A zero-carbon emission plastic oil or crude oil processing system and method

Abstract

The application relates to a zero-carbon-emission plastic oil or crude oil processing method, which comprises the following steps: S1, performing atmospheric distillation on plastic oil or crude oil to obtain a low-boiling-point fraction and a high-boiling-point fraction; S2, reacting the low-boiling-point fraction with oxygen to obtain first carbon dioxide and first synthesis gas; S3, converting the first carbon dioxide into synthesis gas to obtain second synthesis gas; S4, converting the first synthesis gas and the second synthesis gas into methanol; and S5, performing a catalytic cracking reaction on the high-boiling-point fraction and the methanol to obtain a cracking target product, wherein the cracking target product comprises low-carbon olefins with carbon atom numbers of 2-3 and components with carbon atom numbers greater than or equal to 4. The application also relates to a zero-carbon-emission plastic oil or crude oil processing system. The zero-carbon-emission plastic oil or crude oil processing system and method described herein can realize zero carbon emission, the energy consumption of the whole system is low, and the utilization rate of carbon resources in raw materials can be greater than or equal to 90%.

Description

Technical Field

[0001] This application relates to the fields of energy conservation and emission reduction, waste plastic recycling and petrochemical technology, specifically to a zero-carbon emission plastic oil or crude oil processing system and method. Background Technology

[0002] Crude oil can be converted into fuels such as gasoline and diesel, as well as basic chemical products such as ethylene, propylene, and aromatics, through processes such as distillation and cracking. However, current crude oil processing suffers from significant drawbacks, including insufficient carbon recovery and the emission of large amounts of the greenhouse gas carbon dioxide. For example, 1) the traditional naphtha steam cracking process yields only 50% of the target product; 2) hydrogenation of residue oil under high temperature and pressure conditions has significantly higher energy consumption and maintenance costs than gasification; 3) the primary and secondary processing of crude oil is complex, with each energy-consuming process emitting CO2 and leading to carbon loss.

[0003] Furthermore, the widespread use of plastics generates a large amount of plastic waste, causing serious environmental pollution. Chemical recycling of waste plastics can turn them into valuable resources. This typically involves catalytic or thermal pyrolysis of the plastics, breaking down the polymer chains to obtain liquid plastic oil. Plastic oil can serve as a substitute for crude oil or be further processed into chemical raw materials with four or fewer carbon atoms. However, current chemical recycling methods for waste plastics, like crude oil processing, also generate significant amounts of the greenhouse gas CO2. Some of this CO2 is produced by the chemical reactions during recycling, while the rest is generated by the operation of the equipment used in the recycling process.

[0004] In a context where the world is striving to reduce carbon dioxide emissions, there is an ongoing need in this field to develop a zero-carbon emission plastic oil or crude oil processing system and method. Summary of the Invention

[0005] The purpose of this application is primarily to provide a zero-carbon emission plastic oil or crude oil processing method that achieves zero carbon emissions and maximizes the utilization of carbon resources in raw materials by converting carbon dioxide into syngas, and can further convert carbon resources into basic chemical products.

[0006] To address the aforementioned technical problems, this application provides the following technical solution.

[0007] In a first aspect, this application provides a method for processing plastic oil or crude oil with zero carbon emissions, the processing method comprising the following steps:

[0008] S1: Distill plastic oil or crude oil at atmospheric pressure to obtain low-boiling-point fractions and high-boiling-point fractions;

[0009] S2: React the low-boiling-point fraction with oxygen to obtain the first carbon dioxide and the first syngas;

[0010] S3: Convert the first carbon dioxide into syngas to obtain the second syngas;

[0011] S4: Convert the first syngas and the second syngas into methanol;

[0012] S5: The high-boiling-point fraction and the methanol are subjected to a cracking reaction to obtain the cracking target product, which includes low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms.

[0013] In one embodiment of the first aspect, the processing method further includes the following step: S6: recovering the second carbon dioxide in the flue gas of the methanol preparation device in step S4 and converting it into the third syngas.

[0014] In one embodiment of the first aspect, the processing method further includes the following step: S7: recovering the third carbon dioxide in the flue gas of the olefin preparation device in step S5 and converting it into the fourth synthesis gas.

