyzed mixture is maintained at a predetermined temperature in the range of 300 ° C. to 455 ° C., preferably 300 ° C. to 425 ° C., more preferably 300 ° C. to 375 ° C., while the volatile components evaporate therefrom, This will be explained in more detail later. The preheated waste oil from line 16 is sprayed downward into the pyrolyzed waste oil mixture stored at the bottom of the cylindrical reactor 18 to produce a mixture of freshly generated preheated waste oil and pyrolyzed waste oil mixture for further processing. . Spraying the newly generated waste oil also has the effect of cooling the pyrolyzed waste oil mixture to a preferred temperature range of 300 ° C to 455 ° C. The light oil and water from the newly generated preheated waste oil and pyrolyzed waste oil mixture are evaporated and distilled to leave a nonvolatile surplus, and the vapor obtained is moved from the cylindrical reactor 18 through the pipe 22 to exchange heat exchange column 14 ).

The mixture of the non-volatile surplus of the pyrolyzed waste oil mixture formed in the cylindrical reactor 18 and the newly generated waste oil in the described method is produced in the tubular heating unit 20 in series of heating tubes 26 (one of which is shown in FIG. 1). 2 but is pumped by pump 24 as mixed fuel through pipe 25. The heating unit 20 is a device for rapidly raising the temperature of the mixed fuel to a preferred range of 400 ℃ to 490 ℃ for a short period of time (usually 1 to 30 seconds, preferably 1 to 15 seconds, more preferably 3 to 10 seconds) Function as. Heating is carried out in the heating unit 20 by means of a burner 28, moving the interior of the heating unit into the combustion chamber. The burner can burn conventional fuel or fuel or gas from a regeneration process.

The mixed fuel passing through the tube 26 is quickly heated by the relatively small volume of the mixed fuel and the large surface area of the tube in the tube. The tube 26 has a volume per day of raw material to be processed and the speed of the mixed fuel through the tube (preferably 0.6 m to 4.5 m / s (2 to 15 ft / sec), ideally 1.2 m). 6 m to 6.0 m (6 to 20 ft) in length, although preferred, is preferred. The heating tube 26 may be a coil. Since the temperature difference between the contents of the tubular heating unit 20 and the contents of the cylindrical reactor 18 is about 100 ° C., the heat consumption in the tubular heating unit is usually very small, which is the size of the tubular heating unit 20. Is minimized. The diameter of the heating tube 26 is most preferably in the range of 1.25 cm to 12.5 cm (0.5 to 5 inches) for efficient heating of the mixed fuel in the heating tube.

As already pointed out, the mixed fuel is sufficient to cause pyrolysis of bihydrocarbons in the mixed fuel, but in a period of 400 ° C. to 200 ° C. in the tube 26 for a period of time sufficient to cause substantially undesirable polymerization, oxidation and dehydrogenation reactions. Heated to a desired temperature of 490 ° C. The time period depends somewhat to the type of mixed fuel, but is generally in the range of 1 to 30 seconds, preferably 1 to 15 seconds and more preferably 3 to 10 seconds.

The hot stream of the resulting pyrolyzed waste oil mixture is passed from the tube 26 through the pipe 30 to the bottom of the cylindrical reactor 18. The temperature of the fluid in the cylindrical reactor 18 decreases from the bottom to the top due to the cooling caused by endothermic pyrolysis reactions occurring in the reactor 18 and spraying of the newly generated waste oil stock from the pipe 16. Upon traveling from the reactor via pipe 22, the water component and volatile oil from reactor 18 first pass upwardly through heat exchange column 14 to preheat the newly generated waste oil feedstock as previously described and then As described later, it is injected into the distillation column 32 through pipe 34 to form the desired product and recycled oil fraction with water that can be reused.

In the apparatus shown in FIG. 1, three fractions are obtained from the distillation column 32 and transferred to tanks 36, 38, 40. The remaining gas and light product are filled through pipe 42 and condensed in liquid collection tank 44. The most preferred product, # 2 diesel fuel (typically condensed at 110 ° C. to 360 ° C.), is generally collected in tank 38, and light oil (usually condensed at 75 ° C. to 150 ° C.) and water are transferred to tank (40). ), And heated fuel (condensed at temperatures above 360 ° C.) is collected in tank 36.

According to the process described above, the preheated freshly generated waste oil feedstock from the heat exchange column 14 can be optionally removed from the cylindrical reactor 18, for example when the pyrolyzed waste oil mixture in the cylindrical reactor 18 does not require any further cooling. The flow can be diverted completely or partially through the pipe 46 to the inlet of the tubular heating unit 20. The newly produced waste oil stock is then mixed directly with the non-volatile surplus of the pyrolyzed waste oil mixture from reactor 18 into pump 24 before the resulting mixed fuel enters tube 26.

