Method and system for preparing gasoline using mixed waste plastics containing PVC

Abstract

The present invention relates to the technical field of solid waste plastic processing, and discloses a method and system for preparing gasoline using mixed waste plastics containing PVC. The method comprises the following steps: (1) mixing the mixed waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; wherein the organic solvent is selected from one or more of N-methylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, and dimethyl sulfoxide; (2) contacting the dechlorinated waste plastics with a pyrolysis catalyst in the presence of hydrogen to perform a pyrolysis reaction to obtain pyrolysis oil and gas; (3) separating the pyrolysis oil and gas to obtain gasoline. The method provided by the present invention can improve the dechlorination effect of mixed waste plastics containing PVC, obtain high-quality gasoline, reduce production costs, realize high-value-added resource utilization of waste plastics, and is suitable for industrial promotion.

Description

Technical Field

[0001] The present invention relates to the technical field of solid waste plastics processing, and in particular to a method and system for preparing gasoline by utilizing mixed waste plastics containing PVC. Background Art

[0002] Plastics, due to their excellent durability, corrosion resistance, malleability, and stability, are widely used in various industries, including packaging, construction, and manufacturing. According to statistics, global plastic production reached 359 million tons in 2018, with an annual growth rate of approximately 3.2%. This high production volume is countered by the generally short lifespan of plastic products. About half of all plastics have an average lifespan of only one to two years, and packaging plastics have a lifespan of less than one month. Furthermore, the difficulty of plastics to degrade naturally has led to a growing global production of plastic waste, reaching nearly 300 million tons annually. China's waste plastic production accounts for approximately 30% of the world's total plastic production.

[0003] OECD statistics show that 9% of plastic used globally is recycled, 19% is incinerated, nearly 50% is landfilled, and the remaining 22% is discarded in uncontrolled landfills, burned in the open air, or leaked into the environment. The large amount of untreated waste plastic accumulates year by year, causing numerous environmental problems such as marine microplastics and white pollution, posing a serious threat to human health. Furthermore, plastic is derived from petroleum and is rich in carbon and hydrogen. The abandonment of large amounts of waste plastic is a significant waste of petrochemical resources.

[0004] Chemical recycling of waste plastics is currently attracting widespread attention. Pyrolysis of organic waste, with target products such as syngas and pyrolysis oil, is considered one of the most promising technologies for waste plastics utilization due to its wide range of raw material applicability, low pollution, and low emissions. However, mixed waste plastics often contain PVC (polyvinyl chloride). Direct pyrolysis of mixed waste plastics containing PVC results in a high Cl content in the target liquid fuel. This high Cl content is detrimental to further processing of the liquid fuel and can easily increase the production cost of waste plastic recycling.

[0005] Existing technologies for dechlorinating mixed waste plastics containing PVC primarily utilize thermal decomposition of the PVC coupled with alkaline absorption. However, this process generates significant amounts of solid waste and ultimately converts the PVC into inorganic salts, significantly reducing its value. Furthermore, the liquid fuels produced by conventional pyrolysis have poor selectivity, complex composition, and a wide carbon number distribution, requiring further processing before they can be used as replacements for liquid fuels such as gasoline.

[0006] Therefore, there is an urgent need to provide a method for directly preparing gasoline from mixed waste plastics containing PVC, which has the advantages of simple process, low pyrolysis temperature, good dechlorination effect, low production cost and high liquid fuel quality. Summary of the Invention

[0007] The purpose of the present invention is to solve the problems in the prior art of the pyrolysis process of mixed waste plastics containing PVC, such as complex dechlorination process, large solid waste output, poor pyrolysis selectivity, high chlorine content, poor selectivity, complex composition, and wide carbon number distribution in the pyrolysis oil, and to provide a method and system for directly preparing gasoline using mixed waste plastics containing PVC.

[0008] In order to achieve the above object, a first aspect of the present invention provides a method for directly preparing gasoline using mixed waste plastics containing PVC, wherein the method comprises the following steps:

[0009] (1) mixing mixed waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; wherein the organic solvent is selected from one or more of N-methylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, and dimethyl sulfoxide;

[0010] (2) contacting the dechlorinated waste plastic with a pyrolysis catalyst in the presence of hydrogen to perform a pyrolysis reaction to obtain pyrolysis oil and gas;

[0011] (3) Separating the pyrolysis oil and gas to obtain gasoline.

