Method for preparing ethylene from chlorine-containing organic waste

Abstract

The present application relates to the technical field of chemical engineering and environmental protection, and specifically to a method for preparing ethylene from chlorine-containing organic waste. The present application uses efficient and environmentally friendly thermal plasma technology, a gas containing hydrogen and carbon elements is used as a working gas to treat chlorine-containing organic waste, and the treated chlorine-containing organic waste is converted into high-value chemicals such as ethylene and acetylene, thereby realizing the resource recovery treatment of the chlorine-containing organic waste. On the one hand, the working gas can provide a hydrogen-rich reaction atmosphere, and on the other hand, the working gas provides a carbon source, thereby improving the yields of ethylene and acetylene. In addition, staged quenching technology is used to regulate the quenching rates in different temperature ranges during quenching, thereby greatly improving the selectivity and yield of ethylene, solving the problem in the prior art of low ethylene yield in a pyrolyzed gas phase product, and realizing the effective regulation and control of the composition of the pyrolyzed gas phase product from the chlorine-containing organic waste.

Description

A method for preparing ethylene from chlorinated organic waste

[0001] This application claims priority to Chinese Patent Application No. CN202411764674.9, filed on December 4, 2024, entitled "A Method for Preparing Ethylene from Chlorine-Containing Organic Waste", the entire contents of which are incorporated herein by reference. Technical Field

[0002] This application belongs to the fields of chemical and environmental protection technology, and specifically relates to a method for preparing ethylene from chlorinated organic waste. Background Technology

[0003] The chemical, pharmaceutical, and pesticide industries generate large quantities of chlorine-containing waste, whose main organic components include chlorinated alkanes, chlorinated olefins, and chlorinated benzene compounds. Chlorinated organic waste is a hazardous waste, generally characterized by high toxicity, infectiousness, and high accumulation and residue, posing a significant threat to the ecological environment and human health. Therefore, treatment technologies must achieve near 100% efficiency. Furthermore, recycling chlorinated organic waste into high-value-added chemicals can conserve substantial resources, achieving resource recovery on top of waste reduction and harmlessness.

[0004] Traditional methods for treating chlorinated organic waste include incineration and landfill. Incineration can significantly reduce volume and waste, and render the waste harmless. However, the organochlorine compounds in chlorinated organic waste inhibit combustion, reducing efficiency. Furthermore, the low calorific value of this type of waste necessitates the addition of fuel for co-firing, increasing costs. Improper operation can also lead to the production of highly toxic dioxins during incineration, causing secondary pollution. While landfilling is simple and convenient, the presence of chlorine increases the difficulty of waste treatment. Direct landfilling can cause plasticizers and stabilizers to leach into the soil and groundwater, polluting the environment. Moreover, landfills occupy significant space, and as land resources become increasingly scarce, the cost of safe landfilling increases substantially.

[0005] Therefore, there is an urgent need for a technology that can achieve the harmless treatment and resource utilization of chlorine-containing organic waste. Summary of the Invention

[0006] The purpose of this application is to provide a method for preparing ethylene from chlorinated organic waste. The method provided by this application can achieve the harmlessness and resource utilization of chlorinated organic waste.

[0007] To achieve the above objectives, this application provides the following technical solution:

[0008] This application provides a method for preparing ethylene from chlorinated organic waste, comprising the following steps:

[0009] A plasma atmosphere is formed by a working gas, and chlorine-containing organic waste is subjected to a pyrolysis reaction and staged quenching in the plasma atmosphere to obtain pyrolysis products; the staged quenching includes a first quenching and a second quenching in sequence, and the quenching rate of the first quenching is greater than that of the second quenching; the working gas contains hydrogen and carbon elements; the molar ratio of hydrogen to carbon elements in the plasma atmosphere is greater than 2:1;

[0010] The pyrolysis products are subjected to gas-solid separation to obtain gaseous products and solid products, wherein the gaseous products include ethylene.

[0011] Preferably, the quenching rate of the first quenching is greater than or equal to 1×10⁻⁶. 4 K / s, the temperature of the first quenched product is 1100~1300K.

[0012] Preferably, the quenching rate of the second quenching is 300-1000 K / s, and the temperature of the pyrolysis products is below 600 K.

