Method for producing low-chlorine waste plastic oil and / or waste tire oil

Abstract

The invention relates to a method for producing low-chlorine waste plastic oil and / or waste tire oil, waste plastic oil and / or waste tire oil are / is contacted with an extraction agent in an extraction tower for extraction reaction, the extraction agent is a mixture of a reaction reagent and an extraction reagent, a low-chlorine product is extracted from the top of the extraction tower, and the low-chlorine product is extracted from the bottom of the extraction tower. And regenerating a high-chlorine material extracted from the bottom of the extraction tower, and returning part of the regenerated high-chlorine material to the extraction tower as a circulating extraction agent. According to the invention, waste plastic oil and waste tire oil converted by various processes can be treated, chlorine impurities in the waste plastic oil and the waste tire oil can be effectively removed, and high-quality raw materials are provided for subsequent deep processing processes.

Description

Technical Field

[0001] The present invention relates to the technical field of dechlorination of hydrocarbon oil raw materials, and particularly relates to a method for producing low-chlorine waste plastic oil and / or waste tire oil. Background Art

[0002] With the continuous development of the urbanization process in China, the urban population has been increasing year by year, the living standards of the people have been continuously improved, and the output of urban domestic waste has also been increasing. At present, the main methods for treating urban waste include landfill, incineration, etc. There are a series of subsequent environmental protection problems whether it is incineration or landfill.

[0003] Chemical conversion methods can convert plastic waste into valuable industrial raw materials or fuel oil, which can not only eliminate environmental pollution, but also achieve sustainable development and utilization of resources, and is an effective way to control "white pollution". At present, the waste plastic refining industry has spread all over the country, and some enterprises have built small-scale pyrolysis demonstration devices, but the problem of high-value utilization of waste plastic pyrolysis products remains to be effectively solved.

[0004] The waste plastic oil and waste tire oil converted by various processes are quite different from traditional petroleum-based oil products, with high impurity content, especially the chlorine content, which is much higher than that in crude oil. Processing raw materials with high chlorine content using hydrogenation, catalytic and other devices in refineries will seriously corrode the devices, bringing great troubles and safety hazards to subsequent processing.

[0005] Oil dechlorination technology includes two categories. One is to remove inorganic chlorine, and solid adsorbents are used to adsorb hydrogen chloride in the oil. The other is to remove organic chlorine. Usually, the method of hydrogenation can be used to convert organic chlorine into inorganic chlorine and then remove it with an adsorbent. However, when the chlorine content in the raw material is too high, it will bring great safety hazards to high-temperature and high-pressure hydrogenation devices. Therefore, the removal of organic chlorine is the difficulty of oil dechlorination.

[0006] CN102127464A discloses a method for removing organic chlorine from hydrocarbon oil. A demulsifier, an alkaline compound, a phase transfer agent, water injection and hydrocarbon oil are mixed, and under the action of heat and / or electric field, oil-water separation is carried out. The organic chloride is converted into inorganic chloride and removed with the water phase to achieve the purpose of dechlorination. The method of the present invention is applicable to conventional crude oil, heavy crude oil and distillate oil containing organic chlorine.

[0007] CN105885935A discloses a method for removing organic chlorides from wastewater, which includes making the wastewater enter tangentially in a circulating manner to form a swirl and then rise; changing into an upflow to fully fluidize the solid reducing agent or the solid reducing agent particles loaded with a catalyst in the reactor, so that the wastewater and the solid reducing agent or the solid reducing agent particles loaded with a catalyst are in full contact for reaction; after the upflow passes through the main reaction zone, gradually reducing the upward flow velocity of the upflow; the upflow enters the precipitation separation zone, the fluid is approximately laminar flow, and the solid reducing agent or the solid reducing agent particles loaded with a catalyst after reaction effectively settle to remove the organic chlorides in the wastewater. The present invention also provides a device for removing organic chlorides from wastewater. This device is suitable for the mixing reaction of high-density metal particles and wastewater, without scaling, blocking, can operate continuously, the dosage of the reducing agent is adjustable, and the operation and management are simple.

