A method for producing pyrolysis oil from waste plastics with reduced chlorine content

Abstract

The present disclosure provides a method for producing waste plastic pyrolysis oil with reduced chlorine, comprising a first step of preparing a feed containing 1 to 25 parts by weight of water per 100 parts by weight of waste plastic, and a second step of pyrolyzing the feed at 400 to 600°C.

Description

[Technical field]

[0001] The present disclosure relates to a method for producing waste plastic pyrolysis oil with reduced chlorine. [Background technology]

[0002] Pyrolysis oil obtained by pyrolyzing waste plastics contains higher amounts of impurities such as chlorine, nitrogen, and metals than fractions produced from crude oil using conventional methods. As such, it cannot be immediately used as high-value-added fuels such as gasoline and diesel oil and must go through a refinery process.

[0003] Conventionally, chlorine has been removed by converting it into HCl through hydrotreating in the presence of a hydrogenation catalyst in the refinery process, but waste plastic pyrolysis oil contains a high content of chlorine, and excessive HCl is generated during hydrotreating, which causes problems such as equipment corrosion, reaction abnormalities, and deterioration of product properties. In order to remove the chlorine residue using the conventional refinery process, a Cl reduction pretreatment technology is required that reduces the chlorine content in waste plastic pyrolysis oil to a level that can be introduced into the refinery process.

[0004] In addition, since moisture contained in waste plastics reduces the efficiency of impurity removal during the refinery process and reduces the purity of the pyrolysis oil produced, waste plastics containing moisture have been disposed of during the feed selection process, or the moisture has been removed through pretreatment processes such as drying or dehydration, and then the waste plastics are introduced into a heating furnace for the pyrolysis process. However, there are disadvantages in that the installation of drying equipment or pretreatment equipment such as heaters or blower fans requires additional costs, and a purging process using inert gas such as nitrogen is required, reducing the efficiency of the process.

[0005] Therefore, there is a need for a technology that can use waste plastic feed that contains moisture or has moisture as is without pretreatment processes such as drying, and can economically produce waste plastic pyrolysis oil with reduced chlorine. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] Korean Patent Registration No. 10-1026199 Summary of the Invention [Problem to be solved by the invention]

[0007] The present disclosure aims to provide a method for producing waste plastic pyrolysis oil, which can obtain pyrolysis oil at a high yield by directly using waste plastic feed containing moisture within a specific range without a pretreatment process such as drying, and minimizes the chlorine content in the pyrolysis oil.

[0008] Another object of the present disclosure is to provide a method for producing waste plastic pyrolysis oil, which can reduce equipment costs and utility usage by eliminating the pretreatment / drying process of waste plastic and thereby eliminating the need for a purge process to create an inert atmosphere in the pyrolysis process, thereby improving economic efficiency and process efficiency. [Means for solving the problem]

[0009] The present disclosure provides a method for producing waste plastic pyrolysis oil with reduced chlorine, comprising a first step of preparing a feed containing 1 to 25 parts by weight of water per 100 parts by weight of waste plastic, and a second step of pyrolyzing the feed at 400 to 600°C.

[0010] In one example of the present disclosure, the moisture may include moisture contained in waste plastic.

[0011] In one example of the present disclosure, the second step can be carried out in a non-oxidizing atmosphere.

[0012] In one example of the present disclosure, the non-oxidizing atmosphere may be a water vapor atmosphere formed by pressure purging a reactor with vaporized water vapor.

[0013] In one example of the present disclosure, the second step can be carried out under normal pressure conditions.

[0014] In one example of the present disclosure, the second step can be carried out in a batch reactor.

[0015] In one example of the present disclosure, the total chlorine content in the waste plastic pyrolysis oil produced by the first step and the second step can be 300 ppm or less.

[0016] In one embodiment of the present disclosure, the total chlorine content in the pyrolysis oil produced by the first and second steps can be removed by 80% or more relative to the feed. Effect of the Invention

[0017] According to the present disclosure, by using waste plastic feed containing moisture within a specific range without a pretreatment / drying process, pyrolysis oil can be obtained in a high yield and the chlorine content in the pyrolysis oil can be minimized.

[0018] According to the present disclosure, by eliminating the pretreatment / drying process of waste plastic, a purging process for creating an inert atmosphere in the pyrolysis process is not required, reducing equipment costs and utility usage, thereby improving economic efficiency and process efficiency. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0019] As used herein, the singular forms of the terms "a," "an," and "the" can be construed as including the plural forms as well, unless otherwise indicated.