[0013] Preferably, the working gas includes one or more of dry gas, coke oven gas, and natural gas.

[0014] Preferably, the chlorinated organic waste includes carbon and chlorine.

[0015] Preferably, the temperature of the pyrolysis reaction is 1800–3500 K.

[0016] Preferably, the staged quenching method includes indirect wall quenching and / or direct quenching;

[0017] The direct quenching includes physical quenching and / or chemical quenching;

[0018] The cooling medium used in the indirect wall quenching includes water, liquid nitrogen, cooling oil, or refrigerant.

[0019] The cooling medium used in the direct quenching includes one or more of argon, nitrogen, propane, and the working gas.

[0020] Preferably, the pyrolysis reaction is carried out in a plasma reactor;

[0021] The plasma reactor includes a radio frequency plasma reactor, a microwave plasma reactor, or an electric arc plasma reactor.

[0022] Preferably, the flow rate of the working gas is 0.5–1500 Nm³. 3 / h;

[0023] The treatment capacity of the chlorinated organic waste is 0.5–1000 kg / h.

[0024] Preferably, the chlorinated organic waste is introduced into the plasma reactor using a carrier gas, which includes one or more of dry gas, coke oven gas, hydrogen, and argon.

[0025] This application provides a method for preparing ethylene from chlorinated organic waste, comprising the following steps: forming a plasma atmosphere with a working gas; subjecting the chlorinated organic waste to a pyrolysis reaction and staged quenching in the plasma atmosphere to obtain pyrolysis products; the staged quenching includes sequential first quenching and second quenching, wherein the quenching rate of the first quenching is greater than that of the second quenching; the working gas contains hydrogen and carbon elements; the molar ratio of hydrogen to carbon elements in the plasma atmosphere is greater than 2:1; and performing gas-solid separation on the pyrolysis products to obtain gaseous and solid products, wherein the gaseous product includes ethylene.

[0026] This application employs highly efficient and environmentally friendly thermal plasma technology, utilizing a gas containing hydrogen and carbon as the working gas to treat chlorinated organic waste, converting it into high-value chemicals such as ethylene and acetylene, thus achieving the resource-based treatment of chlorinated organic waste. The working gas provides both a hydrogen-rich reaction atmosphere and a carbon source, increasing the yield of ethylene and acetylene. Simultaneously, a staged quenching technology is employed, significantly improving the selectivity and yield of ethylene by controlling the quenching rate within different temperature ranges during the quenching process. This solves the problem of low ethylene yield in the pyrolysis gas phase products under existing technologies, achieving effective control over the composition of the chlorinated organic waste pyrolysis gas phase products.

[0027] Furthermore, this application has good adaptability to raw materials, with no special requirements on the state and composition of chlorinated organic waste, and is highly applicable without the need for pretreatment; it also has no special requirements on the type and specific composition of the working gas; it has high raw material utilization, with a conversion rate of chlorinated organic waste greater than 98%, and a significant increase in the ethylene content in the cracked gas; the equipment is simple, easy to operate, requires no catalyst, is green and environmentally friendly, does not produce harmful substances such as dioxins, and achieves zero emissions of pollutants.

[0028] The method provided in this application has the advantages of short reaction time, high conversion rate, no secondary pollution and controllable product, realizing the comprehensive resource utilization of chlorine-containing organic waste and greatly increasing the yield of ethylene in the product. Attached Figure Description

[0029] Figure 1 is a flowchart illustrating the method provided in this application. Detailed Implementation

[0030] This application provides a method for preparing ethylene from chlorinated organic waste, comprising the following steps:

[0031] A plasma atmosphere is formed by a working gas, and chlorine-containing organic waste is subjected to a pyrolysis reaction and staged quenching in the plasma atmosphere to obtain pyrolysis products; the staged quenching includes a first quenching and a second quenching in sequence, and the quenching rate of the first quenching is greater than that of the second quenching; the working gas contains hydrogen and carbon elements; the molar ratio of hydrogen to carbon elements in the plasma atmosphere is greater than 2:1;

[0032] The pyrolysis products are subjected to gas-solid separation to obtain gaseous products and solid products, wherein the gaseous products include ethylene.

[0033] This application uses a working gas to form a plasma atmosphere, and then sequentially performs a pyrolysis reaction and staged quenching on chlorine-containing organic waste in the plasma atmosphere to obtain pyrolysis products.