[0012] A second aspect of the present invention provides a system for directly preparing gasoline from mixed waste plastics containing PVC; wherein the system comprises a feeding device, a dissolution and dechlorination device, a pyrolysis reactor and a gas-liquid separator; wherein the feeding device is used to transport the mixed waste plastics containing PVC to the dissolution and dechlorination device; the dissolution and dechlorination device is used to mix the mixed waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; the pyrolysis reactor is used to pyrolyze the dechlorinated waste plastics under the action of a pyrolysis catalyst to obtain pyrolysis oil and gas; and the gas-liquid separator is used to separate the pyrolysis oil and gas to obtain gasoline.

[0013] Through the above technical solution, the present invention can improve the dechlorination effect of mixed waste plastics containing PVC, can pyrolyze and dechlorinate waste plastics at low temperatures, solves the problem that the pyrolysis oil product obtained by traditional catalytic pyrolysis of waste plastics has a wide distillation range distribution and a low gasoline fraction content, can obtain high-quality gasoline, reduce production costs, realize high-value-added resource utilization of waste plastics, help solve the environmental crisis caused by waste plastics, and is suitable for industrial promotion. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 This is a schematic diagram of a system for directly preparing gasoline from mixed waste plastics containing PVC in a preferred embodiment of the present invention. DETAILED DESCRIPTION

[0015] The endpoints of the ranges and any values ​​disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoints of each range, the endpoints of each range and individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered to be specifically disclosed herein.

[0016] A first aspect of the present invention provides a method for directly preparing gasoline using mixed waste plastics containing PVC, wherein the method comprises the following steps:

[0017] (1) mixing mixed waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; wherein the organic solvent is selected from one or more of N-methylpyrrolidone, N,N-dimethylformamide, N,N-dimethylacetamide, and dimethyl sulfoxide;

[0018] (2) contacting the dechlorinated waste plastic with a pyrolysis catalyst in the presence of hydrogen to perform a pyrolysis reaction to obtain pyrolysis oil and gas;

[0019] (3) Separating the pyrolysis oil and gas to obtain gasoline.

[0020] In step (1):

[0021] In a preferred embodiment, the mass content of PVC in the PVC-containing waste plastics is 1-10%.

[0022] In a preferred embodiment, the mixed waste plastics further contain one or more of PE (polyethylene), PP (polypropylene), and PS (polystyrene).

[0023] In a preferred embodiment, in order to increase the dissolution rate of PVC in the mixed waste plastics, before mixing the mixed waste plastics containing PVC with the organic solvent, the mixed waste plastics containing PVC are preferably cleaned, dried and crushed to obtain flaky particles with a particle size of ≤20 mm.

[0024] In the present invention, the washing, drying, and crushing are conventional operations and are not particularly limited thereto. The particle size in the present invention refers to the maximum size of the flaky particles, i.e., the longest linear distance between the two endpoints of the flaky particles observed when measured with a ruler.

[0025] In a preferred embodiment, the mixing operating conditions include: a mixing temperature of 50-100°C, preferably 60-80°C; a mixing time of 5-60 min, preferably 20-40 min; a stirring speed of 20-100 r / min, preferably 40-60 r / min; and a mass ratio of the mixed waste plastics containing PVC to the organic solvent of 1:0.1-10, preferably 1:3-10.

[0026] In the present invention, the organic solvent can selectively dissolve PVC in the mixed waste plastics, thereby removing the PVC. The PVC removal method of the present invention not only has a good PVC removal effect, but also avoids the generation of a large amount of solid waste, thereby reducing production costs.

[0027] In a preferred embodiment, the step (1) further comprises first contacting the chlorine-containing solution with a stripping agent for stripping to obtain PVC particles and a filtrate, and then distilling the filtrate to obtain a recovered organic solvent and a recovered stripping agent.

[0028] In the present invention, the recovered organic solvent and the recovered stripping agent are returned to step (1) for repeated use, which can further reduce production costs and improve economic benefits.