[0020] Numerical ranges used herein include lower and upper limits, all values ​​within the range, all values ​​that are doubly limited, and all possible combinations of upper and lower limits of numerical ranges limited in different ways. Unless otherwise specified in the present specification, values ​​outside the numerical ranges that may occur due to experimental error or rounding of values ​​are also included in the defined numerical ranges.

[0021] As referred to in this specification, "comprising" is an open-ended term having the same meaning as terms such as "comprising," "containing," "having," "characterized," and the like, and does not exclude further unrecited elements, materials, or steps.

[0022] In this specification, the unit of % used without special reference means % by weight unless otherwise defined.

[0023] The ppm unit used in this specification without special reference means ppm by mass unless otherwise defined.

[0024] The boiling point (bp) used in this specification without any special mention means the boiling point at 1 atmospheric pressure (normal pressure, 1 atm).

[0025] As used herein without any special mention, MpaG is a gauge pressure and means a pressure measured based on 1 atmosphere (normal pressure, 1 atm).

[0026] Conventionally, waste plastics containing moisture are either disposed of during the sorting process or undergo pretreatment processes such as a drying process or dehydration process to remove moisture from the waste plastics, and then introduced into a heating furnace for pyrolysis.

[0027] However, in order to carry out the pretreatment process, additional equipment such as a heater, a hot air dryer, or a blower fan must be installed, which is quite costly, and a purging process using an inert gas such as nitrogen is required, which is disadvantageous in terms of process efficiency.

[0028] In addition, in the conventional refinery process of waste plastic pyrolysis oil, chlorine is converted to HCl and removed by hydrotreating it in the presence of a hydrogenation catalyst. However, waste plastic pyrolysis oil contains a high amount of chlorine, and excessive HCl is generated during hydrotreating, causing problems such as equipment corrosion, abnormal reactions, and deterioration of product properties.

[0029] Therefore, there is a demand for technology that can produce waste plastic pyrolysis oil with reduced chlorine by introducing the feed of waste plastic that contains moisture or has moisture directly into a heating furnace and carrying out the pyrolysis process without any pretreatment process such as drying.

[0030] Therefore, the present disclosure provides a method for producing waste plastic pyrolysis oil with reduced chlorine, comprising a first step of preparing a raw material (feed) containing 1 to 25 parts by weight of moisture per 100 parts by weight of waste plastic, and a second step of pyrolyzing the raw material (feed) at 400 to 600°C.

[0031] The waste plastics can be household plastic waste (domestic waste plastics) or industrial plastic waste (industrial waste plastics).

[0032] The household waste plastic is a plastic mixed with PVC, PS, PET, PBT, etc. other than PE and PP, and specifically, it can be a mixed waste plastic containing 3% by weight or more of PVC together with PE and PP. The chlorine content can be 5,000 ppm or more, specifically 5,000 to 15,000 ppm, per 100 parts by weight of the waste plastic. The household waste plastic can contain moisture in various ranges, and usually contains a high content. For example, it can contain 0.01 to 40% by weight, but this is an example and is not necessarily limited to this.

[0033] The industrial waste plastics are industrial wastes such as scraps and defective products generated during the manufacturing process in industries, and are mostly PE / PP. The chlorine content may be 100 to 1,000 ppm, specifically 500 to 1,000 ppm, more specifically 700 to 1,000 ppm, per 100 parts by weight of the waste plastics. The industrial waste plastics are scraps generated during the manufacturing process, and are relatively clean. They have a low chlorine content compared to domestic waste plastics, and their moisture content is also low, at 0.03% by weight or less. However, they are characterized by a high organic chlorine content resulting from adhesive or dye components, and in particular a high ratio of chlorine contained in aromatic rings.

[0034] The first step is to prepare a feed containing 1 to 25 parts by weight of moisture per 100 parts by weight of waste plastic. The feed can be prepared by adjusting the moisture content within an appropriate range using various methods depending on the composition of the waste plastic.

[0035] In one embodiment of the present disclosure, the moisture may be moisture contained in waste plastic. For example, a feed may be prepared by selecting a household waste plastic that has a moisture content of a certain weight part, such as the household waste plastic. Since household waste plastic with a high moisture content is used as is, a drying process or a dehydration process may be omitted, which is advantageous in terms of improving process efficiency and economy.