Optionally, the mixed fuel transferred from the cylindrical reactor 18 to the heating unit 20 is steamed in an amount ranging from 3 to 50 mole percent, preferably from 10 to 50 mole percent, before the mixed fuel enters the heating tube 26. Mixed with steam from steam heater 48. The steam heater 48 is a tube coil or steam boiler installed on top of the tubular heater 20. The mixed stream is heated in a heating tube 26 and enters the cylindrical reactor 18 as above. The added steam, such as diesel gas, passes through the heat exchanger 14 through the pipe 22 and is separated from the distillation column 32 into the storage tank 40. Hot water in tank 40 is pumped to steam heater 48 for reuse.

It is useful to provide a pressure of 276 kPa to 1034 kPa (40 to 150 p.s.i.g.) in the heating tube 26 during the process of the present invention. The pressure can be adjusted by appropriate adjustment of a valve (not shown) in the tubular heater outlet line 30.

The amount of freshly generated waste oil added from the tank 10 can be balanced by the amount of product produced by the system so that the process can be performed vaguely on a continuous basis. However, it is generally found that after an operating cycle, the yield of preferably regenerated oil product is tilted as the content of impurities in the recycle pyrolyzed mixture increases. For example, the yield can be tilted to 75% of the desired yield. As above, the temperature of the fluid in the tubular heating unit 20 rises in the range of 460 ° C. to 520 ° C. such as “deep pyrolysis” of the heavy hydrocarbons in the fluid, such as higher hydrocarbon cracking than that normally obtained. Affects. In addition, while there is a risk of undesired polymerization and the like, the yield is improved by substantially increasing the amount of volatile components useful for distillation from the reactor 18. During this step the flow of fluid through the tube 26 remains the same as during the regular part of the process, so the residence time in the tube at a stable high temperature is about 1 to 15 seconds. The time required for deep pyrolysis and the improvement in the yield thus obtained depend very much on the nature of the raw material, such as the content of sludge and other impurities.

According to an important feature of the present invention, sludge and heavy surplus in a cylindrical reactor containing metals from waste oil additives and dirt can be accommodated after the process has been running for a long time (ie 1 to 6 months, depending on the nature of the waste oil). Accumulate to an unprecedented level and the caulking process should be conducted To affect the coking process, the excess is heated in a tube 26 or in a separate set of caulking tubes (not shown) to a temperature in the range of 470 ° C. to 590 ° C. measured at the tube outlet. The heated stream is reinjected into the cylindrical reactor, where it undergoes pyrolysis reaction with the aid of heat entrained under pressure of 21 kPa to 172 kPa (3 to 25 psig) at a temperature of 440 ° C to 570 ° C, the pressure being a control valve 50 is adjusted. The oil vapor produced by this is distilled in the normal way to form the desired product, and the coke containing metal and the like is deposited in the cylindrical reactor. After the coke is formed, the system stops for decoking. The final surplus of the process of the present invention is a relatively small amount of coke which can be deposited using conventional means to avoid environmental pollution or can be used as industrial fuel.

Referring to FIG. 2, this illustrates in more detail the preferred form of the tubular heating unit 20. As can be seen, the heating tube 26 is straight and contains no coils. When steam was used, coiled tubes could optionally be provided to increase the residence time of heavier raw materials. The tubes can be installed vertically, obliquely or horizontally. Hot raw material and steam (when steam is used) enter the heating tube 26 through the valve 52 and leave the valve 54 for the cylindrical reactor 18. At the bottom of each reaction tube 26 a plug 56 is used for decoking and cleaning.

The temperature of the pyrolyzed mixture leaving the tubular heating unit 20 may be measured by a temperature measuring device 57 such as a thermocouple that is remotely controlled.

Each reaction tube can be separated by a designated valve so that a problem in one tube does not affect the operation of the entire system and can be exchanged while the system continues to operate. As indicated above, other sets of caulking tubes (not shown) may be provided for the caulking reaction to avoid excessive deposition in the heating tube 26. The tubes are often the same as tubes 26, but have a diameter in the range of 5 to 12.5 cm (2 to 5 inches) and are arranged in heating unit 20 parallel to tube 26, but with a suitable valve (not shown). Can only be injected into the fluid when required for caulking. However, the reaction tube 26 has a coke reaction because the high liquid velocity (0.6 m to 4.5 m / s (2 to 15 feet / second)), straight heating tube, and optionally steam injection can be used to keep the coke deposition to a minimum. The tube itself can be used.