[0029] In a preferred embodiment, the stripping agent is selected from water and / or alcohol solvents, more preferably water.

[0030] In a preferred embodiment, the stripping operating conditions include: stripping pressure is atmospheric pressure, stripping temperature is 50-90°C, preferably 60-80°C; the volume ratio of chlorine-containing solution to stripping agent is 1:0.5-4, preferably 1:1-3.

[0031] In the present invention, normal pressure has a well-known meaning and is not particularly limited in the present invention. A chlorine-containing solution is contacted with a stripping agent, and the organic solvent in the chlorine-containing solution enters the stripping agent so that PVC is precipitated from the chlorine-containing solution. After stripping, a solid-liquid mixture containing PVC particles can be obtained. The obtained solid-liquid mixture is separated to obtain PVC particles and a filtrate. The filtrate includes a stripping agent and an organic solvent. The purpose of distilling the filtrate is to separate the stripping agent and the organic solvent. The present invention does not particularly limit the operating conditions of the distillation. The distillation can be carried out according to the specific types of the stripping agent and the organic solvent according to conventional operations in the art.

[0032] In step (2):

[0033] In a preferred embodiment, based on the total amount of the pyrolysis catalyst, the pyrolysis catalyst comprises 50-95 wt% of a carrier and 5-50 wt% of an active component; wherein the carrier is selected from one or more of HY molecular sieve, β molecular sieve, ZSM-5 molecular sieve, ZRP molecular sieve, MCM-41 molecular sieve, and SAPO-34 molecular sieve; and the active component exists in the form of an oxide and is selected from Group VIB metal elements and / or Group VIII metal elements.

[0034] In a preferred embodiment, based on the total amount of the pyrolysis catalyst, the pyrolysis catalyst comprises 90-95 wt% of a carrier and 5-10 wt% of an active component.

[0035] In a preferred embodiment, the carrier is selected from one or more of HY molecular sieve, β molecular sieve, and ZSM-5 molecular sieve.

[0036] The present invention does not specifically limit HY molecular sieve, β molecular sieve, ZSM-5 molecular sieve, ZRP molecular sieve, MCM-41 molecular sieve, or SAPO-34 molecular sieve. Preferably, the silicon-to-aluminum ratio of HY molecular sieve, β molecular sieve, ZSM-5 molecular sieve, ZRP molecular sieve, MCM-41 molecular sieve, or SAPO-34 molecular sieve can be independently selected from 20-60:1. When the carrier is one or more of HY molecular sieve, β molecular sieve, or ZSM-5 molecular sieve, the pyrolysis effect is better.

[0037] In a preferred embodiment, the active component is selected from one or more of Mo, W, Ni, Fe, Co, Pt, Pd, and Ru.

[0038] In a preferred embodiment, the operating conditions of the pyrolysis reaction include: pyrolysis temperature of 200-350°C, preferably 250-300°C; pyrolysis pressure of 2-5 MPa, preferably 3-4 MPa; pyrolysis time of 30-180 min, preferably 60-120 min; mass space velocity of the pyrolysis catalyst of 1-10 h -1 , preferably 2-5h -1 .

[0039] In the present invention, hydrogen and a pyrolysis catalyst work together to lower the pyrolysis temperature, enhance the degree of cracking, and improve the pyrolysis effect, resulting in a concentrated distribution of carbon numbers in the cracking products between 5 and 12. This results in a simple gasoline composition with high yields and reduces pollutant emissions, contributing to the development of a circular economy and achieving the dual carbon goals, with excellent environmental, social, and economic benefits.

[0040] In step (3):

[0041] In a preferred embodiment, the pyrolysis oil and gas are separated to obtain gaseous products and gasoline.

[0042] In a preferred embodiment, the gasoline is C5-C 12 The fraction, the chlorine content in the gasoline is ≤5μg / g, preferably ≤3μg / g; the gas phase product includes H2 and C1-C4 small molecule gases.

[0043] Compared with the existing waste plastic pyrolysis, the present invention does not need to reprocess the pyrolysis products and can directly obtain C5-C 12 The gasoline obtained from the distillate has a concentrated carbon number distribution, simple composition, high yield, and can be directly used to replace traditional fuels.