[0015] In one embodiment of the first aspect, the processing method further includes converting the third syngas and / or the fourth syngas into methanol.

[0016] In one embodiment of the first aspect, the processing method further includes the following step: S8: reacting the alkane and recycle oil obtained in step S5 when forming the low-carbon olefin with oxygen to obtain a fourth carbon dioxide and a fifth synthesis gas.

[0017] In one embodiment of the first aspect, the processing method further includes converting the fifth synthesis gas into methanol.

[0018] In one embodiment of the first aspect, the processing method further includes the following steps:

[0019] S9: React the component with 4 or more carbon atoms obtained in step S5 with oxygen, or use it as a reaction raw material in step S5.

[0020] In one embodiment of the first aspect, in step S1, after atmospheric distillation of the plastic oil or crude oil, a medium-boiling-point fraction is obtained. The processing method further includes the following step: S10: reacting the medium-boiling-point fraction with hydrogen to obtain jet fuel. Preferably, the reaction temperature of the hydrogenation reaction is 300–500°C, the reaction pressure is 0.3–3.0 MPa, and the space velocity is 0.1–10 h⁻¹. -1 .

[0021] In one embodiment of the first aspect, the pyrolysis reaction in step S5 is carried out at a reaction temperature of 300–600°C, a reaction pressure of 0.05–1.0 MPa, a catalyst-to-oil ratio of 0.1–12, and a space velocity of 1–50 h⁻¹. -1 .

[0022] In a second aspect, this application provides a zero-carbon emission plastic oil or crude oil processing system, the processing system comprising:

[0023] An atmospheric distillation apparatus for separating the plastic oil or crude oil into high-boiling-point fractions and low-boiling-point fractions;

[0024] A gasifier is used to react the low-boiling-point fraction with oxygen to produce carbon dioxide and a first syngas.

[0025] An electrolysis unit is used to convert the carbon dioxide into a second syngas;

[0026] A methanol production unit is used to convert syngas into methanol;

[0027] An olefin preparation apparatus is used to react methanol with the high-boiling fraction to obtain cracking target products, which include low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms.

[0028] In one embodiment of the second aspect, the atmospheric distillation apparatus is used to separate the plastic oil or crude oil into high-boiling-point fractions, medium-boiling-point fractions and low-boiling-point fractions, and the processing system further includes a hydrogenation reaction apparatus for converting the medium-boiling-point fraction into jet fuel.

[0029] In one embodiment of the second aspect, the gasifier is also used to react alkanes and recycled oil obtained during the preparation of low-carbon olefins with oxygen to produce syngas and carbon dioxide.

[0030] In one embodiment of the second aspect, the electrolysis device is further used to convert carbon dioxide generated during the operation of the methanol preparation unit and / or the olefin preparation unit into syngas.

[0031] Compared with the prior art, the positive effects of the present invention are as follows: the zero-carbon emission plastic oil or crude oil processing system and method described herein can achieve zero carbon emissions, and the entire system has low energy consumption and the carbon resource utilization rate in the raw materials can be greater than or equal to 90%. Attached Figure Description

[0032] Figure 1 This application illustrates a zero-carbon emission plastic oil or crude oil processing system according to one embodiment of the present application.

[0033] The meanings of the reference numerals in the attached figures are as follows:

[0034] 1. Atmospheric distillation apparatus; 2. Gasification furnace; 3. Electrolysis apparatus; 4. Methanol preparation apparatus; 5. Olefin preparation apparatus; and 6. Hydrogenation reaction apparatus. Detailed Implementation

[0035] Unless otherwise stated, implied from the context, or as is customary in the art, all parts and percentages in this application are based on weight, and all testing and characterization methods used are concurrent with the filing date of this application. Where applicable, any patent, patent application, or disclosure relating to this application is incorporated herein by reference in its entirety, and its equivalent patent families are also incorporated herein by reference. If any definition of a specific term disclosed in the prior art is inconsistent with any definition provided in this application, the definition provided in this application shall prevail.

