A method for producing high-carbon alcohol co-produced with ethanol by using plastic cracking oil

Abstract

This invention discloses a method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil, belonging to the field of waste resource utilization. The invention reacts the olefin double bonds in plastic pyrolysis oil with acetic acid to produce acetate esters. The acetate esters are then hydrogenated, and the resulting reaction product is distilled to yield three materials: ethanol, higher alcohols, and a mixture of saturated hydrocarbons. This invention achieves high-value conversion of plastic pyrolysis oil through esterification and hydrogenation processes. The molar ratio of acetic acid to olefin double bonds is controlled at 1–1.3:1. Esterification uses a sulfonic acid resin catalyst with specific pore size and cross-linking degree to enhance the catalyst's tolerance to impurities in the raw materials. Hydrogenation uses a supported metal catalyst. This invention has advantages such as high conversion rate, good selectivity, long catalyst life, and high product value, and is suitable for the deep processing of waste plastic pyrolysis oil and other waste pyrolysis oils containing double bonds.

Description

Technical Field

[0001] This invention relates to the field of utilization of plastic pyrolysis oil, and more specifically to a method for producing higher alcohols and co-producing ethanol using plastic pyrolysis oil. Background Technology

[0002] With the rapid development of the plastics industry, the disposal of waste plastics has become a major environmental concern. Plastics are primarily composed of polyolefin compounds, but they come in a wide variety of types, including polyethylene, polypropylene, polyvinyl chloride, polystyrene, polyethylene terephthalate, acrylonitrile-butadiene-styrene polymers, nylon, and polylactic acid. Waste plastic processing generally relies on high-temperature pyrolysis and catalytic cracking. However, due to the complexity of waste plastics, the resulting plastic pyrolysis oil has a complex composition, containing large amounts of olefins, alkanes, and aromatics, and exhibits poor stability. Its direct use as fuel has low value, and combustion may cause pollution. Therefore, converting plastic pyrolysis oil into high-value-added chemicals is crucial for the resource utilization of waste plastics.

[0003] Existing methods for utilizing plastic cracking oil mainly focus on refining it into fuel oil or producing low-carbon olefins through cracking and reforming. Research on synthesizing oxygen-containing chemicals from the olefin components is relatively limited. Currently, some studies have established mature processes for the targeted conversion of specific components (such as long-chain olefins) in cracking oil into high-value-added fine chemicals (such as plasticizers).

[0004] Patent CN101724426B discloses a method for producing high-quality diesel blending components from waste plastic pyrolysis oil, which converts waste plastic pyrolysis oil into diesel blending components through fractionation and hydrogenation pretreatment.

[0005] Patent CN106281517B discloses a method for producing clean alcohol fuel from waste plastics or oil made from waste plastics. The method involves vaporizing the oil made from waste plastics at 300-400°C and then counteracting it with water vapor at 150-200°C to generate a mixed alcohol gas. The gas is then fractionated under the action of a catalyst to obtain clean high-carbon alcohol fuel, ensuring that there is no smoke or dust during combustion and that copolymerization does not occur during storage.

[0006] Patent CN116390904A discloses a method for producing higher alcohols from waste plastic raw materials, comprising: (a) providing a pyrolysis oil feed obtained from the pyrolysis of plastic waste, wherein the pyrolysis oil contains at least 20% by weight of higher olefins with a carbon number in the range of C5-C20; (b) contacting the pyrolysis oil with syngas under hydroformylation conditions in the presence of a hydroformylation catalyst and recovering the hydroformylation product; and (c) hydrogenating and / or distilling the hydroformylation product to recover the higher alcohol product.

[0007] In addition, patent CN103664529B discloses a method for co-producing cyclohexanol and ethanol. By carrying out the addition esterification of acetic acid with cyclohexene and the hydrogenation reaction of cyclohexyl acetate in a reactive distillation column, the high energy consumption and pollution problems in the production of cyclohexanol and ethanol are solved, and a high-efficiency and low-cost co-production effect is achieved.

[0008] The existing technology has the following problems: the large amount of olefins in plastic pyrolysis oil is not fully utilized, and its direct use as fuel has low value. Ethanol and higher alcohols (C6+ alcohols) are important chemical raw materials and fuel additives with large market demand. Currently, ethanol is mainly produced through grain fermentation or ethylene hydration, and higher alcohols are mainly produced through carbonyl synthesis or fatty alcohols. Moreover, some processes rely on fossil resources, resulting in high production costs.

