JP4866579B2 - Waste oil treatment method in oil refining - Google Patents

Description

  The present invention relates to a method for treating waste oil (slop oil) generated in a petroleum refining process.

  FIG. 2 shows an outline of an example of a typical oil refining process conventionally performed.

  As shown in FIG. 2, in the oil refining process, the crude oil in the crude oil tank 100 is usually fed to the atmospheric distillation column 103 through the crude oil desalting apparatus 101 and the heating furnace 102, and is sent to the atmospheric distillation column 103. , Naphtha, kerosene, light oil, etc. are fractionated for each fraction, and heavy oil is separated as residual oil. Subsequently, the said fraction and residual oil are made into petroleum products through the process process in the processing apparatus 200 arrange | positioned downstream of the atmospheric distillation tower 103. FIG.

  Further, in such a petroleum refining process, waste oil generated from the crude oil desalting apparatus 101, mixed oil generated when the apparatus is switched, and off-spec (non-standard) products are used as waste oil (slop oil) in a slop tank. 300 are collected and processed (see Patent Documents 1 and 2).

  At present, slop oil generated in such refineries is accepted in one slop tank 300 without distinguishing heavy and light distillation characteristics, and thereafter, this slop oil is removed from the slop tank 300 into crude oil. It is sent to the salt device 101 and fractionated for each fraction together with the crude oil, and then sent to the processing device 200 of the next step for processing. In general, slop oil is processed in the same manner as crude oil and residual oil.

  According to the results of studies and experiments conducted by the present inventors, according to the distillation properties of a certain slop oil, a light fraction having a distillation temperature (EP) of 360 ° C. or lower is about 90% by volume, and a heavy fraction having a distillation temperature of 360 ° C. or higher. The fraction was 10% by volume, most of which was lighter than the light oil fraction.

  As the product properties will require severe management due to the planned zero-sulfurization and ultra-deep desulfurization in the future, the amount of off-spec products is expected to increase. Is likely to increase.

  From the above viewpoint, the present inventors do not have such a bad property that the light component in the slop oil has to be returned to the atmospheric distillation column 103. Therefore, the heavy component and the light component are not included. In other words, the heavy component can be returned to the atmospheric distillation column 103 and the light component can be returned to the processing apparatus 200 downstream of the atmospheric distillation column 103.

  Therefore, the present inventors have proposed a waste oil treatment method in petroleum refining as described in Patent Document 3. A brief description will be given with reference to FIG.

  As described above, according to the results of our experiments, according to the conventional method, in the slop oil, the light fraction at 360 ° C. or less is about 90% by volume, according to the distillation properties of the slop oil. It was found that the heavy fraction at 360 ° C. or higher was 10% by volume, and that most of the heavy fraction was lighter than the light oil fraction.

  Therefore, in the invention described in Patent Document 3, the slop oil is roughly divided into a slop oil composed of a light component (light slop oil) and a slop oil composed of a heavy component (residual slop oil). The residual oil slop oil contains a heavier fraction containing vacuum gas oil, and the light slop oil contains a lighter fraction containing light oil.

  Therefore, as shown in FIG. 3, as the slop tank, a tank 300 dedicated to the residual oil slop oil and a tank 400 dedicated to the light slop oil are provided, and the light slop oil and the residual oil slop oil are separated into separate tanks, that is, The residual oil slop oil tank 300 and the light slop oil tank 400 were accepted respectively.

  As described above, the residual oil slop oil and the light slop oil are configured to be received in the separate tanks 300 and 400, respectively, so that the residual oil slop oil is passed from the tank 300 through the crude oil desalting apparatus 101 and the heating furnace 102. The light slop oil is sent to the atmospheric distillation column 103 and processed, and the light slop oil is returned to the raw material of the processing step disposed downstream of the atmospheric distillation column 103 for processing.

  That is, with the above configuration, the residual oil slop oil generated in the residual oil treatment process for treating the residual oil is sent to the atmospheric distillation tower together with the crude oil and processed, and the light slop oil generated in the light oil treatment process for processing the fraction. Is returned and processed as a raw material for the residual oil treatment process or the light treatment process.

