WO2025100675A1 - Method for conversion of waste plastic pyrolysis oil - Google Patents

Abstract

The method for converting waste plastic pyrolysis oil of the present invention comprises a reaction step of reacting waste plastic pyrolysis oil with hydrogen, wherein the reaction step sequentially performs a first reaction step and a second reaction step, the first reaction step performs impurity removal and a hydrogenation reaction in the presence of a first catalyst, and the second reaction step performs a hydrocracking reaction in the presence of a second catalyst.

Description

Method for converting waste plastic pyrolysis oil

The present invention relates to a method for converting waste plastic pyrolysis oil into a high value-added energy source. More specifically, the present invention relates to a method for converting waste plastic pyrolysis oil into a chemical raw material with a high naphtha content.

In the past, incineration and landfilling were the main methods used to process waste plastic. However, these methods had problems such as the loss of waste generated during the process and the generation of various toxic carcinogens.

To solve this problem, several recycling methods for waste plastics are proposed. Recycling methods are largely divided into mechanical recycling, thermal recycling, and chemical recycling. Among these, chemical recycling is a method of changing the chemical structure of waste plastics through thermal decomposition and chemical reaction processes to convert them into materials that can be used as chemical raw materials. Chemical recycling is evaluated to have many advantages over mechanical recycling, which is evaluated to be not only labor-intensive and resource-intensive but also economically unstable, and thermal recycling, which still causes environmental problems caused by existing incineration methods.

However, in chemical recycling, refined oil or pyrolysis oil obtained through thermochemical decomposition generally has a higher content of impurities such as chlorine, nitrogen, and metals compared to conventional oils refined from petroleum, etc., making it difficult to use it as high value-added fuel or materials such as gasoline or diesel.

To improve these problems, proposed technologies have suggested removing some of the impurities in waste plastic pyrolysis oil or separating it by boiling point and using it as fuel. However, it is difficult to convert it into an efficient high value-added energy source using only these conventional technologies, and in particular, there are clear limitations in converting it into a chemical raw material with a high naphtha content.

Related prior art includes U.S. Patent Application No. 2016-0264885.

The purpose of the present invention is to provide a high value-added hydrocarbon chemical raw material containing a high content of naphtha rather than a fuel oil containing a high content of kerosene, etc., by converting waste plastic pyrolysis oil, and a method for converting the same.

Another object of the present invention is to provide a chemical raw material conversion method capable of removing impurities from waste plastic pyrolysis oil and increasing the yield and quality of olefin conversion and high value-added hydrocarbons.

Another object of the present invention is to provide a method for converting waste plastic pyrolysis oil into chemical raw materials by using an optimized catalyst type, ratio, support, etc. in the conversion process.

The above and other objects of the present invention can all be achieved by the present invention described below.

One aspect of the present invention relates to a method for converting waste plastic pyrolysis oil. The method for converting waste plastic pyrolysis oil includes a reaction step of reacting waste plastic pyrolysis oil with hydrogen, wherein the reaction step sequentially performs a first reaction step and a second reaction step, and in the first reaction step, impurity removal and hydrogenation reaction may be performed under a first catalyst, and in the second reaction step, a hydrogenation cracking reaction may be performed under a second catalyst.

In the above specific example, the first reaction step may be a hydrogenation (HDT) reaction.

In the above specific examples, the hydrogenation reaction is performed at a temperature of about 300° C. to about 400° C., in specific examples from about 330° C. to about 370° C., for example from about 340° C. to about 360° C., and the hydrogenation cracking reaction is performed at a temperature of about 300° C. to about 500° C., in specific examples from about 350° C. to about 470° C., for example from about 400° C. to about 440° C., and the temperature of the hydrogenation cracking reaction may be higher than the temperature of the hydrogenation reaction.

In the above specific examples, the flow rate of the hydrogenation reaction is in the range of about 0.1 to about 5.0, in specific examples from about 0.3 to about 3, for example from about 0.5 to about 1.5, based on LHSV, and the flow rate of the hydrogenation cracking reaction is in the range of about 0.1 to about 5.0, in specific examples from about 0.3 to about 3, for example from about 0.5 to about 2, based on LHSV, wherein the flow rate of the hydrogenation reaction may be the same as or higher than the flow rate of the hydrogenation cracking reaction, and in the above specific examples, the ratio of LHSVs of the first reaction step and the second reaction step may be in the range of about 1.5:1 to about 2.5:1, for example, in the range of about 1.5:1 to about 1.8:1, about 1.8:1 to about 2.1:1, or about 2.1:1 to about 2.5:1.