[0009] Therefore, developing a process that can efficiently utilize olefin resources in plastic pyrolysis oil while simultaneously producing ethanol and higher alcohols is of great significance for improving the economic value of plastic pyrolysis oil and reducing carbon emissions. Summary of the Invention

[0010] The technical problem this invention aims to solve is to address the issues of low utilization value of existing plastic cracking oil, high production costs of higher alcohols and ethanol, and independent process routes. This invention provides a method for producing higher alcohols and co-producing ethanol from plastic cracking oil. This method features a simple process, high conversion rate, high product value, low hydrogen consumption in the hydrogenation process, and long catalyst lifetime.

[0011] The technical solution adopted in this invention is as follows: A method for producing higher alcohols and co-producing ethanol using plastic cracking oil includes the following steps: (1) Plastic pyrolysis oil is mixed with acetic acid, and a sulfonic acid resin catalyst is added to react and obtain mixture 1 containing acetate ester. The mass content of olefins in the plastic pyrolysis oil is ≥15%. (2) The sulfonic acid resin catalyst was filtered out from the mixture 1 obtained in step (1), and then an appropriate amount of sodium carbonate solution was added to separate the unreacted acetic acid. The separated mixture was then contacted with hydrogen and hydrogenation catalyst to carry out hydrogenation reaction to obtain mixture 2. (3) The mixture 2 obtained in step (2) is separated by distillation to obtain ethanol product, higher alcohol product and saturated hydrocarbon mixture.

[0012] The higher alcohol is a monohydric alcohol or a mixture of polyhydric alcohols with C8 to C20 carbon atoms, and the saturated hydrocarbon mixture is an aliphatic hydrocarbon and / or aromatic hydrocarbon that has not participated in the reaction.

[0013] In step (1), the amount of acetic acid added is such that the molar ratio of acetic acid to the olefin double bond in the plastic pyrolysis oil is in the range of 1 to 1.3:1.

[0014] More preferably, in step (1), the molar ratio of acetic acid to the olefin double bond in the plastic pyrolysis oil is in the range of 1 to 1.2:1.

[0015] Ensure that the olefin double bond can fully react with acetic acid.

[0016] When calculating the molar ratio of feed, the average molecular weight of olefin compounds in plastic pyrolysis oil is selected within the range of 140–224 g / mol.

[0017] According to the analysis of olefin composition in cracked oil, olefins with chain lengths of C10-C16 account for the majority of the olefins, so the average molecular weight of olefins is within the range of C10-C16 straight-chain olefins.

[0018] More preferably, the average molecular weight of the olefin compounds in the plastic pyrolysis oil is selected in the range of 168-196 g / mol.

[0019] More preferably, the average molecular weight of the olefin compounds in the plastic pyrolysis oil is selected in the range of 175-189 g / mol.

[0020] The sulfonate resin catalyst used in step (1) is sulfonated polystyrene microspheres with an acid capacity of 1.5 to 4.8 mmol / g. The amount of sulfonated polystyrene microspheres used is 2 to 4% of the total mass of the plastic pyrolysis oil.

[0021] The sulfonated polystyrene microspheres have a crosslinking degree of 8-12% and a pore size range of 0.3-3 nm.

[0022] More preferably, the pore size is preferably in the range of 0.5 to 2 nm.

[0023] Because of the complex composition of plastic pyrolysis oil, liquid acid catalysts are prone to side reactions such as oxidation with impurities, which can easily lead to tar formation. Sulfonated polystyrene has strong acidic sulfonic acid groups (-SO3H), which can activate double bonds. It also has mild surface properties, better selectivity, and a certain particle size to ensure easy separation from liquid products after the reaction.

[0024] Sulfonated polystyrene microsphere catalysts with specific pore sizes and degrees of crosslinking enhance tolerance to impurities in the feedstock.

[0025] The reaction conditions for step (1) are: reaction temperature 85-160℃, reaction pressure range 0-1.2 MPa, and reaction time 1-4 hours.

[0026] More preferably, the reaction temperature is 100–130°C, the reaction pressure is 0.05–0.1 MPa, and the reaction time is 2–3 h.

[0027] The conversion rate of olefin double bonds after step (1) is greater than 98%.