[0036] The numerical ranges in this application are approximate values ​​and therefore may include values ​​outside the range unless otherwise stated. A numerical range includes all values ​​from the lower limit to the upper limit, increasing by one unit, provided there is an interval of at least two units between any lower and any higher value. For example, if a component, physical, or other property (such as molecular weight, melt index, etc.) is described as 100 to 1000, this means that all individual values, such as 100, 101, 102, etc., are explicitly listed, as well as all subranges, such as 100 to 166, 155 to 170, 198 to 200, etc. For ranges containing values ​​less than 1 or fractions greater than 1 (e.g., 1.1, 1.5, etc.), one unit is appropriately considered as 0.0001, 0.001, 0.01, or 0.1. For ranges containing single digits less than 10 (e.g., 1 to 5), one unit is generally considered as 0.1. These are merely specific examples of what is intended to be expressed, and all possible combinations of values ​​between the listed minimum and maximum values ​​are considered to be clearly stated in this application. It should also be noted that the terms "first," "second," etc., used herein are not intended to specify a particular order, but are merely used to distinguish substances with different structures.

[0037] When referring to chemical compounds, unless explicitly stated otherwise, the singular includes all isomers, and vice versa. Additionally, unless explicitly stated otherwise, nouns described with "an," "a," or "the" also include their plural forms.

[0038] The terms “comprising,” “including,” “having,” and their derivatives do not exclude the presence of any other components, steps, or processes, regardless of whether such other components, steps, or processes are disclosed in this application. To eliminate any doubt, unless expressly stated otherwise, all compositions using the terms “comprising,” “including,” or “having” in this application may contain any additional additives, excipients, or compounds. Conversely, except for those necessary for operational performance, the term “substantially constitutes…” excludes any other components, steps, or processes described below with respect to that term. The term “consisting of…” does not include any components, steps, or processes not specifically described or listed. Unless expressly stated otherwise, the term “or” refers to the individual members listed or any combination thereof.

[0039] Reducing carbon dioxide emissions, and even achieving zero carbon emissions, is a common challenge faced by the petrochemical and waste plastics recycling industries. This application achieves zero carbon emissions by converting carbon dioxide into syngas. The syngas can be further converted into methanol, which, after olefinization, yields basic chemical products such as olefins.

[0040] Next, we will combine Figure 1 This document describes the zero-carbon emission plastic oil or crude oil processing system and method described herein.

[0041] refer to Figure 1 The zero-carbon emission plastic oil or crude oil processing system described herein may include an atmospheric distillation unit 1, a gasification furnace 2, an electrolysis unit 3, a methanol preparation unit 4, and an olefin preparation unit 5. In this embodiment, the atmospheric distillation unit 1 can be used to separate plastic oil or crude oil into high-boiling-point fractions, medium-boiling-point fractions, and low-boiling-point fractions. The gasification furnace 2 can be used to react the low-boiling-point fractions with oxygen to obtain carbon dioxide and a first syngas. The electrolysis unit 3 can be used to convert the carbon dioxide into a second syngas. The methanol preparation unit 4 can be used to convert the syngas into methanol. The olefin preparation unit 5 is used to react methanol with the high-boiling-point fractions to obtain low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms.

[0042] In one specific embodiment, the atmospheric distillation apparatus 1 can be an atmospheric distillation column, which can separate crude oil, plastic oil, or other plastic oils or crude oil according to their different boiling points to obtain high-boiling-point fractions, medium-boiling-point fractions, and low-boiling-point fractions. In one specific embodiment, the main component of the high-boiling-point fraction is the fraction with an Engler distillation range ≥300℃. In one specific embodiment, the main component of the low-boiling-point fraction is naphtha fraction. In one specific embodiment, the main components of the medium-boiling-point fraction are the first-stage and second-stage atmospheric distillation fractions.