[0008] CN104726134A discloses a method for producing high-quality gasoline and diesel from chlorinated plastic oil. In this method, the chlorinated plastic oil is injected into a high-temperature dechlorination tower filled with activated aluminum oxide for high-temperature dechlorination. A small amount of NaOH aqueous solution is sprayed at the top of the high-temperature dechlorination tower. The plastic oil after dechlorination enters a catalytic distillation tower filled with a molecular sieve / aluminum oxide catalyst for reaction and rectification; after catalytic distillation, the plastic oil enters a hydrofining tower under pressure. The fractionated oil after hydrofining is subjected to atmospheric distillation and cut into gasoline and diesel according to the distillation temperature. The heavy oil at the bottom of the tower is mixed with the raw material chlorinated plastic oil for re-reaction. The dechlorination catalyst and sulfide catalyst used in the present invention are prepared by selecting a suitable method according to the composition and performance of the plastic oil.

[0009] CN104560414A discloses a hydrotreating method for chlorinated catering waste oil. The catering waste oil enters the hydrogenation reactor from the upper part of the hydrogenation reactor, and hydrogen enters the hydrogenation reactor from the lower part of the hydrogenation reactor. Under the hydrogenation reaction conditions, the catering waste oil and hydrogen flow countercurrently through the bed layer containing the hydrogenation catalyst in the hydrogenation reactor; between the bed layers of the hydrogenation reactor, the catering waste oil is divided into multiple strands and enters the hydrogenation reactor. The effluent from the top of the hydrogenation reactor directly enters the dechlorination reactor; under the dechlorination reaction conditions, it passes through the bed layer filled with the dechlorination agent; the effluent from the bottom of the hydrogenation reactor and the effluent from the dechlorination reactor enter the separation system for gas-liquid separation to obtain the hydrorefined oil of the catering waste oil. By using the method provided by the present invention, the problem of chloride ion corrosion in the separation system of the hydrogenation device during the hydrogenation process of the catering waste oil can be effectively solved, and at the same time, the axial temperature difference of the catalyst bed layer can be reduced, and the overall utilization rate of the hydrogenation catalyst can be improved. Summary of the Invention

[0010] The present invention is to solve the technical problems of poor dechlorination effect and high dechlorination cost when processing raw materials of waste plastic oil and / or waste tire oil in the prior art.

[0011] The method for producing low-chlorine waste plastic oil and / or waste tire oil provided by the present invention includes: the waste plastic oil and / or waste tire oil, which are hydrocarbon raw materials, enter the extraction tower from the lower part of the extraction tower and contact with the extractant fed from the upper part of the extraction tower, and an extraction reaction is carried out under certain conditions. The extractant is a mixture of a reaction reagent and an extraction reagent. The reaction reagent is at least one basic compound or salt compound of a Group IA metal, and the extraction reagent is at least one polar organic solvent with a boiling point not lower than 150 °C.

[0012] The low-chlorine material drawn from the top of the extraction tower is the low-chlorine product, and the chlorine content of the low-chlorine product is not greater than 50 μg / g. After the high-chlorine material drawn from the bottom of the extraction tower is regenerated, part of it is returned to the upper part of the extraction tower as a circulating extractant.

[0013] In an embodiment of the present invention, the waste plastic oil is a hydrocarbon material obtained by one or several conversion methods such as thermal cracking, catalytic cracking, and dissolution liquefaction of waste plastics; the distillation range of the waste plastic oil is 30-600 °C, more than 50% of the fractions of the waste plastic oil are less than 350 °C, and the chlorine content is 100-100000 μg / g. In the composition of the waste plastic oil, the volume fraction of olefins is 5-80%, preferably 5-60%, the volume fraction of aromatics is less than 90%, preferably 2-60%, and the volume fraction of paraffins is less than 90%, preferably 5-60%.

[0014] In the present invention, the waste plastics are one or several of waste plastics in fresh domestic waste, waste plastics in industrial and agricultural production, and waste plastics in aged waste, and the types of waste plastics are one or more selected from PE, PP, PS, and PVC.

[0015] In an embodiment of the present invention, the waste tire oil is a hydrocarbon material obtained by one or several conversion methods such as thermal cracking, catalytic cracking, and dissolution liquefaction of waste tires; the distillation range of the waste tire oil is 30-700 °C, more than 50% of the fractions of the waste tire oil are less than 350 °C, and the chlorine content is 100-100000 μg / g. In the composition of the waste tire oil, the volume fraction of olefins is 5-80%, preferably 5-60%, the volume fraction of aromatics is less than 90%, preferably 2-60%, and the volume fraction of paraffins is less than 90%, preferably 5-60%.