In the above specific examples, the flow rate of the hydrogenation reaction is in the range of about 100 to about 1000 based on GOR, in specific examples, in the range of about 300 to about 900, for example, in the range of about 500 to about 800, and the flow rate of the hydrogenation cracking reaction is in the range of about 100 to about 1000 based on GOR, in specific examples, in the range of about 300 to about 900, for example, in the range of about 500 to about 800, wherein the flow rate of the hydrogenation reaction based on GOR may be the same as or higher than the flow rate of the hydrogenation cracking reaction based on GOR.

In the above specific example, the first catalyst may include at least one of molybdenum, nickel, cobalt, and tungsten, and the second catalyst may include at least one of molybdenum, nickel, cobalt, and tungsten.

In the above specific example, the first catalyst and the second catalyst may be the same.

In the above specific example, the method for converting the waste plastic pyrolysis oil further includes a separation step for separating hydrogen after the reaction step, and the separation step may be performed sequentially as a high-pressure separation step and a low-pressure separation step.

Another aspect of the present invention relates to a hydrocarbon chemical raw material, wherein said hydrocarbon chemical raw material is produced by the conversion method of the above specific example.

In the above specific examples, the hydrocarbon chemical raw material may have a naphtha content of about 40 wt% or more, for example, about 40 wt% or more but less than about 100 wt%, about 80 wt% or more but less than about 100 wt%, about 90 wt% or more but less than about 100 wt%, about 95 wt% or more but less than about 100 wt%, and a vacuum residue content of less than about 1%, for example, less than 0.8%, less than 0.6%, less than 0.4%.

In the above specific examples, the hydrocarbon chemical raw material may have a naphtha content of about 40 wt% or more, for example, about 40 wt% or more and less than about 100 wt%, about 80 wt% or more and less than about 100 wt%, about 90 wt% or more and less than about 100 wt%, about 95 wt% or more and less than about 100 wt%, and a vacuum gas oil content of less than about 10%, for example, about 7% or less, about 5% or less, or about 3% or less.

In the above specific example, the hydrocarbon chemical raw material may be characterized by having an olefin content of less than about 4 wt%, for example, less than about 3 wt%, less than about 2 wt%.

Another aspect of the present invention relates to a method for removing impurities from waste plastic pyrolysis oil. The method for removing impurities from waste plastic pyrolysis oil may include the conversion method of the above specific example.

Another aspect of the present invention relates to a method for producing a hydrocarbon chemical raw material having a naphtha content of about 40 wt% or more, for example, about 40 wt% or more and less than about 100 wt%, about 80 wt% or more and less than about 100 wt%, about 90 wt% or more and less than about 100 wt%, or about 95 wt% or more and less than about 100 wt%. The method for producing a hydrocarbon chemical raw material having a naphtha content of about 40 wt% or more may include a first reaction step of hydrogenating waste plastic pyrolysis oil and a second reaction step of hydrogenating and cracking the hydrogenated first reaction product.

Another aspect of the present invention relates to a hydrocarbon chemical raw material derived from waste plastic pyrolysis oil. The hydrocarbon chemical raw material comprises light naphtha in an amount of about 10 wt% or more, specifically about 12% to 30%, for example, about 15% to 28%, heavy naphtha in an amount of about 25% to about 40%, specifically about 27% to about 38%, for example, about 29% to 36%, middle distillate (MD) in an amount of less than about 50%, specifically about 1.5 wt% to less than about 50 wt%, for example, about 5 wt% to less than about 45 wt%, about 10 wt% to less than about 40 wt%, about 15 wt% to less than about 30 wt%, vacuum gas oil (VGO) in an amount of less than about 10%, for example, about 7% or less, about 5% or less, about 3% or less, vacuum residue (VR) in an amount of less than about 1%, for example, 0.8 wt%. It may contain less than 0.6 wt%, less than 0.4 wt%.