[0043] In one specific embodiment, a gasifier 2 is used instead of a conventional steam cracking furnace to crack low-boiling-point fractions. The carbon resource utilization rate of the gasifier process is almost 100m%, while the yield of steam cracking is only about 10m% (CH4). Methane can only be used as fuel in the cracking furnace, releasing a large amount of CO2 into the atmosphere and simultaneously producing a large amount of carbon-containing products that cannot be further efficiently converted, resulting in a significantly lower yield of low-carbon olefins. For example, the low-carbon olefin yield of naphtha steam cracking is about 48m%, while the combined gasification and methanol cracking process has a low-carbon olefin yield of no less than 90m%. In addition, the energy consumption of the gasifier 2 production process is also significantly different. For example, gasification in the gasifier 2 is an exothermic process, while the cracking reaction in the steam cracking furnace is a strongly endothermic process.

[0044] In one specific embodiment, the electrolysis device 3 described herein can convert CO2 in the flue gas of this system into syngas, which will further improve the utilization rate of carbon resources and increase the yield of low-carbon olefins. The electrocatalytic device 3 can perform CO2 conversion under normal temperature and pressure conditions, meaning the hydrogenation reaction can be carried out at normal temperature and pressure. Compared with conventional high-pressure hydrogenation of wax oil and residue oil, the investment, maintenance, and energy consumption for carbon dioxide conversion using an electrolysis device are significantly reduced. It should be further noted that the carbon dioxide input to the electrolysis device 3 is not limited to CO2 in the flue gas of this system, but may also include CO2 generated in oil refining and coal chemical processes, thereby achieving zero-carbon emissions in oil refining and coal chemical processes.

[0045] In one specific embodiment, the methanol preparation device 4 described herein is not particularly limited, as long as it can convert syngas into methanol.

[0046] In one specific embodiment, the olefin preparation unit 5 is a highly selective olefin unit, such as a fluidized bed reactor. The bottom product from the atmospheric distillation unit 1 and methanol are fed into the fluidized bed reactor of the olefin preparation unit 5 for cracking reactions, yielding the target cracking products. These target cracking products include low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms. The low-carbon olefins with 2-3 carbon atoms mainly include ethylene and propylene. In a preferred embodiment, the target cracking products can be separated to obtain basic chemical products such as ethylene and propylene. Components with 4 or more carbon atoms can be returned to the olefin preparation unit 5 or to the gasifier 2. In a preferred embodiment, all target cracking products other than ethylene and propylene can be returned to the gasifier 2. These other target cracking products may include, for example, methane, ethane, propane, butane, gasoline, diesel, and recycled oil, slurry oil, etc. In a preferred embodiment, the fluidized bed pyrolysis reaction is carried out at a temperature of 300–600°C, a reaction pressure of 0.05–1.0 MPa, a catalyst-to-oil ratio of 0.1–12, and a space velocity of 1–50 h⁻¹. -1 .

[0047] In one embodiment, the zero-carbon emission plastic oil or crude oil processing system described herein may further include a hydrogenation reactor 6 for converting the medium-boiling fraction obtained from the atmospheric distillation unit 1 into jet fuel. In a specific embodiment, the hydrogenation reactor 6 may be a fixed-bed hydrogenation reactor with a reaction temperature of 300–500°C, a reaction pressure of 0.3–3.0 MPa, and a space velocity of 0.1–10 h⁻¹. -1 .

[0048] Next, the connection relationships between the above-mentioned devices will be described in detail. For example... Figure 1 As shown, the atmospheric distillation unit 1 can be connected to the gasification furnace 2, which supplies the separated low-boiling-point fraction to the gasification furnace 2. The low-boiling-point fraction reacts with oxygen in the gasification furnace 2 to produce first carbon dioxide and syngas, which is a mixture of carbon monoxide and hydrogen. The gasification furnace can be connected to the electrolysis unit 3, which supplies the first carbon dioxide to the electrolysis unit 3. After processing by the electrolysis unit 3, the first carbon dioxide yields second syngas. Both the gasification furnace 2 and the electrolysis unit 3 can be connected to the methanol preparation unit 4, supplying the first and second syngas to the methanol preparation unit 4, where they are converted into methanol. The methanol preparation unit 4 can be connected to the olefin preparation unit 5, supplying methanol to the olefin preparation unit 5. Simultaneously, the atmospheric distillation unit 1 can also be connected to the olefin preparation unit 5, supplying the high-boiling-point fraction to the olefin preparation unit 5. Methanol and the high-boiling-point fraction can undergo a cracking reaction in the olefin preparation unit 5 to obtain the cracking target product. The cracking target product is then separated to obtain the desired target product.