[0036] Alternatively, the moisture can be prepared by mixing water with waste plastic. For example, when the moisture content in the waste plastic is extremely low, such as 0.03% by weight or less, a feed containing 1 to 25 parts by weight of moisture per 100 parts by weight of waste plastic can be prepared by mixing a certain amount of water with the waste plastic. The mixing can be performed by a conventionally known method, for example, by feeding the waste plastic feed into a batch reactor and adding a certain amount of water to perform mixing, but this is merely an example and the present disclosure is not necessarily limited thereto.

[0037] In this way, a suitable method can be adopted depending on the composition of the waste plastic to prepare a feed with moisture content adjusted to an appropriate range.

[0038] The second step is a step of pyrolyzing the feed at 400 to 600°C, and the feed containing the waste plastic is converted into a hydrocarbon product. The hydrocarbon product includes a gas phase, and the gas phase pyrolysis gas flows into a condenser, where it is cooled and collected in a storage tank as a liquid phase pyrolysis oil.

[0039] When a feed containing 1-25 parts by weight of water per 100 parts by weight of waste plastic is pyrolyzed at 400-600℃, the chlorine content in the pyrolysis oil produced can be minimized. It has been known that the content of impurities such as chlorine in the pyrolysis oil produced increases as the water content in the waste plastic increases. However, when the water content is in the range of 1-25 parts by weight per 100 parts by weight of waste plastic, the chlorine content in the pyrolysis oil produced can be minimized. Since the chlorine dissociated from the waste plastic during the high-temperature pyrolysis process of the waste plastic is trapped by the water, it is possible to prevent the dissociated chlorine from recombining with the olefin in the pyrolysis product and regenerating organic chlorine. When the range of water weight and pyrolysis temperature is satisfied, the chlorine removal efficiency is maximized and the chlorine content in the generated pyrolysis oil is minimized, and a pyrolysis oil with a high olefin yield and low chlorine content can be produced without adding additives / neutralizers during the reaction or performing separate pre- and post-treatment processes. When the water content exceeds 25 parts by weight, the contact area between the olefin and water in the pyrolysis product increases, and the chlorine content in the pyrolysis oil increases due to the back-mixing effect in which chlorine recombines with the olefin. In addition, excessive water may cause problems such as corrosion of the container or piping and a decrease in the purity and quality of the generated pyrolysis oil. When the pyrolysis temperature is less than 400°C, the moisture in the feed prevents pyrolysis from proceeding smoothly, and the chlorine removal efficiency decreases. Preferably, the temperature range is between 400°C and 600°C, which can prevent the fusion of waste plastics and maximize the yield of pyrolysis oil with minimized chlorine. The water content may be preferably 2 to 25 parts by weight, more preferably 3 to 25 parts by weight, and most preferably 5 to 25 parts by weight, based on 100 parts by weight of the waste plastic.

[0040] The pyrolysis temperature can be specifically 450 to 580°C, more specifically 480 to 550°C.

[0041] In one embodiment of the present disclosure, the second step may be carried out in a batch reactor. Specifically, the second step may be carried out in any reactor capable of stirring and temperature control, for example, a rotary kiln type batch reactor, but the present disclosure is not limited thereto.

[0042] In one example of the present disclosure, the second step can be performed in a non-oxidizing atmosphere. The non-oxidizing atmosphere is an atmosphere in which waste plastics are not oxidized (burned), and efficient pyrolysis can be performed in the non-oxidizing atmosphere. The non-oxidizing atmosphere can be, for example, an atmosphere in which the oxygen concentration is adjusted to 1% by volume or less, and can be an atmosphere of an inert gas such as nitrogen, water vapor, carbon dioxide, and argon. The pyrolysis process can be stably performed in a low-oxygen atmosphere in which the oxygen concentration is adjusted to 1% by volume or less. The second step can be performed for 150 to 350 minutes in a non-oxidizing atmosphere, and when the maintenance time is satisfied, it is preferable that the non-oxidizing atmosphere composition can be activated and sufficient pyrolysis can be performed, and energy consumption and operation time can be minimized. Specifically, it can be 170 to 330 minutes, and more specifically, it can be 200 to 300 minutes.