According to the invention described in Patent Document 3, as described above, slop oil is treated by distinguishing residual oil slop oil and light slop oil according to the generation process thereof, and the residual oil slop oil is treated with an atmospheric distillation column in the same manner as in the past. 103, and the light slop oil is returned to the processing apparatus downstream of the atmospheric distillation column 103, so that all the slop oils are returned to the atmospheric distillation column 103 as compared with the conventional case. The fuel corresponding to the basic unit of the device can be saved for the flow rate passing through 103, and as a result, it is possible to save energy and reduce carbon dioxide emissions, and to make gasoline and diesel oil sulfur-free. Further, if ultra-deep desulfurization proceeds, the advantage is further increased from the viewpoint of the amount of off-spec products generated.
JP-A-5-222374 Special table 2003-511546 gazette Japanese Patent Application No. 2004-027357

  However, according to the results of further research and experiments by the present inventors, the following has been found.

  In other words, among the slop oil, if the light slop oil generated in the light processing step that processes the atmospheric pressure fraction is mixed with the intermediate product in the oil refining process, the processing equipment is contaminated. , Processing may be difficult. For example, in a heat exchanger, dirt due to slop oil is deposited on the inner surface, so that the heat exchange efficiency deteriorates, so that a predetermined operation may not be performed.

  The inventors of the present invention have obtained the idea that by limiting the intermediate product oil mixed with the light slop oil, the problem of dirt can be avoided, and as a result of intensive studies, the present invention has been completed.

  The present invention has been made based on such novel findings of the present inventors.

  The main object of the present invention is to provide a method for treating waste oil in an oil refining process, which can avoid the problem caused by dirt caused by slop oil.

  Another object of the present invention is to provide a method for treating waste oil in an oil refining process that can reduce fuel in an atmospheric distillation tower, thereby saving energy and reducing carbon dioxide emissions.

The above object is achieved by the method for treating waste oil in the oil refining process according to the present invention. In summary, the present invention separates crude oil into residual oil and at least one atmospheric distillation fraction in an atmospheric distillation tower, and then the fraction and the residual oil are downstream of the atmospheric distillation tower. In the waste oil treatment method for treating in the oil refining process slop oil generated in the oil refining process for further processing in the processing apparatus arranged in
The intermediate product oil containing 30% by volume or more of the aromatic content of light slop oil generated in the light treatment step of treating the normal pressure fraction, including the heaviest heavy light oil fraction of the normal pressure fraction. the 0.1 to 15% by volume mixed oil mixture against the a waste oil processing method and performing slop oil treatment in the process unit for processing the residual oil.
According to an embodiment of the present invention, the light slop oil has a 90% distillation temperature of 160 to 420 ° C, and the intermediate product oil has a 90% distillation temperature of 450 to 580 ° C.

According to another embodiment of the present invention, the processing apparatus performs processing without vaporizing the entire amount of the mixed oil.

According to another embodiment of the invention, the intermediate product oil further comprises a fraction derived from the residual oil. Here, according to another embodiment of the present invention, the fraction derived from the prior chopped oil is a vacuum gas oil fraction or bottoms obtained by vacuum distillation residual oil thermal or catalytic cracking to obtain Cracked oil.

  In the present invention, a mixed oil obtained by mixing a light slop oil with an intermediate product oil containing 30% by volume or more of an aromatic component is processed by a processing apparatus, and contamination caused by the slop oil is hardly generated.

  Moreover, according to this invention, light slop oil can be utilized as a part of intermediate product oil, without using it as an atmospheric distillation raw material.

  The present invention separates crude oil into residual oil and at least one atmospheric distillation fraction in an atmospheric distillation tower, and then the fraction and the residual oil are disposed in a processing apparatus disposed downstream of the atmospheric distillation tower. The present invention relates to a waste oil processing method for processing slop oil generated in an oil refining process for further processing to produce a petroleum product in the oil refining process. In particular, in the waste oil treatment method in such a petroleum refining process, the present invention provides a light slop oil generated in a light treatment process for treating a normal pressure fraction as an intermediate product oil containing 30% by volume or more of an aromatic component. The mixed oil is subjected to slop oil treatment in the processing device.

  Next, the light slop oil, intermediate product oil, and mixed oil in the present invention will be described.

[Light slop oil]
Light slop oil is generated in a light processing step of processing a normal pressure fraction.

  The 90% distillation temperature is preferably 160 to 420 ° C, particularly 180 to 380 ° C, and the 97% distillation temperature is preferably 200 to 380 ° C, particularly 220 to 340 ° C.

[Intermediate product oil]
The intermediate product oil contains an aromatic content of 30% by volume or more, preferably 30 to 60% by volume. When the content is less than 30% by volume, the stain generated from the slop oil cannot be completely dissolved, causing a problem that the stain is deposited.