[0049] In addition, the olefin preparation unit 5 can be connected to the gasifier 2 to transport other cracking products from the olefin preparation unit 5, excluding ethylene, propylene and butene, to the gasifier 2.

[0050] In one specific embodiment, the methanol preparation device 4 can be connected to the electrolysis device 3 to transport the second carbon dioxide from the flue gas of the methanol preparation device 4 to the electrolysis device 3, where it is processed to obtain the third syngas. Similarly, the olefin preparation device 5 can be connected to the electrolysis device 3 to transport the third carbon dioxide from the flue gas of the olefin preparation device 5 to the electrolysis device 3, where it is processed to obtain the fourth syngas. Preferably, the third and fourth syngas can be further transported to the methanol preparation device 4 and converted into methanol in the methanol preparation device 4.

[0051] In one specific embodiment, the atmospheric distillation apparatus 1 can also be connected to the hydrogenation reaction apparatus 6 to supply a medium-boiling fraction to the hydrogenation reaction apparatus 6. The medium-boiling fraction reacts with hydrogen in the hydrogenation reaction apparatus 6 to obtain jet fuel.

[0052] The following section will describe in detail the zero-carbon emission plastic oil or crude oil processing method described in this article.

[0053] In one specific embodiment, the processing method includes the following steps: S1: Distilling plastic oil or crude oil under atmospheric pressure to obtain a low-boiling-point fraction and a high-boiling-point fraction; S2: Reacting the low-boiling-point fraction with oxygen to obtain a first carbon dioxide and a first syngas; S3: Converting the first carbon dioxide into syngas to obtain a second syngas; S4: Converting the first syngas and the second syngas into methanol; S5: Performing a cracking reaction on the high-boiling-point fraction and the methanol to obtain a cracking target product, which includes low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms. In one specific embodiment, the reaction temperature of the cracking reaction in step S5 is 300-600°C, the reaction pressure is 0.05-1.0 MPa, and the space velocity is 1-50 h⁻¹. -1 .

[0054] In the zero-carbon emission plastic oil or crude oil processing method described in this article, a step of converting carbon dioxide into syngas is added, thereby turning carbon dioxide waste into treasure. On the one hand, carbon dioxide emissions are reduced, and on the other hand, the yield of the target product, low-carbon olefins, is increased, thus maximizing the utilization of carbon resources.

[0055] To further maximize the utilization of carbon resources, the processing method described herein further includes the following step: S6: recovering the second carbon dioxide from the flue gas of the methanol preparation unit in step S4 and converting it into a third syngas. Further, the processing method described herein also includes the following step: S7: recovering the third carbon dioxide from the flue gas of the olefin preparation unit in step S5 and converting it into a fourth syngas. Preferably, the third syngas and / or the fourth syngas can be further converted into methanol.

[0056] These two steps can recover carbon dioxide from the flue gas of methanol preparation unit 4 and olefin preparation unit 5, respectively, adding an extra carbon source for the reaction feedstock, so that the carbon resource recovery rate of the entire system exceeds 100%.

[0057] In one specific embodiment, the processing method described herein further includes the following step: S8: reacting the alkane and recycled oil obtained in step S5 during the formation of the low-carbon olefin with oxygen to obtain a fourth carbon dioxide and a fifth syngas. Preferably, the fifth syngas is converted into methanol.

[0058] In one specific embodiment, the processing method described herein further includes the following step: S9: reacting the component with 4 or more carbon atoms obtained in step S5 with oxygen, or using it as a reaction raw material in step S5.

[0059] Both steps S8 and S9 can improve the utilization rate of carbon resources.

[0060] In one specific embodiment, in step S1, after atmospheric distillation of plastic oil or crude oil, a medium-boiling-point fraction is obtained. The processing method further includes the following step: S10: reacting the medium-boiling-point fraction with hydrogen to obtain jet fuel. As mentioned above, the reaction temperature of the hydrogenation reaction is 300–500°C, the reaction pressure is 0.3–3.0 MPa, and the space velocity is 0.1–10 h⁻¹. -1 .