[0043] In one embodiment of the present disclosure, the non-oxidizing atmosphere may be a water vapor atmosphere formed by pressurizing and purging the reactor with vaporized water vapor. The pyrolysis process of the second step may be performed after uniformly melting the feed containing moisture at 100 to 130°C for 1 to 2 hours in order to improve the reaction efficiency. During this process, water vapor is generated, and oxygen may be removed by pressurizing and purging with the water vapor. That is, there is an advantage that a non-oxidizing atmosphere can be formed by water vapor from the moisture contained in the feed, and a purge process using a separate inert gas is not required.

[0044] In one embodiment of the present disclosure, the second step may be carried out under atmospheric pressure conditions. The pyrolysis reactor of the second step may be operated under atmospheric pressure conditions to obtain a pyrolysis product in high yield, and the reaction may be carried out in an environment with excellent workability and safety.

[0045] Without limitation, the second step pyrolysis reactor may be operated at 0.005-0.3 MPaG and the storage tank at 0.001-0.02 MPaG in order to form a fluid flow and improve reaction efficiency.

[0046] The pyrolysis gas produced by the pyrolysis may contain, based on the total weight, 5-35% by weight of naphtha (bp ~ 150 ° C), 10-60% by weight of Kero (bp 150 ~ 265 ° C), 20-40% by weight of LGO (bp 265 ~ 380 ° C), and 5-40% by weight of UCO-2 / AR (bp 380 ° C ~), specifically, 5-30% by weight of naphtha (bp ~ 150 ° C), 15-50% by weight of Kero (bp 150 ~ 265 ° C), 20-35% by weight of LGO (bp 265 ~ 380 ° C), and 10-40% by weight of UCO-2 / AR (bp 380 ° C ~). In addition, it may contain the remaining amount of low boiling point hydrocarbon compounds such as methane (CH4), ethane (C2H6), and propane (C3H8). The pyrolysis gas may have a weight ratio of light fraction (total of naphtha and Kero) to heavy fraction (total of LGO and UCO-2 / AR) of 0.1 to 3, 0.1 to 2.0, or 0.2 to 1.0.

[0047] Before the pyrolysis gas flows into the condenser, low boiling point gas including low boiling point hydrocarbon compounds such as methane (CH4), ethane (C2H6), and propane (C3H8) can be separately recovered from the pyrolysis gas. The pyrolysis gas generally includes combustible substances such as hydrogen, carbon monoxide, and low molecular weight hydrocarbon compounds. Examples of the hydrocarbon compounds include methane, ethane, ethylene, propane, propene, butane, and butene. Since the pyrolysis gas includes combustible substances, it can be reused as fuel for heating the reactor and the rotary kiln.

[0048] The condenser includes a region where cooling water flows, and the pyrolysis gas flowing into the condenser can be liquefied by the cooling water and converted into pyrolysis oil. When the pyrolysis oil produced in the condenser rises to a predetermined water level, it is transported and collected in a storage tank.

[0049] A heat exchanger may be further provided between the condenser and the storage tank. The pyrolysis gas not condensed in the condenser flows into the heat exchanger and is condensed again, and the generated pyrolysis oil may be collected in the storage tank. By collecting the uncondensed pyrolysis gas again, the reaction yield may be improved.

[0050] The liquid-phase pyrolysis oil collected in the storage tank may contain an oil layer and a water layer. The water vapor generated from the water together with the pyrolysis gas is liquefied and collected in the storage tank, where oil-water separation is performed to form an oil layer and a water layer in the liquid-phase pyrolysis oil.

[0051] The water layer contains chlorine compounds, which may cause corrosion of the storage tank. To prevent this, a neutralizing agent may be added to the water layer. The neutralizing agent may include an alkali metal compound or an alkaline earth metal compound having a pH value of 7 or more when dissolved in water. Specifically, the neutralizing agent may include hydroxides, oxides, carbonates, hydrogen carbonates, basic carbonates, or fatty acid salts of alkali metals or alkaline earth metals. The alkali metals or alkaline earth metals may be metals commonly used in the art. For example, the alkali metals may include lithium (Li), sodium (Na), potassium (K), rubidium (Rb), cesium (Cs), or francium (Fr), and the alkaline earth metals may include beryllium (Be), magnesium (Mg), calcium (Ca), strontium (Sr), barium (Ba), or radium (Ra). The neutralizing agent may be added alone or mixed with a solvent such as alcohol to improve the efficiency of the neutralizing agent.