3 illustrates in more detail a preferred embodiment of the cylindrical reactor 18. 6 shows an optional cylindrical reactor. In each case, the pipe 16 injects the preheated raw material into the cylindrical reactor 18 and the pipe 25 is a line for conveying the mixture to the tubular heating unit 20. In practice, the pipe 25 may be a series of tubes with inlets at different levels in the cylindrical reactor. The fluid heated from the heating tube 26 is recycled to the cylindrical reactor 18 by the pipe 30, which may be a number of tubes or one tube depending on the size of the tubular heating unit 20. . The oil and steam vapors are transferred to the heat exchange column 14 by a tube 22, which is located on top of the cylindrical reactor 18. Flange 58 is provided for coke cleaning and line 60 is for sampling. The reactor is economical and manufactured in a cylindrical shape for better suppression of normal reaction pressure, but may be provided in other shapes as needed. The top and bottom of the cylindrical reactor are preferably flat or cone shaped.

During normal use, coke formation in the cylindrical reactor 18 is subject to high convection of fluid in the reactor caused by the inflow of high speed oil and steam from the tubular heating unit 20 as well as the low reaction temperature of the cylindrical reactor below 455 ° C. Limited by Therefore a long running length can be obtained in this way. Decoking is usually required after the coking process has been carried out, which can be obtained by steam decoking, water decoking, mechanical decoking or other methods.

In order to continue working without stopping the decoking system, another cylindrical reactor may be provided to continue the reaction while the first reactor is decoked and cleaned. The two cylindrical reactors will have essentially the same structure. 4 shows in more detail a preferred embodiment of the apparatus with two cylindrical reactors 18a, 18b. When one cylindrical reactor 18a undergoes a decoking process, the raw material from the heat exchanger 14 and the heated effluent from the tubular heating unit 20 are transferred to the other cylindrical reactor 18b by valves 62 and 64. Can be switched. The device of FIG. 4 is the same as the device of FIG. 1.

Optionally, when one cylindrical reactor 18a is used for the time for the method of the present invention, the heavy surplus and sludge in the cylindrical reactor can be pumped into a tubular heating unit 20, with a heater outlet temperature of 470 ° C to 590 ° C. Can be heated. The heated effluent from the tubular heating unit 20 is switched to another cylindrical reactor 18b to undergo a coking reaction at a temperature of 440 ° C. to 570 ° C. and a pressure of 21 kPa to 172 kPa (3 to 25 p.s.i.g.). When the sludge and heavy surplus in the cylindrical reactor 18a are pumped into the tubular heating unit 20, the newly generated waste oil is pumped into the cylindrical reactor 18a which enters the normal cooling, evaporation, mixing and temperature increase stages. The cylindrical reactor 18b then enters the decoking process. After the decoking process, the heated effluent from the tubular heating unit 20 is switched to another cylindrical reactor 18b and the newly generated feedstock for the cylindrical reactor 18a is stopped. Cylindrical reactor 18b enters the normal cooling, evaporating, mixing and temperature increase stages. The cylindrical reactor 18a is prepared for the next coking and decoking step.

Alternatively, the process may be carried out to make the most efficient use of the equipment and to allow the heat contained during the preheating and various process steps to be regenerated and used. For example, an optional task is shown in FIG.

Waste oil raw material from tank 10 is pumped to heat exchanger 14 via pump 65 to preheat the raw material to a temperature of about 115 ° C. with steam. The preheated raw material passes through line 66 to flash drum 67 where water is evaporated from the raw material and passed through line 68 to heat exchanger 69 for cooling. Evaporated water is removed. Heated raw material from flash drum 67 is pumped to distillation column 32 via pump 70 via line 71 to further preheat with hot steam steam from cylindrical reactors 18a and 18b. The heavy oil fraction from the bottom of the distillation column 32 is mixed with 3% to 10% steam and the tubular heater 20 whose temperature is raised to 450 ° C. to 530 ° C. via the line 73 by the pump 72. Pumped). The heated effluent from the tubular reactor 20 is passed through line 74 to the bottom of one of the cylindrical reactors 18a or 18b for further reaction at 375 ° C to 455 ° C. Vapor fuel from cylindrical reactor 18a or 18b is passed through line 75 to the bottom of distillation column 32 to preheat raw material from flash drum 70. The vapor fuel in the distillation column 32 moves upward through the column and is separated into # 2 fuel which is removed through the stripper 76 leading to the heat exchanger 77, and the diesel oil is replaced by the heat exchanger 79 for cooling and recovery. Pass through line 78, and # 4 fuel passes through line 80 through heat exchanger 81 for cooling and recovery.