[0044] In a preferred embodiment, the present invention does not specifically limit the separation, and the separation is preferably gas-liquid separation; for example, cold hydrazine can be used to condense the pyrolysis oil and gas. During the condensation process, the condensed product is the pyrolysis oil, and the non-condensable gas is the gas phase product.

[0045] In a preferred embodiment, the gaseous product is returned to the pyrolysis reaction. In the present invention, returning the gaseous product to the pyrolysis reaction can reduce hydrogen consumption.

[0046] The second aspect of the present invention provides a system for directly preparing gasoline using mixed waste plastics containing PVC, the system comprising a feeding device, a dissolving and dechlorinating device, a pyrolysis reactor and a gas-liquid separator; wherein the feeding device is used to transport the mixed waste plastics containing PVC to the dissolving and dechlorinating device; the dissolving and dechlorinating device is used to mix the waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; the pyrolysis reactor is used to pyrolyze the dechlorinated waste plastics under the action of a pyrolysis catalyst to obtain pyrolysis oil and gas; the gas-liquid separator is used to separate the pyrolysis oil and gas to obtain gasoline, such as Figure 1 shown.

[0047] In a preferred embodiment, the dissolution dechlorination device is a countercurrent reactor, preferably a countercurrent reactor with a heating function, and more preferably a countercurrent reactor with an external heating function.

[0048] A countercurrent reactor is a novel chemical reaction device characterized by the fact that the two reacting substances, rather than being stirred or co-flowing together, meet and react in a countercurrent flow within the reactor. The product and the starting materials exit the reactor through separate outlets, achieving continuous production. The present invention does not impose any particular limitations on the countercurrent reactor; any conventional countercurrent reactor can be used in this invention.

[0049] In a preferred embodiment, the pyrolysis reactor is selected from a slurry bed reactor, a fixed bed reactor, an ebullient bed reactor, and a fluidized bed reactor.

[0050] In a preferred embodiment, the feeding device includes a vacuum loader, a silo, a transverse screw extruder and a vertical screw extruder; wherein the vacuum loader is used to transport the mixed waste plastics containing PVC to the silo; the silo is used to store the mixed waste plastics containing PVC; the transverse screw extruder and the vertical screw extruder are used to transport the mixed waste plastics containing PVC in the silo to the dissolution and dechlorination device; wherein the mixed waste plastics containing PVC in the silo are transported in sequence by the transverse screw extruder and the vertical screw extruder and then enter the dissolution and dechlorination device.

[0051] Among them, in the present invention, the mixed waste plastics containing PVC in the silo are transported by the horizontal screw extruder and the vertical screw extruder in sequence and then enter the dissolution and dechlorination device. The high pressure generated by the mechanical movement can be used to ensure sealing and prevent the organic solvent in the dissolution and dechlorination device from back-gassing into the silo.

[0052] In a preferred embodiment, the silo is a conical hopper with a feed screw, the diameter of the feed screw blades gradually decreasing, and a scraper is installed on the largest diameter blade. The silo of the present invention can prevent PVC waste plastics from "bridging" in the silo and preventing them from entering the horizontal screw extruder at the bottom of the silo.

[0053] In a preferred embodiment, the system further comprises a pre-processing device, which comprises a washer, a dryer and a crusher.

[0054] In a preferred embodiment, the system further includes a recovery device, which includes a stripper, a solid-liquid separator and a distillation tower; wherein the stripper is used to mix the chlorine-containing solution with the stripping agent to obtain a solid-liquid mixture; the solid-liquid separator is used to separate the solid-liquid mixture to obtain PVC particles and a filtrate; and the distillation tower is used to separate the filtrate to obtain a recovered organic solvent and a recovered stripping agent.

[0055] The present invention will be described in detail below by way of examples. Figure 1 The process is carried out in the system shown in the figure, wherein the dissolution dechlorination device is a countercurrent reactor, the pyrolysis reactor is a fixed bed reactor, the oil-gas separator is a two-stage cold hydrazine device, the stripper is a stripper tank with a stirring paddle, the solid-liquid separator is a filter, and the silo is a conical funnel with a feed spiral. The diameter of the feed spiral blades gradually decreases, and a scraper is installed on the blade with the largest diameter.