[0028] The hydrogenation catalyst used in step (2) is a supported metal catalyst. The active metal component is selected from one or more of copper, nickel, platinum, palladium, and ruthenium. The support is selected from one or more of alumina, silicon oxide, titanium dioxide, and activated carbon. The preferred catalyst combination is: copper supported by alumina, copper supported by silicon oxide, nickel supported by alumina, nickel supported by silicon oxide, platinum supported by alumina, platinum supported by silicon oxide, palladium supported by alumina, and palladium supported by silicon oxide.

[0029] The hydrogenation catalyst also contains a co-catalyst, which is selected from one or more oxides of zinc, chromium, manganese, and magnesium, and the mass ratio of the co-catalyst to the active metal component is 0.1 to 1:1.

[0030] The hydrogenation reaction conditions in step (2) are selected according to the type of catalyst: When using a noble metal hydrogenation catalyst, the noble metal (based on elemental content) loading is 0.3–3 wt%, the reaction temperature is 70–110 °C, the reaction pressure is 0.5–2 MPa (gauge pressure), the volume hourly space velocity is 0.2–6 h⁻¹, the hydrogen-ester molar ratio is 5:1–20:1, and the amount of catalyst added is 2%–10% of the mass of the mixed acetate. When using a non-precious metal hydrogenation catalyst, the non-precious metal (calculated as oxide) loading is 8–21 wt%, the reaction temperature is 120–160 °C, the reaction pressure is 0.8–4 MPa (gauge pressure), the volume hourly space velocity is 0.5–5 h⁻¹, the hydrogen-ester molar ratio is 10:1–30:1, and the amount of catalyst added is 3%–20% of the mass of the mixed acetate.

[0031] In step (2), the hydrogenation conversion rate of acetate is greater than 95%, the selectivity of alcohol products is greater than 98%, and the catalyst single-cycle lifetime is greater than 7200 hours. The catalyst after the reaction can be regenerated by hydrogen reduction or inert gas purging.

[0032] The saturated hydrocarbon mixture can be sold directly as fuel oil or returned to the plastic pyrolysis unit for recycling as a diluent.

[0033] The plastic pyrolysis oil is derived from one or more pyrolysis products of waste polyethylene, waste polypropylene, and waste polystyrene.

[0034] Furthermore, the present invention is applicable to the deep processing of olefin-rich mixed oils formed from the pyrolysis of other waste materials.

[0035] Furthermore, the present invention is applicable to the deep processing of mixed oils rich in olefins formed by the pyrolysis of other waste materials such as waste tire pyrolysis oil and biomass pyrolysis oil.

[0036] Compared with the prior art, the beneficial effects of the present invention are as follows: 1. This invention uses a sequential esterification-hydrogenation process to convert the core component olefins of low-value plastic pyrolysis oil into high-value ethanol and higher alcohols, significantly improving the economic benefits of waste plastic treatment. At the same time, unreacted saturated hydrocarbons are recovered as byproducts and can be used as fuel.

[0037] 2. The sulfonic acid resin catalyst used in this invention is non-corrosive, easily separated from the product, and reusable. It also facilitates the better conversion of various olefins in the raw materials into esters. Controlling the degree of crosslinking and pore size of the sulfonic acid resin catalyst within a certain range can enhance its ability to withstand the influence of impurities in the raw materials. Since the presence of halide ions, ash, and inorganic metal ions in the raw materials has a significant impact on the catalyst in the esterification stage, selecting a sulfonic acid resin catalyst with a certain degree of crosslinking and pore size range can maintain high conversion rates and low catalyst consumption without impurity removal.

[0038] 3. This invention can utilize a wide range of molar ratio control (acetic acid: double bond = 1 to 1.3:1) and average molecular weight estimation for feeding, effectively adapting to fluctuations in the molecular weight of olefins in the raw materials (104-280 g / mol). It eliminates the need for extremely stringent single-component separation of the raw materials, reducing pretreatment costs and making it suitable for large-scale industrial processing of mixed waste plastics.

[0039] 4. Wide range of applications: It is not only applicable to plastic pyrolysis oil, but also to other pyrolysis oils rich in olefins, and has good prospects for promotion. Detailed Implementation

[0040] The present invention will be further described below with reference to specific embodiments, but the scope of protection of the present invention is not limited thereto. (1) Plastic pyrolysis oil: Plastic pyrolysis oil 1: derived from the pyrolysis of waste polyethylene and polypropylene.