The present invention provides a hydrocarbon chemical raw material having a high content of high value-added substances such as naphtha and a low content of impurities. The present invention also has the effect of providing a method for efficiently converting waste plastic pyrolysis oil into a hydrocarbon chemical raw material having a high content of high value-added substances and a low content of impurities.

FIG. 1 is a process flow diagram schematically illustrating a process for converting waste plastic pyrolysis oil into hydrocarbon chemical raw materials according to one specific example of the present invention.

Hereinafter, the present invention will be described in more detail. In the case where the terms “includes,” “has,” and “consists of” are used in this specification, other parts may be added unless “only” is used. In the case where a component is expressed in the singular, it includes the case where the plural is included unless there is a specifically explicit description, and it does not exclude additionally unlisted elements, materials, or steps. In the case where the numerical range mentioned in this specification is described as “OO to OO,” it means “OO or more and OO or less” unless there is a specifically explicit description.

When interpreting a component, it is interpreted as including the error range even if there is no separate explicit description.

In this specification, 'waste plastic pyrolysis oil' may be expressed as 'pyrolysis oil', the hydrogenation reaction may be expressed as Hydrotreating or HDT, and the hydrocracking reaction may be expressed as Hydrocracking or HCK. In this specification, LHSV (liquid hourly space velocity) or GOR (gas/oil ratio) are used as units representing flow rates. LHSV is an abbreviation for liquid hourly space velocity and means the ratio of the flow rate of the catalyst entering the reactor and the volume of the catalyst present in the reactor. GOR is an abbreviation for gas/oil ratio and means the volume ratio of the hydrogen gas supplied to the reactor and the waste plastic pyrolysis oil.

Method for converting waste plastic pyrolysis oil into chemical raw materials

Hereinafter, the present invention will be described in detail with reference to the attached drawings so that those skilled in the art can easily practice the present invention. The present invention may be implemented in various different forms and is not limited to the embodiments described herein, and descriptions of well-known functions and configurations that may unnecessarily obscure the gist of the present invention will be omitted.

Figure 1 is a process flow diagram schematically showing a method for converting waste plastic pyrolysis oil according to one specific example of the present invention. The method for converting waste plastic pyrolysis oil according to the present invention includes a step of reacting waste plastic pyrolysis oil and hydrogen, and the reaction step includes a first reaction step and a second reaction step, and in the first reaction step, impurity removal and hydrogenation reaction can be performed, and in the second reaction step, a hydrogenation cracking reaction can be performed.

Input stage

In the injection step according to the present invention, waste plastic pyrolysis oil and hydrogen are injected into a reactor filled with a catalyst. The waste plastic pyrolysis oil and hydrogen may be injected separately or simultaneously through one or more inlets. For example, they may be injected simultaneously for the continuity of the process, or they may be injected through separate inlets depending on the form of the fluid.

The above waste plastic pyrolysis oil refers to a hydrocarbon mixture produced by pyrolyzing waste plastic. Here, the waste plastic may be a polymer compound such as a synthetic resin, a synthetic fiber, a synthetic rubber, vinyl, and solid or liquid impurities related thereto. The hydrocarbon mixture may include various forms of hydrocarbon oil and impurities. Here, the impurities include both metallic and non-metallic impurities, and the metallic impurities may be, for example, one or more of iron, nickel, calcium, magnesium, chromium, zinc, aluminum, and silicon, and the non-metallic impurities may be, for example, one or more of chlorine, nitrogen, sulfur, oxygen, and phosphorus.