[0016] In the present invention, the waste tires are various waste tires made of natural rubber and / or synthetic rubber.

[0017] In the present invention, the thermal cracking reaction refers to the reaction in which hydrocarbon molecules, including waste plastics and waste tires, decompose into smaller molecules under high-temperature conditions and in an air-free environment. In the present invention, the catalytic cracking reaction refers to the reaction in which hydrocarbon molecules, including waste plastics and waste tires, decompose into smaller molecules under high-temperature conditions in the presence of a catalyst. In the present invention, the dissolution and liquefaction reaction refers to the reaction in which waste plastics and waste tires are converted from a solid state to a liquid state in the presence of solvent oil and / or organic solvents.

[0018] In the present invention, the hydrocarbon raw material entering the extraction tower is the whole fraction of waste plastic oil and / or waste tire oil, or any cut fraction. In addition, the extraction dechlorination method of the present invention can be used in any combination with other dechlorination methods, and the other dechlorination methods are not limited to existing dechlorination technologies such as hydrodechlorination and adsorption dechlorination.

[0019] In one embodiment of the present invention, waste plastic oil and / or waste tire oil are cut to obtain a light fraction and a heavy fraction. The cutting point is 100°C to 300°C, preferably 150°C to 250°C, and the obtained light fraction enters the extraction tower for reaction.

[0020] In one embodiment of the present invention, the heavy fraction obtained after cutting is subjected to hydrodechlorination treatment.

[0021] In one embodiment of the present invention, after the waste plastic oil and / or waste tire oil are subjected to extraction dechlorination, the obtained low-chlorine product is subjected to hydrorefining.

[0022] In one embodiment of the present invention, the extraction reagent is one or more selected from ethylene glycol, diethylene glycol, triethylene glycol, glycerol, diglycerol, and ethanolamine.

[0023] In one embodiment of the present invention, the reaction reagent is one or more selected from NaOH, KOH, NaHS, KHS, Na2CO3, and Na2S2O3.

[0024] In one embodiment of the present invention, in the extractant, the mass ratio of the reaction reagent to the extraction reagent is 1:1 to 1:2.

[0025] In one embodiment of the present invention, the molar ratio of the reaction reagent to the chlorine atoms in the hydrocarbon raw material is 1:1 to 20:1.

[0026] In one embodiment of the present invention, the extractant further contains a catalyst, the catalyst is KI, and the dosage of the catalyst is 0.5% to 10% of the raw material mass fraction.

[0027] In one embodiment of the present invention, the extraction tower is any one or a combination of a spray tower, a packed tower, a sieve plate tower, and a rotary tower.

[0028] In one embodiment of the present invention, the extraction reaction conditions are as follows: the top pressure of the tower is 0.01 - 5 MPa, the extraction reaction temperature is 100°C - 350°C, and the mass ratio of the extractant to the hydrocarbon raw material is 0.1 - 10:1. Preferably, the extraction reaction conditions are: the top pressure of the tower is 0.05 - 3 MPa, the extraction reaction temperature is 100°C - 300°C, and the mass ratio of the extractant to the hydrocarbon raw material is 0.3 - 5:1.

[0029] In one embodiment of the present invention, the regeneration process of the high-chlorine material at the bottom of the extraction tower is to separate the inorganic chlorides generated by the reaction by using one or several methods selected from centrifugal separation and filtration. And the high-chlorine material from which the inorganic chlorides are removed is used as a circulating extractant and recycled to the extraction tower.

[0030] Features of the present invention:

[0031] (1) The present invention can process waste plastic oil and waste tire oil converted from various processes, effectively remove their chlorine impurities, and provide high-quality raw materials for subsequent deep processing processes, such as the hydrogenation and catalytic processes for producing vehicle fuels and chemical raw materials.

[0032] (2) The extraction dechlorination method provided by the present invention solves, on the one hand, the problem of low dechlorination rate when using adsorption dechlorination to treat high-chlorine raw materials, and on the other hand, solves the problems of high cost and potential safety hazards caused by chlorine ion corrosion when directly using hydrogenation dechlorination for high-chlorine raw materials.