[0041] Plastic pyrolysis oil 2: derived from the pyrolysis of waste polyethylene, polypropylene, and polystyrene (mainly polyethylene, with a small amount of polystyrene).

[0042] Table 1 below shows the specific indicators of plastic pyrolysis oil. Tables 2 and 3 show the calculation of the olefin composition and average molecular weight in plastic pyrolysis oil. The average molecular weight is calculated based on the molecular weight of straight-chain olefins with the corresponding number of carbon atoms.

[0043] Table 1. Indicators of Plastic Pyrolysis Oil index Plastic pyrolysis oil 1 Plastic pyrolysis oil 2 Total hydrocarbon content (wt%) > 95 > 95 Olefins / (wt%) 52.8 49.6 Alkanes / (wt%) 42.4 25.2 Aromatic hydrocarbons (wt%) 21.5 Impurities (S, N, Cl, etc.) / (wt%) 1 0.81 Table 2 Olefin composition and average molecular weight of plastic pyrolysis oil 1

[0044] Table 3. Olefin composition and average molecular weight of plastic pyrolysis oil 2

[0045] (2) Sulfonated polystyrene Catalyst 1: Acid capacity 3.5 mmol / g, crosslinking degree 10%, average pore size 1.2 nm.

[0046] Catalyst 2: Acid capacity 2.6 mmol / g, crosslinking degree 6%, average pore size 4.5 nm (3) Hydrogenation catalyst Since the type, composition and amount of hydrogenation catalyst have a certain impact on the product higher alcohols, Table 4 below lists the types of hydrogenation catalysts used in specific examples.

[0047] Table 4 Hydrogenation catalysts used in the examples Example Types of hydrogenation catalysts Catalyst composition Example 1 <![CDATA[Cu-Zn / Al2O3 catalyst]]> CuO loading 15 wt%, ZnO:CuO mass ratio 0.3:1 Example 2 <![CDATA[Pd / Al2O3 catalyst]]> Pd loading 1.5 wt% Example 3 <![CDATA[Ni-Mg / Al2O3 catalyst]]> NiO loading 20 wt%, MgO:NiO mass ratio 0.5:1 Example 4 Pd / activated carbon catalyst Pd loading 2.0 wt% Example 5 Cu-Cr / SiO2 <![CDATA[CuO loading is 12 wt%, mass ratio of Cr2O3:CuO is 0.4:1]]> Example 6 Ru-Mn / TiO2 Ru loading 2.0 wt%, MnO:Ru mass ratio 0.8:1 (4) Acetic acid: Acetic acid is commercially available industrial glacial acetic acid.

[0048] (5) Product composition analysis: Gas chromatography-mass spectrometry was used for analysis, and the results were calculated using the area normalization method.

[0049] Example 1 Esterification addition reaction: Take 1000g of plastic pyrolysis oil 1 (calculate the molar amount of olefins based on olefin content and average molecular weight of 185g / mol), add acetic acid, controlling the molar ratio of acetic acid to olefin double bonds to be 1.1:1, and add catalyst 1 (2% of the total mass of reactants). React for 3 hours under normal pressure and 120℃. After the reaction, specifically, use vacuum filtration with a filter paper pore size of 0.45 micrometers. Add 10% sodium carbonate solution to the filtered liquid to adjust the pH of the system to 7.0. Separate the system; unreacted acetic acid reacts with sodium carbonate and enters the aqueous phase. Take a sample of the upper organic phase for analysis, test the olefin content, and calculate the olefin double bond conversion rate. The main product is the corresponding acetate ester.

[0050] Hydrogenation reaction: The above-mentioned mixture containing acetate was mixed with a hydrogenation catalyst (see Table 2), placed in a reactor, and hydrogen gas was introduced. The reaction conditions were: temperature 140℃, pressure 2MPa, space velocity 1.0 h⁻¹. The amount of catalyst used is usually calculated as the mass ratio of catalyst to substrate (ester). In this example, the amount added was 12% of the total acetate mass.

[0051] Separation and purification: After the reaction, the product is filtered to remove the hydrogenation catalyst, and then the filtrate is sent to an atmospheric distillation column for separation. Ethanol is collected from the top of the column, and the mixture at the bottom of the column is sent to a vacuum distillation column to separate higher alcohols and unreacted saturated hydrocarbons. The product composition is analyzed by gas chromatography-mass spectrometry.