[0034] In this application, the working gas contains hydrogen and carbon. In this application, the molar ratio of hydrogen to carbon in the plasma atmosphere is greater than 2:1, more preferably 4 to 20:1, specifically 4.9:1, 5.2:1, 5.6:1, or 6.5:1. In this application, the working gas preferably includes one or more of dry gas, coke oven gas, and natural gas; the dry gas preferably includes one or more of reforming dry gas, hydrocracking dry gas, catalytic cracking dry gas, and coking dry gas.

[0035] This application does not impose any special limitations on the process for forming the plasma atmosphere; any process well known to those skilled in the art can be used.

[0036] In this application, the chlorinated organic waste preferably includes carbon and chlorine, and may also include hydrogen. This application does not have specific requirements regarding the source and state of the chlorinated organic waste or the proportions of the elements; methods well-known to those skilled in the art can be used. In a specific embodiment of this application, the chlorinated organic waste is preferably solid hexachlorobenzene waste or liquid tetrachloroethylene waste provided by a chemical plant.

[0037] In this application, the pyrolysis reaction is preferably carried out in a plasma reactor; the plasma reactor preferably includes a radio frequency plasma reactor, a microwave plasma reactor, or an electric arc plasma reactor; the electric arc plasma reactor is preferably a direct current electric arc plasma reactor; the direct current electric arc plasma reactor is further preferably a magnetic rotating electric arc thermal plasma reactor. In this application, a magnetic rotating electric arc thermal plasma reactor is used, in which the electric arc rotates at high speed, which is beneficial to extending the service life of the anode, while also allowing for more thorough mixing of the raw materials and plasma, thereby improving the efficiency of the pyrolysis reaction.

[0038] In this application, when the chlorinated organic waste is solid hexachlorobenzene waste, it is preferably fed into the plasma reactor through a solid feed system; when the chlorinated organic waste is liquid tetrachloroethylene waste, it is preferably fed into the plasma reactor by pumping, preferably by a peristaltic pump.

[0039] In this application, the flow rate of the working gas is preferably 0.5 to 1500 Nm³. 3 / h. In this application, the processing capacity of the chlorinated organic waste is preferably 0.5 to 1000 kg / h. In this application, the chlorinated organic waste is preferably introduced into the plasma reactor using a carrier gas, which preferably includes one or more of dry gas, coke oven gas, hydrogen, and argon. In this application, a suitable working gas and carrier gas flow rate are selected according to the feed rate of the chlorinated organic waste and the required hydrogen / carbon ratio; the carrier gas flow rate has no special requirements, as long as it is sufficient to fluidize the chlorinated organic waste into the plasma reactor.

[0040] In this application, when using an electric arc plasma reactor to treat chlorinated organic waste, the chlorinated organic waste is preferably introduced into the electric arc plasma reactor from above or below the electric arc; more preferably, it enters the electric arc plasma reactor from above the electric arc, thereby making full use of the heat in the electric arc region, so that the raw materials are fully mixed with the thermal plasma, and the pyrolysis reaction proceeds rapidly and fully.

[0041] In this application, the temperature of the pyrolysis reaction is preferably 1800-3500K, specifically 1800K, 2000K, 2200K, 2400K, 2500K, 2800K, 3000K, 3200K, or 3500K.

[0042] In this application, the quenching rate of the first quenching is preferably greater than or equal to 1×10⁻⁶. 4 The temperature of the product after the first quenching is preferably 1100–1300 K / s. In this application, the quenching rate of the second quenching is preferably 300–1000 K / s, and the temperature of the pyrolysis product is preferably below 600 K. This application adjusts the quenching rate by changing the internal structure of the quenching section wall, the type of cooling medium, and / or the flow rate. The quenching rate has a significant impact on the composition of the pyrolysis gas. If the quenching rate of the high-temperature quenching section (i.e., the first quenching) is too low, acetylene will rapidly decompose into solid carbon and hydrogen at high temperatures, greatly reducing the total yield of hydrocarbons in the gaseous products. If the quenching rate of the low-temperature quenching section (i.e., the second quenching) is too high, the reaction of acetylene hydrogenation to ethylene cannot proceed fully, reducing the yield of ethylene in the gaseous products.