[0033] (3) The present invention can completely remove the organic chlorine in high-chlorine raw materials by combining with a hydrogenation process, thereby increasing the product value. Description of the Drawings

[0034] Figure 1 It is a schematic diagram of one embodiment of the method for producing low-chlorine waste plastic oil and / or waste tire oil provided by the present invention.

[0035] Figure 2 It is a schematic diagram of one embodiment of the method for producing low-chlorine waste plastic oil and / or waste tire oil provided by the present invention. Detailed Embodiments

[0036] The present invention will be further described below in conjunction with the drawings, but the present invention is not limited thereby.

[0037] Figure 1 It is a schematic diagram of one embodiment of the method for producing low-chlorine waste plastic oil and / or waste tire oil provided by the present invention. As Figure 1As shown in the figure, the waste plastic oil obtained from the waste plastic pyrolysis device 1 enters the extraction tower 3 from the lower part through the pipeline 2, contacts with the extractant fed from the upper part of the extraction tower 3, and undergoes an extraction reaction under certain conditions. The extractant is a mixture of a reaction reagent and an extraction reagent. The low-chlorine material drawn from the top of the extraction tower 3 is taken out as a low-chlorine product through the pipeline 4, and the high-chlorine material at the bottom of the extraction tower 3 enters the regeneration unit 6 through the pipeline 5. After regeneration, part of the high-chlorine material is returned to the upper part of the extraction tower 3 as a circulating extractant through the pipeline 7.

[0038] Figure 2 It is a schematic diagram of one of the embodiments of the method for producing low-chlorine waste plastic oil and / or waste tire oil provided by the present invention. As Figure 2 shown in the figure, the waste plastic oil obtained from the waste plastic pyrolysis device 1 enters the fractionating tower 3 through the pipeline 2 for cutting. The obtained light fraction enters the extraction tower 6 from the lower part through the pipeline 4, contacts with the extractant fed from the upper part of the extraction tower 6, and undergoes an extraction reaction under certain conditions. The low-chlorine material drawn from the top of the extraction tower is taken out through the pipeline 7. The high-chlorine material at the bottom of the extraction tower 6 enters the regeneration unit 9 through the pipeline 8. After regeneration, part of the high-chlorine material is returned to the upper part of the extraction tower 6 as a circulating extractant through the pipeline 10. The heavy fraction obtained by cutting in the fractionating tower 3 enters the hydrogenation unit 12 through the pipeline 5 for hydrodechlorination. The heavy fraction after hydrodechlorination is taken out through the pipeline 13, mixed with the low-chlorine product taken out through the pipeline 7, to obtain low-chlorine hydrocarbon oil, and is taken out through the pipeline 11.

[0039] The present invention will be further described below in conjunction with embodiments, but the present invention is not limited thereby.

[0040] In the embodiment, the chlorine content in the liquid material is determined by the coulomb method. The specific method is the method of "Determination of Total Chlorine Content in Crude Oil by Coulometry" (RIPP 64-90) in "Analysis Methods of Petrochemical Industry" (RIPP Test Methods). The instrument used is a microcoulomb analyzer, and the sample is the liquid material.

[0041] The commercial brand numbers of the hydrogenation catalysts used in the embodiment are RSA-100 and RS-2100, both produced by Sinopec Catalyst Changling Company.

[0042] The hydrocarbon raw materials used include:

[0043] Hydrocarbon raw material 1: Waste plastic oil, chlorine content 3700 μg / g, boiling range 97-481 °C;

[0044] Hydrocarbon raw material 2: Waste plastic oil, chlorine content 109.3 μg / g, boiling range 122-431 °C;

[0045] Hydrocarbon raw material 3: Waste tire pyrolysis oil, chlorine content 127 μg / g, boiling range 27-546 °C.