[0052] When adding a neutralizing agent to the water layer, the pH of the water layer can be measured using a pH meter located at the bottom of the storage tank, so that the neutralizing agent can be added in an appropriate amount.

[0053] When the oil layer and water layer are separated, the oil layer can be collected immediately or after removing the water layer, resulting in an oil layer with minimized chlorine (waste plastic pyrolysis oil). The water layer can be removed by draining, and the drained water can be purified and recycled to the first step to be reused as water to be mixed with waste plastic.

[0054] In order to effectively separate the oil layer and the water layer, an electric field can be applied, and the oil layer and the water layer can be separated in a short time by electrostatic adhesion due to the application of the electric field. In addition, in order to improve the efficiency of the oil-water separation, an additive can be added as necessary, and the additive can be a conventional demulsifier well known in the art.

[0055] When the water layer is drained and removed, a density profiler is used to detect the density, which makes it possible to prevent the oil layer from being removed together with the water layer and to effectively remove only the water layer.

[0056] In one embodiment of the present disclosure, the total chlorine content in the waste plastic pyrolysis oil produced by the first and second steps may be 300 ppm or less. The waste plastic pyrolysis process of the present disclosure can minimize the total chlorine content in the pyrolysis oil produced by only controlling the weight of water and the temperature range without adding additives / neutralizers. Specifically, the total chlorine content may be 290 ppm or less, more specifically, 280 ppm or less. It may be, but is not limited to, 10 to 280 ppm.

[0057] In one embodiment of the present disclosure, the total chlorine content in the pyrolysis oil generated by the first and second steps may be removed by 80% or more relative to the feed. As described above, when the range of the weight of moisture and the pyrolysis temperature is satisfied, the total chlorine content in the generated waste plastic pyrolysis oil can be minimized. The chlorine removal rate can be increased in proportion to the weight of moisture, and can be reduced by 80% or more relative to the feed. Specifically, it can be reduced by 90% or more, and can be reduced, but not limited to, 90% to 97%. When the moisture exceeds 25 parts by weight per 100 parts by weight of waste plastic, the chlorine dissociation efficiency decreases, and the chlorine content in the pyrolysis oil increases, thereby reducing the chlorine removal rate.

[0058] Preferred examples and comparative examples of the present disclosure are described below. However, the following examples are preferred embodiments, and the present disclosure is not limited to the following examples.

[0059] Example 1 A household waste plastic pellet was produced by extruding a household waste plastic mixture containing 3% by weight or more of PVC together with PE and PP at a temperature of 250° C. The total Cl content of the household waste plastic pellet was 4000 ppm, and the moisture content was 0.03% by weight.

[0060] 200g of household waste plastic pellets and 50g of water (approximately 25g of water per approximately 100g of dry weight of waste plastic) were placed in a batch reactor and pyrolyzed at 500°C for 250 minutes. A non-oxidizing atmosphere was created with the water vapor generated during the pyrolysis process of the waste plastic, and the reaction was carried out in a non-oxidizing atmosphere.

[0061] The produced pyrolysis gas was collected in a condenser, and waste plastic pyrolysis oil was obtained in a storage tank.

[0062] Example 2 In Example 1, 40 g of water (approximately 20 g of water per approximately 100 g of dry weight of waste plastic) was added to a batch reactor and pyrolysis oil was performed at 520°C for 250 minutes. The reaction was carried out in the same manner as in Example 1, and waste plastic pyrolysis oil was obtained.

[0063] Example 3 In Example 1, 250 g of household waste plastic pellets containing 20% ​​by weight of moisture (about 25 g of moisture per about 100 g of dry weight of waste plastic) were prepared, and the reaction was carried out at 500° C. without adding additional water, but the same reaction method as in Example 1 was carried out to obtain liquid-phase waste plastic pyrolysis oil. The total Cl content of the household waste plastic was 4,000 ppm.

[0064] Example 4 In Example 3, 250 g of household waste plastic pellets containing 17% by weight of moisture (about 20 g of moisture per about 100 g of dry weight of waste plastic) were prepared, and the reaction was carried out at 540° C., but the same reaction method as in Example 3 was used to obtain waste plastic pyrolysis oil. The total Cl content of the household waste plastic was 4,000 ppm.

[0065] Comparative Example 1 A reaction was carried out under the same conditions as in Example 1, except that 60 g of water (approximately 30 g of water per approximately 100 g of dry weight of waste plastic) was used, to obtain a waste plastic pyrolysis oil.