[0052] Example 2 Esterification addition reaction: The plastic pyrolysis oil and acetic acid raw materials are the same as in Example 1. The molar ratio of acetic acid to olefin double bond is controlled at 1.3:1. The amount of catalyst is 3% of the total mass of reactants. The reaction temperature is 100℃ and the reaction time is 3 hours.

[0053] Hydrogenation reaction: Catalysts are shown in Table 2. Reaction conditions: temperature 90℃, pressure 1.0 MPa (gauge pressure), space velocity 2.0 h⁻¹, and the amount of catalyst added is 6% of the total acetate mass.

[0054] Separation and purification: Same as in Example 1.

[0055] The results are shown in Table 5.

[0056] Example 3 Esterification addition reaction: The plastic pyrolysis oil and acetic acid feedstock were the same as in Example 1, with the molar ratio of acetic acid to olefin double bonds controlled at 1.2:1. The catalyst dosage was 4% of the total mass of the reactants, the reaction temperature was 130°C, and the reaction time was 1.5 hours.

[0057] Hydrogenation reaction: Catalysts are shown in Table 2. Reaction conditions: temperature 155℃, pressure 3.5 MPa (gauge pressure), space velocity 0.8 h⁻¹, and the amount of catalyst added is 17% of the total acetate mass.

[0058] Separation and purification: The method is the same as in Example 1.

[0059] The results are shown in Table 5. A small amount of excessive hydrogenation produced alkanes, and the proportion of C12+ components in the higher alcohol products was significantly increased.

[0060] Example 4: Esterification addition reaction: 1000g of plastic pyrolysis oil 2 (calculated based on olefin content and average molecular weight of 186g / mol), other conditions were the same as in Example 1. The molar ratio of acetic acid to olefin double bonds was controlled at 1.3:1, and the amount of catalyst added was 2.5% of the total reactant mass. The reaction temperature was 120℃, and the reaction time was 3 hours.

[0061] Hydrogenation reaction: Catalysts are shown in Table 2. Reaction conditions: temperature 105℃, pressure 1.5 MPa (gauge pressure), space velocity 1.5 h⁻¹, and the amount of catalyst added is 8% of the total acetate mass.

[0062] Separation and purification: Same as in Example 1.

[0063] The results are shown in Table 5.

[0064] Example 5:

[0065] Esterification addition reaction: The starting materials were the same as in Example 4, but the molar ratio of acetic acid to olefin double bonds was controlled at 1.15:1, and the amount of catalyst added was 3.5% of the total mass of the reactants. The reaction temperature was 103℃ and the reaction time was 3 hours.

[0066] Hydrogenation reaction: Catalysts are shown in Table 2. Reaction conditions: temperature 130℃, pressure 2.5 MPa (gauge pressure), space velocity 4.0 h⁻¹, and the amount of catalyst added is 15% of the total acetate mass.

[0067] Separation and purification: Same as in Example 1.

[0068] The results are shown in Table 5, demonstrating good performance even at high airspeeds.

[0069] Example 6: Esterification addition reaction: The starting materials were the same as in Example 4, but the molar ratio of acetic acid to olefin double bond was controlled at 1.1:1, and the amount of catalyst added was 3% of the total reactant mass. The reaction temperature was 130℃ and the reaction time was 1.5 hours.

[0070] Hydrogenation reaction: Catalysts are shown in Table 2. Reaction conditions: Temperature 110℃, pressure 2.0 MPa (gauge pressure), space velocity 0.5 h⁻¹, catalyst addition amount is 6% of total acetate mass.

[0071] Separation and purification: Same as in Example 1.

[0072] The results are shown in Table 5. The ruthenium catalyst exhibits excellent long-chain ester hydrogenation activity, and the C16+ component accounts for more than 60% of the obtained high-carbon alcohol product, making it suitable for high-end surfactant raw materials.

[0073] Comparative Example 1: The difference between this comparative example and Example 1 is that the added sulfonated polystyrene catalyst is catalyst 2, which has a lower degree of crosslinking and a larger pore size than catalyst 1. The results are shown in Table 5.