[0046] Example 1-2

[0047] The hydrocarbon raw material 1 used in this example is waste plastic oil. The hydrocarbon raw material 1 enters the extraction tower from the lower part of the extraction tower, contacts with the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product is drawn from the top of the extraction tower, and the high-chlorine material drawn from the bottom of the extraction tower enters the centrifugal separation unit to separate the inorganic chloride salt generated by the reaction. The high-chlorine material after removing the inorganic chloride salt is used as a circulating extractant for recycling. The extractant used, the process conditions of the extraction tower, and the chlorine content of the low-chlorine product are listed in Table 1. The solvent ratio by mass in Table 1 refers to the mass ratio of the extractant to the hydrocarbon raw material, and the same applies hereinafter.

[0048] Example 3

[0049] The hydrocarbon raw material 2 used in this example is waste plastic oil. The hydrocarbon raw material 2 enters the extraction tower from the lower part of the extraction tower, contacts with the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product is drawn from the top of the extraction tower, and the high-chlorine material drawn from the bottom of the extraction tower enters the centrifugal separation unit to separate the inorganic chloride salt generated by the reaction. The high-chlorine material after removing the inorganic chloride salt is used as a circulating extractant for recycling. The extractant used, the process conditions of the extraction tower, and the chlorine content of the low-chlorine product are listed in Table 1.

[0050] Table 1

[0051]

[0052]

[0053] Example 4

[0054] The hydrocarbon raw material 1 used in this example is waste plastic oil. The hydrocarbon raw material 1 enters the extraction tower from the lower part of the extraction tower, contacts with the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product is drawn from the top of the extraction tower, and the high-chlorine material drawn from the bottom of the extraction tower enters the filtration separation unit to separate the inorganic chloride salt generated by the reaction. The high-chlorine material after removing the inorganic chloride salt is used as a circulating extractant for recycling. The extractant used, the process conditions of the extraction tower, and the chlorine content of the low-chlorine product are listed in Table 2.

[0055] Example 5

[0056] The hydrocarbon raw material 3 used in this example is waste tire oil. The hydrocarbon raw material 3 enters the extraction tower from the lower part of the extraction tower, contacts with the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product is drawn from the top of the extraction tower, and the high-chlorine material drawn from the bottom of the extraction tower enters the filtration separation unit to separate the inorganic chloride salt generated by the reaction. The high-chlorine material after removing the inorganic chloride salt is used as a circulating extractant for recycling. The extractant used, the process conditions of the extraction tower, and the chlorine content of the low-chlorine product are listed in Table 2.

[0057] Table 2

[0058]

[0059]

[0060] Examples 6 - 7

[0061] The hydrocarbon raw material 1 used in this example is waste plastic oil. The hydrocarbon raw material 1 enters the extraction tower from the lower part of the extraction tower, contacts the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product drawn from the top of the extraction tower then enters the hydrogenation unit for hydrorefining to obtain the low-chlorine product after hydrogenation; the high-chlorine material drawn from the bottom of the extraction tower is filtered in the regeneration unit, and part of it is returned to the upper part of the extraction tower as a circulating extractant.

[0062] The extractant used, the process conditions of the extraction tower, the process conditions of the hydrogenation unit, and the chlorine content of the low-chlorine product are listed in Table 3.

[0063] Table 3

[0064]

[0065]

[0066] Examples 8 - 9

[0067] The hydrocarbon raw material 1 used in this example is waste plastic oil. The hydrocarbon raw material 1 enters the fractionating tower for cutting. The obtained light fraction enters the extraction tower from the lower part of the extraction tower, contacts the extractant fed from the upper part of the extraction tower, and undergoes an extraction reaction under certain conditions. The low-chlorine product is drawn from the top of the extraction tower. The high-chlorine material at the bottom of the extraction tower is centrifugally separated and regenerated, and part of it is returned to the upper part of the extraction tower as a circulating extractant. After the heavy fraction obtained by cutting in the fractionating tower is mixed with the low-chlorine product, low-chlorine hydrocarbon oil is obtained.

[0068] The distillation range of the light fraction, the extractant used, the process conditions of the extraction tower, and the chlorine content of the low-chlorine hydrocarbon oil are listed in Table 4.