[0066] Comparative Example 2 A reaction was carried out under the same conditions as in Example 1, except that the reaction was carried out at 300°C, to obtain waste plastic pyrolysis oil.

[0067] Comparative Example 3 In Example 3, 250 g of household waste plastic pellets containing 23% by weight of water (about 30 g of water per about 100 g of dry weight of waste plastic) were used, but the reaction was carried out under the same conditions as in Example 3 to obtain waste plastic pyrolysis oil. The total Cl content of the household waste plastic was 4,000 ppm.

[0068] Comparative Example 4 In Example 1, no additional water was added, and the reaction was carried out under the same conditions as in Example 1 to obtain waste plastic pyrolysis oil.

[0069] Evaluation example The moisture content in the waste plastics was measured using the Karl Fischer method.

[0070] The total chlorine, organic chlorine and inorganic chlorine contents (ppm) in the obtained waste plastic pyrolysis oil were measured by ICP and XRF analysis.

[0071] [Table 1]

[0072] As shown in Examples 1 to 4, it can be seen that the total chlorine content in the waste plastic pyrolysis oil is reduced to 300 ppm or less in all cases. In particular, it can be seen that Example 1 has a lower total chlorine content than Example 2, and Example 3 has a lower total chlorine content than Example 4. This shows that the chlorine in the pyrolysis oil can be reduced more effectively when the moisture content is 25 parts by weight relative to 100 parts by weight of waste plastic than when the moisture content is 20 parts by weight. Furthermore, while moisture is added separately in Examples 1 and 2, moisture is included in the waste plastic in Examples 3 and 4, and in this case, moisture is uniformly included in the waste plastic, and it can be seen that the efficiency of the chlorine removal reaction due to moisture is further improved.

[0073] On the other hand, the total chlorine content in the pyrolysis oil of Comparative Examples 1 and 3 is 382 ppm and 379 ppm, respectively, and it can be confirmed that it increases significantly. Therefore, it can be seen that when the moisture content exceeds 25 parts by weight, the total chlorine content in the pyrolysis oil increases, and it can be confirmed that the total chlorine content is as high as 428 ppm in Comparative Example 4 when pyrolysis is performed in the absence of moisture. It can also be confirmed that not only the total chlorine content but also the organic chlorine and inorganic chlorine contents are excellently reduced in Examples 1 to 4 compared to Comparative Examples 1 to 4.

[0074] In Comparative Example 2, when pyrolysis was performed at 300°C, it was confirmed that the pyrolysis process of the waste plastic did not proceed smoothly, and the yield dropped significantly to 45%. It was also confirmed that the total chlorine content in the pyrolysis oil was 500 ppm or more, and the chlorine removal rate also decreased.

[0075] Although the embodiments of the present invention have been described above, the present invention is not limited to the above embodiments and may be manufactured in various different forms, and a person having ordinary skill in the art to which the present invention pertains can understand that the present invention may be embodied in other specific forms without changing the technical concept or essential features of the present invention.

Claims

1. A first step of preparing a feed containing 100 parts by weight of waste plastic and 1 to 25 parts by weight of water; A second step of pyrolyzing the feed at 400 to 600°C.

2. The method for producing waste plastic pyrolysis oil with reduced chlorine content according to claim 1 , wherein the moisture includes moisture contained in the waste plastic.

3. The method for producing waste plastic pyrolysis oil with reduced chlorine content according to claim 1 , wherein the second step is carried out in a non-oxidizing atmosphere.

4. The method for producing waste plastic pyrolysis oil with reduced chlorine content according to claim 3, wherein the non-oxidizing atmosphere is a water vapor atmosphere formed by purging a reactor with vaporized water vapor under pressure.

5. The method for producing waste plastic pyrolysis oil with reduced chlorine content according to claim 1 , wherein the second step is carried out under normal pressure conditions.

6. The method for producing waste plastic pyrolysis oil with reduced chlorine content according to claim 1, wherein the second step is carried out in a batch reactor.

7. The method for producing waste plastic pyrolysis oil with reduced chlorine as described in claim 1, wherein the total chlorine content in the waste plastic pyrolysis oil produced by the first step and the second step is 300 ppm or less.

8. The method for producing waste plastic pyrolysis oil with reduced chlorine according to claim 1, wherein the total chlorine content in the pyrolysis oil produced by the first step and the second step is removed by 80% or more relative to the feedstock.

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