[0074] Comparative Example 2: The difference between this comparative example and Example 4 is that the added sulfonated polystyrene catalyst is catalyst 2, which has a lower degree of crosslinking and a larger pore size range than catalyst 1. The results are shown in Table 5.

[0075] The reduced crosslinking degree of sulfonated polystyrene catalysts leads to increased sensitivity to impurities during the reaction process, decreased activity, and reduced olefin conversion.

[0076] Table 5 Conversion rate and selectivity of the examples Example Double bond conversion rate Acetate hydrogenation conversion rate alcohol selectivity Example 1 98.0% 96.5% 98.2% Example 2 98.2% 97.0% 99.0% Example 3 99.1% 98.2% 96.5% Example 4 98.5% 97.8% 99.5% Example 5 98.7% 95.0% 98% Example 6 98.4% 98.5% 98.8% Comparative Example 1 92.5% 95.8% 98.3% Comparative Example 2 93.2% 97.3% 98.8%

Claims

1. A method for producing higher alcohols and co-producing ethanol using plastic pyrolysis oil, characterized in that, Includes the following steps: (1) Plastic pyrolysis oil is mixed with acetic acid, and a sulfonic acid resin catalyst is added to react and obtain mixture 1 containing acetate ester. The mass content of olefins in the plastic pyrolysis oil is ≥15%. (2) The sulfonic acid resin catalyst was filtered out from the mixture 1 obtained in step (1), and then an appropriate amount of sodium carbonate solution was added to separate the unreacted acetic acid. The separated mixture was then contacted with hydrogen and hydrogenation catalyst to carry out hydrogenation reaction to obtain mixture 2. (3) The mixture 2 from step (2) is separated by filtration and distillation to obtain a mixture of ethanol, higher alcohols and saturated hydrocarbons.

2. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 1, characterized in that, The higher alcohol is a monohydric alcohol or a mixture of polyhydric alcohols with C8 to C20 carbon atoms, and the saturated hydrocarbon mixture is an aliphatic hydrocarbon and / or aromatic hydrocarbon that has not participated in the reaction.

3. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 1, characterized in that, In step (1), the molar ratio of acetic acid to olefin double bonds in plastic pyrolysis oil is 1 to 1.3:

1. When calculating the molar ratio of feed, the average molecular weight of olefin compounds is 140 to 224 g / mol.

4. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 1, characterized in that, The sulfonate resin catalyst used in step (1) is sulfonated polystyrene microspheres. The sulfonated polystyrene microspheres have an acid capacity of 1.5 to 4.8 mmol / g, a crosslinking degree of 8 to 12%, and a pore size range of 0.3 to 3 nm. The amount of sulfonated polystyrene microspheres used is 2 to 4% of the total mass of the plastic pyrolysis oil.

5. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 1, characterized in that, The reaction conditions for step (1) are: reaction temperature 85-160℃, reaction pressure range 0-1.2 MPa, and reaction time 1-4h.

6. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 1, characterized in that, The hydrogenation catalyst used in step (2) is a supported metal catalyst, wherein the active metal component is selected from one or more of copper, nickel, platinum, palladium and ruthenium, and the support is selected from one or more of alumina, silicon oxide, titanium dioxide and activated carbon.

7. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 6, characterized in that, The hydrogenation catalyst also contains a co-catalyst, which is selected from one or more oxides of zinc, chromium, manganese, and magnesium, and the mass ratio of the co-catalyst to the active metal component is 0.1 to 1:

1.

8. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to claim 6 or 7, characterized in that, The hydrogenation reaction conditions in step (2) are selected according to the catalyst type as follows: When using a noble metal hydrogenation catalyst, the noble metal loading is 0.3–3 wt%, the reaction temperature is 70–110 °C, the reaction pressure is 0.5–2 MPa (gauge pressure), and the volume hourly space velocity is 0.2–6 h⁻¹. When using a non-precious metal hydrogenation catalyst, the non-precious metal loading is 8–21 wt%, the reaction temperature is 120–160℃, the reaction pressure is 0.8–4 MPa (gauge pressure), and the volume hourly space velocity is 0.5–5 h⁻¹.

9. The method for producing higher alcohols and co-producing ethanol from plastic pyrolysis oil according to any one of claims 1 to 8, characterized in that, The plastic pyrolysis oil is derived from one or more pyrolysis products of waste polyethylene, waste polypropylene, and waste polystyrene.

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