Waste plastic pyrolysis oil may contain light naphtha, heavy naphtha, middle distillate (MD), vacuum gas oil (VGO), vacuum residue (VR), and other impurities. In one specific embodiment, light naphtha in the waste plastic is present in an amount of about 4 wt% to about 5 wt%, for example, about 4 wt% to about 4.3 wt%, about 4.3 wt% to about 4.6 wt%, about 4.6 wt% to about 5 wt%, heavy naphtha is present in an amount of about 20 wt% to about 25 wt%, for example, about 20 wt% to about 21.5 wt%, about 21.5 wt% to about 23 wt%, about 23 wt% to about 25 wt%, middle distillate is present in an amount of about 45 wt% to about 50 wt%, for example, about 45 wt% to about 46.5 wt%, about 46.5 wt% to about 48 wt%, about 48 wt% to about 50 wt%, and compressed gas oil is present in an amount of about 20 wt% to about 25 wt%, for example, about 20 wt% to about 21.5 wt %, about 21.5 wt % to about 23 wt %, about 23 wt % to about 25 wt %, the vacuum residue may be included at about 0 wt % to about 3 wt %, for example, about 0.2 wt % to about 1 wt %, about 1 wt % to about 2 wt %, about 2 wt % to about 2.8 wt %. Light naphtha and heavy naphtha contained in waste plastic pyrolysis oil contain paraffin (C5-C30) at about 30 wt% to about 35 wt%, for example, about 30 wt% to about 31.5 wt%, about 31.5 wt% to about 33 wt%, about 33 wt% to about 35 wt%, olefin (C5-C30) at about 35 wt% to about 40 wt%, for example, about 35 wt% to about 36.5 wt%, about 36.5 wt% to about 38 wt%, about 38 wt% to about 40 wt%, naphthenes at about 1 wt% to about 10 wt%, for example, about 1 wt% to about 4 wt%, about 4 wt% to about 7 wt%, about 7 wt% to about 10 wt%, and aromatics at about 10 wt%. % to about 20 wt %, for example, about 10 wt % to about 13 wt %, about 13 wt % to about 16 wt %, about 16 wt % to about 19 wt %, and other carbonates may be contained in an amount of less than about 1 wt %, for example, less than 0.8 wt %, less than 0.6 wt %, less than 0.4 wt %.

The above hydrogen may be introduced in various forms, but according to one specific example of the present invention, it may be introduced in a gaseous state.

Reaction phase

The reaction step includes a first reaction step and a second reaction step, and may further include additional reactions as needed, but the effects of the invention can be achieved with these two types of reactors. There is no limitation on the connection of the first reaction step and the second reaction step, but in order to increase the efficiency of the process, a separate separation process may not be provided between the first reaction step and the second reaction step. The first reaction step and the second reaction step may be connected, for example, in a multi-bed or series manner.

In the first reaction step, impurity removal and hydrogenation reactions can be performed under the first catalyst. The impurity removal and hydrogenation reaction may be a hydrogenation (Hydrotreating, HDT) reaction in which waste plastic pyrolysis oil and hydrogen gas come into contact, and olefins contained in the waste plastic pyrolysis oil are converted into paraffins and other impurities are removed. When the first reaction step is a hydrogenation reaction, the reaction conditions may be performed at about 300° C. to about 400° C., specifically, about 330° C. to about 370° C., for example, about 340° C. to about 360° C., and the pressure may be performed at about 10 bar to about 100 bar, specifically, about 30 bar to about 70 bar, for example, about 40 bar to about 60 bar, and the impurity removal effect and the olefin conversion effect are high within the above range.

In order to maximize the naphtha content, the LHSV of the first reaction region of the above hydrogenation reaction is about 0.1 to about 5, in specific examples about 0.3 to about 3, for example about 0.5 to about 1.5, and the supply volume flow rate ratio of gaseous hydrogen and waste plastic pyrolysis oil GOR may be about 100 to about 1,000, in specific examples about 300 to about 900, for example about 500 to about 800, and within the above range, the impurity removal effect, the olefin conversion effect, and the process efficiency may be improved.

The above first catalyst may be used in various ways as long as it can achieve the purpose of the above reaction. Specific examples thereof include molybdenum, nickel, cobalt, tungsten, etc. In addition, the above catalyst may be used alone or in combination of two or more. For example, NiMo-based catalysts, WMO, PtPd, etc. may be used. When the above catalyst is included, the hydrogenation reaction and impurity removal performance may be improved. The support is also not limited to a specific material, and any one or more of silicon, aluminum, zircon, silicon, magnesium, thorium, beryllium, titanium, carbon black, activated carbon, graphene, carbon nanotubes, and graphite may be used.

In the second reaction step, a hydrogenation cracking reaction can be performed under a second catalyst. In the second reaction step, a hydrogenation cracking reaction is performed. In the case of the hydrogenation cracking reaction, the reaction conditions may be performed at about 300° C. to about 500° C., in specific examples, about 350° C. to about 470° C., for example, about 400° C. to about 440° C., and the pressure may be performed at about 10 bar to about 100 bar, in specific examples, about 30 bar to about 70 bar, for example, about 40 bar to about 60 bar. Within the above range, the naphtha conversion rate is high and high-quality naphtha can be secured.