A portion of the raw material from the flash drum 70 is lined with the pyrolyzed waste oil mixture stored at the bottom of the cylindrical reactor 18a or 18b to produce a mixture of pyrolyzed waste oil mixture and freshly generated preheated waste oil for further processing. Sprayed downward through 82. Spraying the waste oil raw material from the flash drum 70 has the effect of cooling the pyrolyzed waste oil mixture to a preferred temperature range of 375 ° C to 455 ° C. Excess in the bottom of the cylindrical reactor 18a or 18b is mixed with raw material in the bottom of the distillation column 32 via the recirculation line 83 and enters the tubular heater 20. When one of the cylindrical reactors 18a or 18b is filled with coke, the effluent heated from the tubular reactor 20 is switched to another reactor to enter the pyrolysis and coking reaction. The first reactor can then enter the decoking process.

The decoking reaction can be carried out by methods such as steam decoking, water decoking and mechanical decoking.

While the invention has been described in detail above, it will be apparent that various modifications and changes can be made without departing from the spirit and scope of the invention.

Claims (15)

It is sufficient to cause thermal decomposition of heavy hydrocarbons contained in the mixed fuel, but the temperature of the mixed fuel of the regenerated nonvolatile surplus and the newly generated waste oil for a period of time sufficient to cause undesired polymerization, oxidation and dehydrogenation reactions in the mixed fuel. Raise to the range of 400 ° C to 490 ° C; Cooling the pyrolysis waste oil mixture to a temperature in the range of 300 ° C. to 455 ° C., evaporating the volatile components in the pyrolysis waste oil mixture and maintaining at this temperature while leaving a non-volatile surplus containing the impurities; The evaporated volatile components condense to form a regenerated oil product; And The nonvolatile surplus is continuously repeated based on the step of mixing with the newly generated waste oil to form a mixed fuel, raising the temperature, cooling, evaporating and mixing, while volatile components evaporated from the pyrolyzed waste oil mixture. Method for treating waste oil containing heavy hydrocarbons and impurities, characterized in that it comprises a step of continuously condensing. The method of claim 1, When the yield of regenerated oil product falls below a predetermined level, the temperature of the mixed fuel rises to facilitate deep cracking of the heavy hydrocarbons, and the pyrolyzed waste oil mixture enters further cooling, evaporating, mixing and temperature increase stages. Way. The method of claim 1, When the impurities in the pyrolyzed waste oil mixture increase to a predetermined level, the non-volatile surplus containing impurities is heated to a temperature in the range of 470 ° C to 590 ° C to a temperature range of 440 ° C to 570 ° C, and 21 to 172 ° C. Maintained at this temperature under pressure of kPa, the surplus undergoes additional pyrolysis and coking reactions to produce additional volatile components and solid coke, whereby other volatile components are removed and condensed to collect and discard the solid goke. Characterized in that the method. The method of claim 1, Wherein said steam is injected into said mixed fuel prior to said temperature increasing step and said water is separated from said volatile components. The method of claim 1, The mixed fuel enters a pressure in the range of 276 kPa to 1034 kPa as the temperature increases. The method of claim 1, The mixed fuel is maintained at a temperature in the range of 400 ° C. to 490 ° C. for a time period of 1 to 15 seconds. The method of claim 6, The time period is 3 to 10 seconds. The method of claim 1, The obtained pyrolyzed waste oil mixture is cooled to a temperature in the range of 300 ° C to 425 ° C. The method of claim 1, The obtained pyrolyzed waste oil mixture is cooled to a temperature in the range of 300 ° C to 375 ° C. It is sufficient to cause thermal decomposition of the heavy hydrocarbons contained in the mixed fuel, but the waste oil and the regenerated ratio of the newly produced waste oil in the range of 400 ° C. to 490 ° C. for a period of time insufficient to cause undesired polymerization, oxidation and dehydrogenation reactions in the mixed fuel. A heating unit for raising the temperature of the mixed fuel of the volatile surplus; Receive the pyrolyzed waste oil mixture obtained while evaporating the volatile components in the pyrolyzed waste oil mixture, leaving a non-volatile surplus containing impurities, and maintaining and storing the pyrolyzed waste oil mixture at a temperature in the range of 300 ° C to 455 ° C. Containers for; A condenser for condensing the evaporated volatile components to form a recycled oil product; And Non-volatile surplus from the vessel is mixed with freshly generated waste oil to form the mixed fuel, the mixed fuel is continuously recycled to the vessel through the heating unit, and the volatile components from the vessel are condenser An apparatus for treating waste oil containing heavy hydrocarbons and impurities, comprising a pumping device and a pipe for transporting the furnace. The method of claim 10, And the heating unit comprises at least one heating tube. The method of claim 11, And the at least one heating tube is straight. The method of claim 11, The at least one heating tube is installed in the heating unit in a direction selected from the group consisting of vertical, oblique and horizontal. The method of claim 10, The apparatus comprises two pipes and a pipe and a valve for selectively using the container. The method of claim 14, Wherein the two containers are substantially identical.