[0069] Table 4

[0070]

[0071] Examples 10 - 11

[0072] The hydrocarbon raw material 1 used in this embodiment is waste plastic oil. The hydrocarbon raw material 1 enters the fractionating tower for cutting. The obtained light fraction enters the extraction tower from the lower part of the extraction tower and contacts the extractant fed from the upper part of the extraction tower, and an extraction reaction is carried out under certain conditions. The low-chlorine product is drawn from the top of the extraction tower. After the high-chlorine material at the bottom of the extraction tower is centrifugally separated and regenerated, part of it is returned to the upper part of the extraction tower as a circulating extractant. The heavy fraction obtained by the cutting of the fractionating tower enters the hydrogenation unit for hydrodechlorination. After the heavy fraction after hydrodechlorination is mixed with the low-chlorine product, low-chlorine hydrocarbon oil is obtained.

[0073] The distillation range of the light fraction, the extractant used, the process conditions of the extraction tower, the process conditions of the hydrogenation unit, and the chlorine content of the low-chlorine hydrocarbon oil are listed in Table 5.

[0074] Table 5

[0075]

[0076]

Claims

1. A method for producing low-chlorine waste plastic oil and / or waste tire oil, characterized in that Waste plastic oil and / or waste tire oil, as hydrocarbon raw materials, enter the extraction tower from the lower part of the extraction tower, contact with the extractant fed from the upper part of the extraction tower, and carry out an extraction reaction under certain conditions. The extractant is a mixture of a reaction reagent and an extraction reagent. The reaction reagent is at least one basic compound or salt compound of a Group IA metal, and the extraction reagent is at least one polar organic solvent with a boiling point not lower than 150 °C; The low-chlorine material drawn from the top of the extraction tower is a low-chlorine product, and the chlorine content of the low-chlorine product is not greater than 50 μg / g. After the high-chlorine material drawn from the bottom of the extraction tower is regenerated, part of it is returned to the upper part of the extraction tower as a circulating extractant.

2. The method according to claim 1, characterized in that, The waste plastic oil is a hydrocarbon material obtained by one or several conversion methods such as thermal cracking, catalytic cracking, and dissolution liquefaction of waste plastics; the distillation range of the waste plastic oil is 30-600 °C, more than 50% of the fractions in the waste plastic oil are less than 350 °C, and the chlorine content is 100-100000 μg / g; The waste tire oil is a hydrocarbon material obtained by one or several conversion methods such as thermal cracking, catalytic cracking, and dissolution liquefaction of waste tires; the distillation range of the waste tire oil is 30-700 °C, more than 50% of the fractions in the waste tire oil are less than 350 °C, and the chlorine content is 100-100000 μg / g.

3. The method according to claim 1, wherein The extraction reagent is one or more selected from ethylene glycol, diethylene glycol, triethylene glycol, glycerol, triglycol, and ethanolamine.

4. The method according to claim 1, characterized in that, The reaction reagent is one or more selected from NaOH, KOH, NaHS, KHS, Na2CO3, and Na2S2O3; In the extractant, the mass ratio of the reaction reagent to the extraction reagent is 1:1 to 1:2; The molar ratio of the reaction reagent to the chlorine atoms in the hydrocarbon raw material is 1:1 to 20:

1.

5. The method according to claim 1, wherein The extractant also contains a catalyst, the catalyst is KI, and the dosage of the catalyst is 0.5%-10% of the raw material mass fraction.

6. The method according to claim 1, wherein Extraction reaction conditions: the top pressure is 0.01-5 MPa, the extraction reaction temperature is 100 °C-350 °C, and the mass ratio of the extractant to the hydrocarbon raw material is 0.1-10:1; Preferred extraction reaction conditions: the top pressure is 0.05-3 MPa, the extraction reaction temperature is 100 °C-300 °C, and the mass ratio of the extractant to the hydrocarbon raw material is 0.3-5:

1.

7. The method according to claim 1, characterized in that, The regeneration process of the high-chlorine material at the bottom of the extraction tower is to separate the inorganic chlorides generated by the reaction by one or several methods selected from centrifugal separation and filtration.

8. The method according to claim 1, wherein The waste plastic oil and / or waste tire oil are cut to obtain a light fraction and a heavy fraction. The cutting point is 100 °C-300 °C, and the obtained light fraction enters the extraction tower for reaction.

9. The method according to claim 8, wherein The cutting point of the light fraction and the heavy fraction is 150 °C-250 °C.

10. The method according to claim 1, characterized in that The obtained heavy fraction is subjected to hydrodechlorination treatment.

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