Meanwhile, according to one specific example of the invention, the hydrogenation cracking reaction is performed at a temperature in the above range, but may be performed at a higher temperature than the first reaction step, and in this case, even if the reactors are connected in a multi-bed manner, a smooth process can be performed, and in this case, a higher naphtha yield can be obtained.

In order to maximize the naphtha content in the final product, the hydrocracking reaction, the LHSV of the second reaction region is about 0.1 to about 5, specifically about 0.3 to about 3, for example about 0.5 to about 2, and the supply volume flow rate ratio of hydrogen gas to the waste plastic pyrolysis oil that has undergone impurity removal and olefin conversion in the first reaction step, GOR, may be about 100 to about 1,000, specifically about 300 to about 900, for example about 500 to about 800, and within the above range, the impurity removal effect, the olefin conversion effect, and the process efficiency may be improved.

In one specific embodiment, the ratio of LHSV of the first reaction step to the second reaction step can be in the range of about 1:1 to about 5:1, for example, in the range of about 1.5:1 to about 2.5:1. In a specific embodiment, the ratio can be in the range of about 1.2:1 to about 4.8:1, for example, in the range of about 1.2:1 to about 2.4:1, in the range of about 2.4:1 to about 3.6:1, in the range of about 3.6:1 to about 4.8:1. The efficiency of the process can be improved within the LHSV ratio range.

The second catalyst may be of various types as long as it can achieve the purpose of the above reaction. Specific examples thereof include molybdenum, nickel, cobalt, tungsten, etc. In addition, the catalyst may be used alone or in combination of two or more. For example, NiMo-based catalysts, WMO, PtPd, etc. may be used. When any one of the above catalysts is included, the hydrogenation reaction and impurity removal performance may be improved. The support is also not limited to a specific material, and any one or more of silicon, aluminum, zircon, silicon, magnesium, thorium, beryllium, titanium, carbon black, activated carbon, graphene, carbon nanotubes, and graphite may be used.

Meanwhile, the first catalyst and the second catalyst may be the same, in which case the efficiency of the process may be increased.

Separation stage

In the separation step, the hydrocarbon chemical raw material and hydrogen that have undergone the above reaction step are separated. The separation step may be performed using a commonly used separation method, for example, a flash drum or a distillation process, and for example, a high-pressure process and a low-pressure process may be performed continuously. The high-pressure process may be performed at about 40 bar to about 100 bar, for example, about 40 bar to about 60 bar, about 60 bar to about 80 bar, or about 80 bar to about 100 bar, and the low-pressure process may be performed at a lower pressure than the high-pressure process, for example, about 1 bar to about 40 bar, in specific examples, about 1 bar to about 14 bar, about 14 bar to about 27 bar, or about 27 bar to about 40 bar. Through the separation step, a hydrocarbon chemical raw material can be obtained.

Hydrocarbon chemical raw materials

Another aspect of the present invention relates to a hydrocarbon chemical raw material. The hydrocarbon chemical raw material is formed from waste plastic pyrolysis oil according to the conversion method. In one embodiment, the hydrocarbon chemical raw material may have a naphtha content of about 40 wt% or more and less than about 100 wt%, and according to one embodiment, about 80 wt% or more and less than about 100 wt%, for example, about 90 wt% or more and less than about 100 wt% or about 95 wt% or more and less than about 100 wt%. The naphtha may include about 10 wt% or more of light naphtha, for example, about 15 wt% to 30 wt%, and about 20 wt% or more of heavy naphtha, for example, about 25 wt% to about 40 wt%. The above light naphtha refers to naphtha having a boiling point of about 30°C to about 90°C at room temperature and pressure, for example, about 30°C to about 50°C, about 50°C to about 70°C, or about 70°C to about 90°C, and the above heavy naphtha refers to naphtha having a boiling point of about 90°C to about 180°C at room temperature and pressure, for example, about 90°C to about 120°C, about 120°C to about 150°C, or about 150°C to about 180°C. The hydrocarbon chemical raw material may contain a middle distillate (MD) of less than about 50 wt%, for example, about 1.5 wt% to less than about 50 wt%, and in specific examples, about 5 wt% to less than about 45 wt%, about 10 wt% to less than about 40 wt%, or about 15 wt% to less than about 30 wt%. The above hydrocarbon chemical raw material may contain vacuum gas oil (VGO) in an amount of less than about 10%, for example, less than about 7%, in specific examples, less than about 5%, or less than about 3%, and vacuum residue (VR) may contain less than about 1 wt%, for example, less than 0.8 wt%, less than 0.6 wt%, or less than 0.4 wt%.