  As preferable distillation properties, the 90% distillation temperature is 450 to 580 ° C., particularly 500 to 550 ° C., and 250 to 400 ° C., particularly 300 to 350 ° C. higher than that of light slop oil.

  The intermediate product oil is preferably the heaviest fraction of the atmospheric pressure fraction and / or the fraction derived from the residual oil. The heaviest fraction in the atmospheric pressure fraction is a so-called heavy gas oil fraction. Examples of the fraction derived from the residual oil include a vacuum gas oil fraction obtained by distilling the residual oil under reduced pressure, and a cracked oil obtained by pyrolyzing or catalytically cracking the residual oil.

  Cracked light oil which is a fraction containing a large amount of aromatics, that is, (1) catalytic cracked light oil (including so-called “LCO”) obtained by catalytic cracking using residual oil or heavy gas oil as a raw material, (2) An intermediate product oil containing pyrolysis gas oil obtained by pyrolysis using residual oil or heavy gas oil as a raw material is preferred. The content of the cracked light oil in the intermediate product oil is preferably 5 to 60% by volume, particularly 20 to 50% by volume.

[Mixed oil]
The mixed oil is obtained by blending light slop oil with intermediate product oil, and the blending amount of light slop oil is preferably 0.1 to 15% by volume, particularly preferably 0.5 to 5% by volume. When the blending amount is outside the range of 0.1 to 15% by volume, there is a large amount of dirt generated from the slop oil, so that it cannot be completely dissolved and the dirt is deposited.

[Treatment of mixed oil]
The petroleum refining step for treating the mixed oil preferably includes at least one step of hydrorefining and hydrocracking.

  Since mixed oil does not generate dirt, it is preferable to process it without vaporizing the whole quantity. Preferred reaction conditions are a reaction temperature of 250 to 450 ° C., a reaction pressure of 1 to 25 MPa, particularly a reaction temperature of 300 to 430 ° C., and a reaction pressure of 8 to 25 MPa.

Example 1
EXAMPLES Hereinafter, although an Example demonstrates this invention, this invention is not interpreted limitedly by this Example. In this example, the density is JIS K 2249, the sulfur content is JIS K 2541 (ultraviolet fluorescence method), the nitrogen content is JIS K 2609 (chemiluminescence method), the bromine value is JIS K 2605, and the aromatic content is The FIA method, open column method, and distillation properties were measured according to JIS K 2254.

  Properties of various hydrocarbon oils corresponding to light slop oil and intermediate product oil are summarized in Table 1.

  In this example, the light slop oil is discharged from each refinery unit, and the hydrocarbon oil is a light oil fraction obtained by atmospheric distillation of Middle Eastern crude oil, hydrocarbon oil 1 and heavy oil. This is hydrocarbon oil 2 which is a mixed oil of 20% by volume of a light gas oil fraction, 55% by volume of a vacuum fraction obtained by distillation of the residual oil under reduced pressure, and 25% by volume of a pyrolysis gas oil fraction.

  Heat of “hydrocarbon oil 1” and “hydrocarbon oil 2” having the properties shown in Table 1 and a mixed oil obtained by mixing 10% by volume of light slop oil with “hydrocarbon oil 1” and “hydrocarbon oil 2”, respectively. Stability evaluation was performed.

  A 500 ml round bottom flask was charged with 500 ml of sample oil and heated to 300 ° C. using a mantle heater in a nitrogen atmosphere. Evaluation was made based on the weight of the filtration residue after heating for 5 hours.

  The results are shown in Table 2. As a result, the residue increased in the mixed oil with the hydrocarbon oil 1 having a low aromatic content. The fouling was reduced when mixed with hydrocarbon oil 2. In the mixing treatment with the oil having a low aromatic content, it is expected that the soiling occurs and the long-term treatment is difficult.

Example 2
Next, the waste oil treatment method in oil refining according to the present invention will be described in more detail with reference to the drawings.

  FIG. 1 shows an overview of one embodiment in a typical oil refining process.

  In the oil refining process shown in FIG. 1, crude oil is continuously supplied from the crude oil tank 100, and desalting, dehydration, and solid content removal are performed by the crude oil desalting apparatus 101. The crude oil leaving the crude oil desalting apparatus 101 is further heated to an appropriate temperature in the heating furnace 102 and fed to the atmospheric distillation tower 103.