[0056] The PVC-containing mixed plastic waste used in the Examples and Comparative Examples was sorted from a landfill in Ganzhou, Jiangxi Province, by Haotian Environmental Protection Co., Ltd., and contained 5% PVC by mass. After being crushed, dried, and processed through a decontamination unit, the PVC-containing mixed plastic waste had a moisture content of 0% by weight, an organic impurity content of 3.6% by weight, a plastic content of 96.4% by weight, and a particle size of ≤20 mm. The Si / Al ratio of the HY molecular sieve in the catalyst was 40.

[0057] Example 1

[0058] (1) The mixed waste plastics containing PVC are transported to a silo via a vacuum feeder, enter a horizontal screw extruder from the bottom of the silo, and then enter a vertical screw extruder, which transports the particles to a dissolution and dechlorination device;

[0059] Mixed waste plastics containing PVC were fully mixed and dissolved with the organic solvent N,N-dimethylformamide in a dissolution and dechlorination device to separate the chlorine-containing solution and the dechlorinated waste plastics. The mass ratio of the mixed waste plastics containing PVC to the organic solvent was 1:10, the mixing temperature was 80°C, the mixing time was 20 minutes, and the stirring speed was 60 r / min. The chlorine content of the dechlorinated waste plastics was 19 μg / g.

[0060] The obtained chlorine-containing solution is introduced into a stripping device and brought into contact with stripping agent water for stripping to obtain a solid-liquid mixture, and the solid-liquid mixture is filtered to obtain PVC particles and a filtrate; wherein the stripping pressure is normal pressure, the stripping temperature is 80°C, and the volume ratio of the chlorine-containing solution to the stripping agent is 1:3;

[0061] The obtained filtrate is distilled to obtain a recovered organic solvent and a recovered stripping agent; the recovered organic solvent and the recovered stripping agent are returned for reuse;

[0062] (2) In the presence of hydrogen, the dechlorinated waste plastic is contacted with a pyrolysis catalyst in a pyrolysis reactor to carry out a pyrolysis reaction to obtain pyrolysis oil and gas; wherein the pyrolysis catalyst comprises 5 wt% of Pd and 95 wt% of HY molecular sieve, the pyrolysis temperature is 250°C, the pyrolysis pressure is 3 MPa, the pyrolysis time is 60 min, and the mass space velocity of the pyrolysis catalyst is 5 h -1 ;

[0063] (3) The pyrolysis oil and gas are introduced into an oil-gas separator for oil-gas separation to obtain gas phase products and gasoline; wherein the separation temperature of the oil-gas separator is -10°C, the separation pressure is normal pressure, and the mass yield of the obtained gasoline is 58.2%, and the gasoline is C5-C 12 The content of chlorine in the distillate is less than 3μg / g.

[0064] Example 2

[0065] The same as Example 1, except that the organic solvent and catalyst were changed. The specific operating conditions and analysis results are shown in Table 1.

[0066] Example 3

[0067] The same as Example 1, except that the catalyst was changed. The specific operating conditions and analysis results are shown in Table 1.

[0068] Comparative Example 1

[0069] The same process as in Example 1 was performed, except that the pyrolysis catalyst was an HY molecular sieve without active components, and the pyrolysis oil and gas were introduced into an oil-gas separator for oil-gas separation to obtain gaseous and liquid products. The specific operating conditions and analysis results are shown in Table 1. The obtained liquid product was cut to obtain gasoline.

[0070] Comparative Example 2

[0071] The same as Example 1, except that step (1) is omitted, and the mixed waste plastics containing PVC are directly subjected to pyrolysis in step (2) and separation in step (3). The specific operating conditions and analysis results are shown in Table 1.

[0072] Table 1

[0073]

[0074]

[0075] Note: The carbon number distribution in the table was determined by gas chromatography.