As described above, by using the method according to the present invention, waste plastic pyrolysis oil can be converted to obtain a hydrocarbon chemical raw material having a low impurity content and a high naphtha content.

Hereinafter, the present invention will be described more specifically through examples; however, these examples are for the purpose of explanation only and should not be construed as limiting the present invention.

Examples and Comparative Examples

The waste plastic pyrolysis oil (WPPO) having the composition shown in Table 2 was subjected to the conversion processes of Examples 1 to 3 and Comparative Examples 1 to 3 under the conditions of Table 1, and NiMo catalyst was used as the catalyst. Next, the compositions of the waste plastic pyrolysis oil, Examples, and Comparative Examples are described again in Table 2, and the composition of naphtha in each component is described in Table 3. The evaluation of the composition was performed using gas chromatography (GC) equipment, simulated distillation analysis (SIMDIS) and PONA (Paraffin, Olefin, Naphthene, Aromatic) analysis.

In order to confirm the change in the first reaction stage, the composition of naphtha was confirmed for the intermediate result after the HDT reaction in Example 1 and is recorded as in Table 3.

HDT reaction HCK reaction LHSV
ratio temperature enter LHSV GOR temperature enter LHSV GOR Example 1 350 50 1.0 700 380 50 0.5 700 2 Example 2 350 50 1.0 700 400 50 0.5 700 2 Example 3 350 50 1.0 700 420 50 0.5 700 2 Comparative Example 1 330 50 1.0 700 - - - - - Comparative Example 2 370 50 1.0 700 - - - - - Comparative Example 3 350 50 2.0 700 - - - - - Comparative Example 4 - - - - 380 50 0.5 700 - Comparative Example 5 - - - - 400 50 0.5 700 - Comparative Example 6 - - - - 420 50 0.5 700 -

Ingredient classification Composition ratio (weight%) designation Boiling point (℃) WPPO Example 1 Example 2 Example 3 Comparative Example 4 Comparative Example 5 Comparative Example 6 Light naphtha 30-90 4.8 10.3 47.3 68.3 7.3 17.3 27.3 Chinese naphtha 90-180 23.4 34.8 39.3 29.1 29.0 38.8 43.8 MD 180-343 47.7 47.4 12.8 1.9 47.9 40.8 25.7 VGO 343-524 21.8 6.8 0.6 0.7 14.7 2.2 1.0 VR 524 or more 2.3 0.8 0 0 1.1 0.9 2.2

*Temperature unit is ℃, pressure unit is bar.

*LHSV ratio means LHSV(HDT): LHSV(HCK).

division WPPO
Example 1 (HDT) Example 1 (HDT-HCK) Example 2 (HDT-HCK) Example 3 (HDT-HCK) Comparative Example 1 (HDT) Comparative Example 2 (HDT) Comparative Example 3 (HDT) Paraffin (C5-C30, wt%) 31.8 59.9 59.7 66.6 65.2 59.3 59.4 45.0 Olefin (C5-C30, wt%) 37.4 4.4 3.7 1.9 0.7 4.9 4.5 18.7 Naphthene (wt%) 7 16.6 22 19.7 20.7 16.1 17.4 13.0 Aromatic (wt%) 15.8 19.1 14.2 11.7 13.3 19.7 18.7 23.3 Other (ppm) 865 <0.5 <0.5 <0.5 <0.5 <1 <1 <1

When the reaction temperature of the hydrogenation reaction is 300℃ or higher, the impurity removal efficiency is high and the olefin saturation is also high. When the reaction temperature is 370℃ or higher, similar results are shown as the 350℃ reaction, but the 350℃ process is evaluated to be more desirable in terms of energy efficiency.