  Next, the atmospheric gas distillation column 103 collects the gas component, and distills fractions such as naphtha, kerosene, light oil, and heavy gas oil, and the heavy oil that does not distill as residual oil. To separate. These distillates and residual oil are sent to the processing apparatus 200 for processing, and the final petroleum product is obtained.

  That is, according to the present embodiment, LPG is recovered from the gas component by the gas recovery device 201, and LPG is made into a product. The naphtha is directly used as a petrochemical raw material, subjected to desulfurization treatment by the naphtha hydrorefining device 202, and further reformed by the catalytic reforming device 203 and used for blending gasoline. The kerosene component is desulfurized in the kerosene hydrorefining device 204, and the sulfur and nitrogen components are removed as product kerosene, or refined naphtha is blended into jet fuel.

  Some diesel oil components are used as diesel oil as they are, but many are desulfurized by diesel oil hydrorefining device 205 to remove diesel sulfur diesel diesel oil.

  Further, the heavy gas oil is desulfurized by the gas oil hydrorefining device 215, and the sulfur content is removed to obtain A fuel oil.

  The residual oil may be used as heavy oil as it is, and if necessary, it is blended into product heavy oil such as C heavy oil by desulfurization using a direct desulfurization apparatus, excluding sulfur.

  In addition, the residual oil is distilled under reduced pressure in a vacuum distillation apparatus 206, and separated into a vacuum gas oil that does not contain residual oil and a vacuum residual oil that is a residual oil. The obtained vacuum gas oil is converted into a vacuum desulfurized gas oil that has been desulfurized by the indirect desulfurization device 207, and this vacuum desulfurized gas oil is decomposed by the catalytic cracking device 208 to produce cracked gasoline. Cracked gasoline is blended into product gasoline. The vacuum desulfurized gas oil is blended with A heavy oil.

  Further, the vacuum residue is directly desulfurized by the direct desulfurization apparatus 210 to be C heavy oil. Alternatively, it is pyrolyzed with a heavy oil pyrolyzer 209 to form pyrolyzed oil and petroleum coke. Petroleum coke becomes a product as coke. The pyrolysis oil is used as a raw material for the indirect desulfurization device 207 together with the fraction by-produced in the direct desulfurization device 210.

  In some cases, the residual oil is desulfurized by a direct desulfurization device 210 and then decomposed by a cracking device such as a fluid catalytic cracking device 216 or a thermal cracking device, as shown by a one-dot chain line in FIG. It can have a process of making gasoline and C heavy oil.

  According to the above oil refining process, mixed oil may be produced when the operation of each apparatus is switched, or a product with off-standard properties (off-spec) may be generated. In this case, these oils are collected in a slop tank as slop oil and are not shipped as a product.

  According to the results of the experiments conducted by the present inventors, among the slop oils, according to the distillation properties of the slop oil, the light fraction at 360 ° C. or lower is about 90% by volume, and the heavy fraction at 360 ° C. or higher is 10%. It was found that some of the volume was lighter than the light oil fraction.

  Therefore, in this example, the slop oil was roughly divided into a slop oil composed of a light component (light slop oil) and a slop oil composed of a heavy component (residual oil slop oil). The residual oil slop oil contains a heavier fraction containing vacuum gas oil, and the light slop oil contains a lighter fraction containing light oil.

  In particular, in this embodiment, the light slop oil is generated in the light processing step of processing the atmospheric pressure fraction.

  Accordingly, as described above, the light slop oil has a 90% distillation temperature, preferably 160 to 420 ° C, particularly 180 to 380 ° C, and a 97% distillation temperature, preferably 200 to 380 ° C, particularly 220. ~ 340 ° C.

  Further, according to the present embodiment, as the slop tank, the tank 300 dedicated to the residual oil slop oil and the tank 400 dedicated to the light oil slop oil are provided, and the light oil slop oil and the residual oil slop oil are separated into separate tanks, that is, The residual oil slop oil tank 300 and the light slop oil tank 400 were accepted respectively.

  A feature of the present invention is that a mixed oil obtained by mixing a light slop oil generated in a light treatment step for treating a normal pressure fraction with an intermediate product oil containing 30% by volume or more of an aromatic component is added to the slop oil in the processing apparatus. It is in the configuration for processing. This configuration will be described in more detail later.