[0076] Table 1 (continued)

[0077]

[0078] As can be seen from Examples 1-3, by using the method provided by the present invention in the system for directly preparing gasoline from mixed waste plastics containing PVC provided by the present invention, gasoline with a carbon number distribution between 5 and 12 can be directly prepared with a high gasoline yield and low chlorine content.

[0079] Comparative Example 1 shows that without adding active components to the pyrolysis catalyst, the resulting liquid product has a complex carbon number and low yield, requiring further processing to produce gasoline. Comparative Example 2 shows that directly pyrolyzing mixed waste plastics results in gasoline with a high chlorine content, making it unsuitable for direct use.

[0080] The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, various simple variations of the technical solution of the present invention may be made, including combining the various technical features in any other appropriate manner. These simple variations and combinations should also be regarded as disclosed in the present invention and fall within the scope of protection of the present invention.

Claims

1. A method for directly preparing gasoline from mixed waste plastics containing PVC, characterized in that: The method comprises the following steps: (1) Mixing mixed waste plastics containing PVC with an organic solvent to obtain a chlorine-containing solution and dechlorinated waste plastics; wherein the organic solvent is selected from one or more of N-methylpyrrolidone, N,N-dimethylformamide, and N,N-dimethylacetamide; (2) contacting the dechlorinated waste plastic with a pyrolysis catalyst in the presence of hydrogen to carry out a pyrolysis reaction to obtain pyrolysis oil and gas; (3) separating the pyrolysis oil and gas to obtain gasoline; The operating conditions of the pyrolysis reaction include: pyrolysis temperature of 250-300°C; pyrolysis pressure of 3-4 MPa; pyrolysis time of 60-120 min; mass space velocity of pyrolysis catalyst of 2-5 h -1 ; Based on the total amount of the pyrolysis catalyst, the pyrolysis catalyst comprises 50-95 wt% of a carrier and 5-50 wt% of an active component, wherein the carrier is selected from HY molecular sieve; and the active component is selected from one or more of W, Pt, and Pd; The mass ratio of the mixed waste plastics containing PVC to the organic solvent is 1:0.1-10.

2. The method according to claim 1, wherein The mixed waste plastics containing PVC also contain one or more of polyethylene, polypropylene and polystyrene.

3. The method according to claim 1, wherein The mass content of PVC in the mixed waste plastics containing PVC is 1-10%.

4. The method according to claim 1, wherein The particle size of the mixed waste plastics containing PVC is ≤20 mm.

5. The method according to claim 1, wherein The mixing operating conditions include: mixing temperature of 50-100° C.; mixing time of 5-60 min; and stirring speed of 20-100 r / min.

6. The method according to claim 5, wherein: The mixing operating conditions include: a mixing temperature of 60-80°C.

7. The method according to claim 5, wherein: The mixing operation conditions include: mixing time is 20-40 minutes.

8. The method according to claim 5, wherein The stirring speed is 40-60r / min.

9. The method according to claim 5, wherein: The mass ratio of the mixed waste plastics containing PVC to the organic solvent is 1:3-10.

10. The method according to claim 1, wherein The step (1) further comprises first contacting the chlorine-containing solution with a stripping agent for stripping and separation to obtain PVC particles and a filtrate, and then distilling the filtrate to obtain a recovered organic solvent and a recovered stripping agent.

11. The method according to claim 10, wherein: The recovered organic solvent and the recovered stripping agent are returned to step (1) for recycling.

12. The method according to claim 10, wherein: The stripping agent is selected from one or more of water and / or alcohol solvents.

13. The method according to claim 12, wherein: The stripping agent is selected from water.

14. The method according to claim 10, wherein: The operating conditions of the stripping include: stripping pressure is normal pressure, stripping temperature is 50-90° C.; and the volume ratio of the chlorine-containing solution to the stripping agent is 1:0.5-4.

15. The method according to claim 14, wherein The operating conditions of the stripping include: the stripping temperature is 60-80°C.

16. The method according to claim 14, wherein The operating conditions of the stripping include: the volume ratio of the chlorine-containing solution to the stripping agent is 1:1-3.

17. The method according to claim 1, wherein Based on the total amount of the pyrolysis catalyst, the pyrolysis catalyst includes 90-95 wt % of a carrier and 5-10 wt % of an active component.

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