It was evaluated that the impurity removal efficiency was particularly desirable when the LHS of the hydrogenation reaction was performed at 2.0 or lower.

Simple modifications or changes of the present invention can be easily implemented by those skilled in the art, and all such modifications or changes can be considered to be included in the scope of the present invention.

The present invention provides a hydrocarbon chemical raw material having a high content of high value-added substances such as naphtha and a low content of impurities. The present invention also has the effect of providing a method for efficiently converting waste plastic pyrolysis oil into a hydrocarbon chemical raw material having a high content of high value-added substances and a low content of impurities.

Claims (15)

As a method for converting waste plastic pyrolysis oil, It includes a reaction step of reacting waste plastic pyrolysis oil and hydrogen. The above reaction steps are performed sequentially in the first reaction step and the second reaction step, In the first reaction step, impurity removal and hydrogenation reaction are performed under the first catalyst, A method for converting waste plastic pyrolysis oil, characterized in that in the second reaction step, a hydrogenation cracking reaction is performed under a second catalyst. A method for converting waste plastic pyrolysis oil, characterized in that in claim 1, the first reaction step is a hydrogenation (HDT) reaction. A method for converting waste plastic pyrolysis oil, characterized in that in the second paragraph, the hydrogenation reaction is performed at a temperature of 300°C to 400°C, the hydrogenation cracking reaction is performed at a temperature of 300°C to 500°C, and the temperature of the hydrogenation cracking reaction is higher than the temperature of the hydrogenation reaction. A method for converting waste plastic pyrolysis oil, characterized in that in the second paragraph, the flow rate of the hydrogenation reaction is 0.1 to 5.0 based on LHSV, and the flow rate of the hydrogenation cracking reaction is 0.1 to 5.0 based on LHSV, and the flow rate of the hydrogenation reaction is equal to or higher than the flow rate of the hydrogenation cracking reaction based on LHSV. A method for converting waste plastic pyrolysis oil in the second paragraph, wherein the ratio of LHSV of the first reaction step and the second reaction step is in the range of 1.5:1 to 2.5:1. A method for converting waste plastic pyrolysis oil, characterized in that in the second paragraph, the flow rate of the hydrogenation reaction is in the range of 100 to 1000 based on GOR, and the flow rate of the hydrogenation cracking reaction is in the range of 100 to 1000 based on GOR, and the flow rate of the hydrogenation reaction based on GOR is equal to or higher than the flow rate of the hydrogenation cracking reaction based on GOR. A method for converting waste plastic pyrolysis oil, characterized in that in claim 1, the first catalyst comprises at least one of molybdenum, nickel, cobalt, and tungsten, and the second catalyst comprises at least one of molybdenum, nickel, cobalt, and tungsten. A method for converting waste plastic pyrolysis oil, characterized in that in claim 7, the first catalyst and the second catalyst are the same. A method for converting waste plastic pyrolysis oil, characterized in that in claim 1, after the reaction step, a separation step for separating hydrogen is further included, wherein the separation step sequentially performs a high-pressure separation step and a low-pressure separation step. Hydrocarbon chemical raw material converted by any one of the conversion methods of claims 1 to 9. In claim 10, the hydrocarbon chemical raw material is characterized in that the naphtha content is 40 wt% or more and the vacuum residue oil content is less than 1%. In claim 10, the hydrocarbon chemical raw material is characterized in that the naphtha content is 40 wt% or more and the vacuum gas oil content is less than 10 wt%. In claim 10, the hydrocarbon chemical raw material is characterized in that the olefin content is less than 4 wt%. A method for producing a hydrocarbon chemical raw material having a naphtha content of 40 wt% or more from waste plastic pyrolysis oil, the method comprising: A first reaction step of hydrogenating waste plastic pyrolysis oil; and A second reaction step of subjecting the hydrogenated first reaction product to a hydrogenation decomposition reaction; A method for producing a hydrocarbon chemical raw material comprising: A hydrocarbon chemical raw material derived from waste plastic pyrolysis oil, containing light naphtha in an amount of 10% or more by weight, heavy naphtha in an amount of 25% to 40%, middle distillate (MD) in an amount of less than 50%, vacuum gas oil (VGO) in an amount of less than 10%, and vacuum residue (VR) in an amount of less than 1% by weight.

Images