  In addition, according to the present embodiment, the residual oil slop oil and the light slop oil are received in the separate tanks 300 and 400, respectively. It can be sent to the atmospheric distillation column 103 via the furnace 102 and processed.

  Next, the light slop oil treatment process will be described.

  In the present embodiment, the light treatment process for treating the atmospheric pressure fraction is a hydrorefining, catalytic reforming, or the like, which treats a fraction mainly composed of naphtha, gasoline, kerosene, light oil or heavy light oil. The residual oil treatment step includes (1) vacuum distillation of atmospheric residual oil, hydrorefining, thermal cracking or catalytic cracking, (2) hydrorefining of vacuum residual oil, heat It can be a process of hydrocracking, hydrocracking, thermal cracking or catalytic cracking of a distillate by distillation under reduced pressure or catalytic cracking or (3) atmospheric residue.

  Further, as described above, the light slop oil is mixed with an intermediate product oil containing an aromatic content of 30% by volume or more, preferably 30 to 60% by volume.

  As described above, the intermediate product oil has a 90% distillation temperature of 450 to 580 ° C., particularly 500 to 550 ° C., preferably 250 to 400 ° C. than that of light slop oil. It is higher by 300 to 350 ° C., and is preferably the heaviest fraction of the atmospheric pressure fraction and / or the fraction derived from the residual oil.

  The heaviest fraction in the atmospheric pressure fraction is a so-called heavy gas oil fraction. Examples of the fraction derived from the residual oil include a vacuum gas oil fraction obtained by distilling the residual oil under reduced pressure, and a cracked oil obtained by pyrolyzing or catalytically cracking the residual oil.

  Cracked light oil which is a fraction containing a large amount of aromatics, that is, (1) catalytic cracked light oil (including so-called “LCO”) obtained by catalytic cracking using residual oil or heavy gas oil as a raw material, (2) An intermediate product oil containing pyrolysis gas oil obtained by pyrolysis using residual oil or heavy gas oil as a raw material is preferred. As described above, the content of the cracked light oil in the intermediate product oil is preferably 5 to 60% by volume, particularly 20 to 50% by volume.

  The mixed oil obtained by blending light slop oil with intermediate product oil preferably has a light slop oil content of 0.1 to 15% by volume, particularly 0.5 to 5% by volume.

  Moreover, it is preferable that the petroleum refining process which processes mixed oil contains at least 1 process of hydrorefining and hydrocracking.

  Since mixed oil does not generate dirt, it is preferable to process it without vaporizing the whole quantity. Preferred reaction conditions are a reaction temperature of 250 to 450 ° C., a reaction pressure of 1 to 25 MPa, particularly a reaction temperature of 300 to 430 ° C., and a reaction pressure of 8 to 25 MPa.

  Further specific description will be given with reference to FIG.

  According to the present embodiment, the light slop oil is processed into a processing apparatus 200 for processing a fraction distilled at atmospheric pressure, for example, a naphtha hydrotreating apparatus 202, a kerosene hydrotreating apparatus 204, a light oil hydrotreating apparatus 205, It is slop oil from the heavy gas oil hydrorefining device 215, the catalytic reforming device 203, and the like.

  According to the present embodiment, the light slop oil a is sent to the heavy oil indirect desulfurization apparatus 207 as a raw material.

  The heavy oil indirect desulfurization unit 207 includes a heavy gas oil fraction b obtained by atmospheric distillation, a vacuum gas oil fraction c obtained from the vacuum distillation unit 206 obtained by vacuum distillation of the residual oil, and a vacuum residual oil. The pyrolyzed light oil fraction d from the heavy oil pyrolyzer 209 obtained by pyrolyzing is supplied as a raw material.

  In this example, the mixed oil containing the heavy gas oil fraction b, the vacuum gas oil fraction c, and the pyrolysis gas oil fraction d corresponds to the “hydrocarbon oil 2” described in Example 1. The proportion of each fraction in the mixed oil was 20% by volume for heavy gas oil fraction b, 55% by volume for vacuum gas oil fraction c, and 25% by volume for pyrolysis gas oil fraction d.

  The light slop oil a corresponds to the “light slop oil” described in Example 1, and as described in Example 1, 10% by volume was mixed with the mixed oil.

  The reaction conditions of the indirect desulfurization apparatus 207 were a reaction temperature of 350 ° C. and a reaction pressure of 8.0 MPa.