[0061] Example

[0062] The technical solution of this application will be clearly and completely described below with reference to the embodiments of this application. Unless otherwise specified, the reagents and raw materials used can be purchased commercially. Experimental methods in the following embodiments that do not specify specific conditions are performed according to conventional methods and conditions, or according to the product instructions.

[0063] Example 1

[0064] In this embodiment, plastic oil is used as raw material. The density and distillation range of the plastic oil are shown in Table 1. The group composition, carbon residue and viscosity analysis data of the plastic oil are shown in Table 2. The elemental and metal analysis data of the plastic oil are shown in Table 3.

[0065] Table 1 Density and distillation range of plastic oils

[0066] Density (20℃) <![CDATA[g / cm 3 ]]> 0.832 0.858 Distillation range (ASTM D1160) Initial boiling point ℃ 133.0 139.0 10％ ℃ 240.0 276.5 30％ ℃ 359.0 386.5 50％ ℃ 435.5 469.0 70％ ℃ 510.0 546.0 95％ ℃ * * Distillation yield at 350℃ ％ 28.6 22.4 Distillation yield at 500℃ ％ 77.5 68.3 Flash point ℃ 42 55

[0067] Table 2. Analysis data of group components, carbon residue, and viscosity of plastic oils.

[0068]

[0069]

[0070] Table 3. Elemental and metal analysis data of plastic oils

[0071] S m％ 0.028 0.0312 Total N μg / g 390 392 Base N μg / g 53.3 54.7 Cl μg / g 356.6 281.1 Si μg / g 175 257 sodium μg / g 22 11 iron μg / g 290 253 vanadium μg / g 0.2 0.2 nickel μg / g 1.5 1.5

[0072] The plastic oil or crude oil processing system described in this paper is used to process plastic oil. The process parameters of each device are shown in Table 7, and the target product recovery rate is shown in Table 8.

[0073] Example 2

[0074] In this embodiment, crude oil is used as raw material. The density and distillation range of crude oil are shown in Table 4. The group composition, carbon residue and viscosity analysis data of crude oil are shown in Table 5. The elemental and metal analysis data of crude oil are shown in Table 6.

[0075] Table 4 Density and Distillation Range of Crude Oil

[0076] Density (20℃) <![CDATA[g / cm 3 ]]> 0.8666 0.8346 Distillation range (ASTM D1160) Initial boiling point ℃ ≯15 ≯15 10％ ℃ 165.0 106.0 30％ ℃ 320.0 198.8 50％ ℃ 415.5 285.7 70％ ℃ 530.0 410.2 95％ ℃ * 520.5 Distillation yield at 350℃ ％ 38.5 63.4 Distillation yield at 500℃ ％ 65.0 90.8 Flash point ℃ ≯36 ≯25

[0077] Table 5. Analysis data of group components, carbon residue, and viscosity of crude oil.

[0078] Saturated hydrocarbons ％ 24.9 11.7 Aromatics ％ * * gelatin ％ 14.3 5.7 Asphalt ％ ≯0.1 ≯0.2 Carbon residue ％ 4.97 3.93 Ash ％ * * Viscosity (50℃) <![CDATA[mm 2 / s]]> 26.50 6.373 Viscosity (100℃) <![CDATA[mm 2 / s]]> 10.15 * Pour point ℃ 34 22 Flash point ℃ ≯36 ≯25

[0079] Table 6 Elemental and Metallic Analysis of Crude Oil

[0080] S m％ 0.34 0.16 Total N μg / g 2800 1000 Base N μg / g * * Cl μg / g 10 934.6 Si μg / g * * sodium μg / g 3.9 2.5 iron μg / g 8.7 0.8 vanadium μg / g 0.4 0.2 nickel μg / g 14.0 3.8

[0081] The zero-carbon emission plastic oil or crude oil processing system described in this paper is used to process crude oil. The process parameters of each device are shown in Table 7, and the target product recovery rate is shown in Table 8.