  According to this example, in the indirect desulfurization apparatus 207, the entire amount of the mixed oil could be processed without being vaporized, and there was no occurrence of dirt due to the slop oil. This is because the intermediate product oil contains a large amount of aromatics, so that the solubility is high and the occurrence of dirt is suppressed.

  From the above results, it was found that according to the present example, the light slop oil can be used as a part of the intermediate product oil without using the atmospheric distillation raw material.

  According to another embodiment of the present invention, as shown by a one-dot chain line in FIG. 1, it is also possible to send the light slop oil a to the direct desulfurization device 210 for processing the residual oil for processing.

  In this embodiment, slops from the direct desulfurization apparatus 210, the vacuum distillation apparatus 206, the indirect desulfurization apparatus 207, the heavy oil pyrolysis apparatus 209, and the fluid catalytic cracking apparatus 208, which are residual oil treatment steps for treating the residual oil. The “residual slop oil” that is oil can be sent out from the tank 300 to the atmospheric distillation tower 103 via the crude oil desalting apparatus 101 and the heating furnace 102 for processing.

  Therefore, in the present invention, as in the invention described with reference to FIG. 3, the slop oil is treated by distinguishing the residual oil slop oil and the light slop oil according to the generation process. Returning to the atmospheric distillation column 103, the light slop oil is returned to the processing apparatus downstream of the atmospheric distillation column 103, so that all of the conventional slop oil is returned to the atmospheric distillation column 103, The fuel corresponding to the basic unit of the apparatus with respect to the flow rate passing through the atmospheric distillation column 103 can be saved. As a result, energy saving can be achieved, and the emission amount of carbon dioxide can be reduced. In addition, if gasoline or light oil is made sulfur-free or ultra-deep desulfurized, the above-mentioned merit is further increased from the viewpoint of the amount of off-spec products generated.

  In this example, if the ratio of light slop oil to all slop oil is 90% and the ratio of slop oil generated to the crude oil throughput is 2.5%, the amount of crude oil processed annually in Japan is 234. 964,381 KL and the fuel unit required for atmospheric distillation is 9.5 L / KL, which can reduce fuel consumption by 50,789 KL throughout Japan, Generation can be reduced.

It is a diagram which shows the outline | summary of one Example of the oil refinery process which enforces the waste-oil processing method of this invention. It is a diagram which shows the outline | summary of an example of an oil refinery process. It is a diagram which shows the outline | summary of the prior art of the oil refinery process which implements a waste oil processing method.

Explanation of symbols

DESCRIPTION OF SYMBOLS 100 Crude oil tank 101 Crude oil desalination apparatus 102 Heating furnace 103 Atmospheric distillation tower 200 Processing apparatus 201 Gas recovery apparatus 202 Naphtha hydrorefining apparatus 203 Contact reformer 204 Kerosene hydrotreating apparatus 205, 215 Light oil hydrotreating apparatus 206 Depressurization Distillation unit 207 Indirect desulfurization unit 208, 216 Catalytic cracking unit 209 Heavy oil thermal decomposition unit 210 Direct desulfurization unit 300 Residual oil slop oil tank 400 Light slop oil tank

Claims (5)

Crude oil is separated into a residual oil and at least one atmospheric distillation fraction in an atmospheric distillation column, and then the fraction and the residual oil are further processed in a processing apparatus disposed downstream of the atmospheric distillation tower. In a waste oil processing method for processing slop oil generated in an oil refining process to produce a petroleum product by processing in the oil refining process,
The intermediate product oil containing 30% by volume or more of the aromatic content of light slop oil generated in the light treatment step of treating the normal pressure fraction, including the heaviest heavy light oil fraction of the normal pressure fraction. waste oil treatment method with 0.1 to 15 volume% mixed oil mixture, and performing a slop oil treatment in the process unit for processing the residual oil for the. The waste oil treatment method according to claim 1, wherein the light slop oil has a 90% distillation temperature of 160 to 420 ° C, and the intermediate product oil has a 90% distillation temperature of 450 to 580 ° C. The waste oil processing method according to claim 1 or 2, wherein the processing apparatus performs processing without vaporizing the entire amount of the mixed oil. The waste oil treatment method according to any one of claims 1 to 3, wherein the intermediate product oil further includes a fraction derived from residual oil. Fraction derived from the pre-chopped oil in claim 4, characterized in that the vacuum gas oil fraction or bottoms obtained residual oil was distilled under reduced pressure is an exploded oil obtained by pyrolysis or catalytic cracking The waste oil processing method as described .

Images