[0082] Table 7. Process parameters of each piece of equipment in Examples 1-2

[0083]

[0084]

[0085] Table 8. Recovery rates of target products in Examples 1-2

[0086] ethylene 45％ 44％ propylene 53％ 50％ Carbon resource utilization rate 98％ 94％

[0087] As can be seen from the above embodiments, the plastic oil or crude oil processing system described herein does not require high pressure, significantly reducing the energy consumption of the entire process, and the carbon resource recovery rate is higher than 94%.

[0088] The above description of the embodiments is intended to enable those skilled in the art to understand and apply this application. It will be apparent to those skilled in the art that various modifications can be easily made to these embodiments, and the general principles described herein can be applied to other embodiments without creative effort. Therefore, this application is not limited to the embodiments described herein, and any improvements and modifications made by those skilled in the art based on the disclosure of this application without departing from the scope and spirit of this application are within the scope of this application.

Claims

1. A method for processing plastic oil or crude oil with zero carbon emissions, characterized in that, The processing method includes the following steps: S1: Distill plastic oil or crude oil under atmospheric pressure to obtain low-boiling-point fraction, medium-boiling-point fraction and high-boiling-point fraction; S2: React the low-boiling-point fraction with oxygen to obtain the first carbon dioxide and the first syngas; S3: Convert the first carbon dioxide into syngas to obtain the second syngas; S4: Convert the first syngas and the second syngas into methanol; S5: The high-boiling-point fraction and the methanol are subjected to a cracking reaction to obtain the cracking target product, which includes low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms. It also includes: reacting the medium-boiling fraction with hydrogen to obtain jet fuel; wherein the hydrogenation reaction temperature is 300–500°C, the reaction pressure is 0.3–3.0 MPa, and the space velocity is 0.1–10 h⁻¹. -1 ; In step S5, the pyrolysis reaction is carried out at a temperature of 300–600℃, a pressure of 0.05–1.0 MPa, a catalyst-to-oil ratio of 0.1–12, and a space velocity of 1–50 h⁻¹. -1 .

2. The processing method as described in claim 1, characterized in that, The processing method further includes the following steps: S6: Recover the second carbon dioxide from the flue gas of the methanol preparation unit in step S4 and convert it into the third syngas.

3. The processing method as described in claim 2, characterized in that, The processing method further includes the following steps: S7: Recover the third carbon dioxide from the flue gas of the olefin preparation unit in step S5 and convert it into the fourth syngas.

4. The processing method as described in claim 3, characterized in that, The processing method further includes converting the third syngas and / or the fourth syngas into methanol.

5. The processing method according to any one of claims 1-3, characterized in that, The processing method further includes the following steps: S8: React the alkanes and recycled oil obtained in step S5 when forming the low-carbon olefins with oxygen to obtain the fourth carbon dioxide and the fifth synthesis gas.

6. The processing method as described in claim 5, characterized in that, The processing method further includes converting the fifth synthesis gas into methanol.

7. The processing method according to any one of claims 1-3, characterized in that, The processing method further includes the following steps: S9: React the component with 4 or more carbon atoms obtained in step S5 with oxygen, or use it as a reaction raw material in step S5.

8. A system for performing a zero-carbon emission plastic oil or crude oil processing method as described in any one of claims 1-7, characterized in that, The system includes: An atmospheric distillation apparatus is used to separate the plastic oil or crude oil into high-boiling-point fractions, medium-boiling-point fractions, and low-boiling-point fractions. A gasifier is used to react the low-boiling-point fraction with oxygen to produce carbon dioxide and a first syngas. An electrolysis unit is used to convert the carbon dioxide into a second syngas; A methanol production unit is used to convert syngas into methanol; An olefin preparation apparatus is used to react methanol and the high-boiling fraction to obtain cracking target products, which include low-carbon olefins with 2-3 carbon atoms and components with 4 or more carbon atoms. A hydrogenation reactor is used to convert the medium-boiling fraction into jet fuel.

9. The system as described in claim 8, characterized in that, The gasifier is also used to react alkanes and recycled oil obtained during the preparation of low-carbon olefins with oxygen to produce syngas and carbon dioxide.

10. The system as described in claim 8, characterized in that, The electrolysis unit is also used to convert carbon dioxide generated during the operation of the methanol preparation unit and / or olefin preparation unit into syngas.

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