[0043] In this application, the staged quenching method preferably includes indirect quenching and / or direct quenching; the direct quenching preferably includes physical quenching and / or chemical quenching; the cooling medium used for indirect quenching preferably includes water, liquid nitrogen, cooling oil, or cryogenic fluid; the cooling medium used for direct quenching preferably includes one or more of argon, nitrogen, propane, and the working gas. In this application, the direction in which the cooling medium is injected into the quenching zone of the plasma reactor is preferably radial or tangential.

[0044] After obtaining the pyrolysis products, this application performs gas-solid separation on the pyrolysis products to obtain gas-phase products and solid-phase products, wherein the gas-phase products include ethylene.

[0045] This application does not have any special requirements for the gas-solid separation method. Conventional gas-solid separation technology in the field can be used, preferably a cyclone separator, a bag filter, or a ceramic separator, specifically a ceramic separator.

[0046] In this application, the gaseous products include ethylene, and more preferably acetylene and hydrogen chloride. After obtaining the gaseous products, it is also preferred to transport them to the enyne process for vinyl chloride production, or to perform conventional separation and purification operations such as absorption and distillation to obtain the products ethylene and acetylene. The separated hydrogen and argon can be returned to the plasma device and used again as carrier gas and / or quenching medium for the transport and cracking of chlorinated organic waste, thereby improving gas utilization.

[0047] In this application, the solid product is preferably elemental carbon, which is preferably present in the form of nano-carbon black particles and / or graphene.

[0048] In this application, the conversion rate of the chlorine-containing organic waste is preferably greater than 98%, and the ethylene yield in the cracked gas is preferably greater than 40%.

[0049] The flowchart of the method provided in this application is shown in Figure 1, wherein the working gas is dry gas, the high-temperature quenching zone is the first quenching zone, and the low-temperature quenching zone is the second quenching zone.

[0050] Unless otherwise specified, all materials and equipment used in this application are commercially available products in this field.

[0051] The technical solutions of this application will be clearly and completely described below with reference to the embodiments therein. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are within the scope of protection of this application.

[0052] Example 1

[0053] Chlorine-containing organic waste (solid hexachlorobenzene waste provided by a chemical plant) was transported into a microwave plasma reactor via a solid feed system using a carrier gas. The hexachlorobenzene feed rate was 2.8 kg / h, and the working gas was dry gas with a flow rate of 5 Nm³. 3 / h, the carrier gas argon flow rate is 3.3 Nm 3 The plasma reactor temperature is 2000K / h, and the molar ratio of hydrogen to carbon in the plasma atmosphere is 4.9. After a millisecond-level pyrolysis reaction, the pyrolysis products undergo a first quench and a second quench until the temperature of the pyrolysis products is below 600K. The quenching rate of the first quench is 1×10⁻⁶. 4 K / s, the temperature of the product after the first quench is 1200K, the quenching rate of the second quench is 500K / s, and the quenching method is to use deionized water as the cooling medium for indirect heat exchange.

[0054] The pyrolysis products obtained after quenching were subjected to gas-solid separation using a ceramic separator to obtain gaseous and solid products, respectively.

[0055] Gas chromatography analysis revealed that the main components of the gaseous products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 19.66%, 19.26%, and 48.13%, respectively. The yield of ethylene was 40.64%, and the yield of acetylene was 39.82%. TEM-EDS elemental analysis showed that the solid products were mainly composed of C, O, and Cl, with C accounting for 96.7% and Cl accounting for 0.33%. The solid products were primarily composed of nano-carbon black particles.

[0056] Example 2

[0057] Chlorine-containing organic waste (solid hexachlorobenzene waste provided by a chemical plant) is transported into the radio frequency plasma reactor via a solid feed system using a carrier gas. The hexachlorobenzene feed rate is 10 kg / h, and the working gas is dry gas with a flow rate of 20 Nm³. 3 / h, carrier argon flow rate is 8Nm 3 The plasma reactor operates at a temperature of 2400 K / h, with a hydrogen to carbon molar ratio of 5.2 in the plasma atmosphere. Following a millisecond-level pyrolysis reaction, the resulting pyrolysis products undergo a first and second quenching process until their temperature drops below 600 K. The quenching rate for the first quenching is 1.2 × 10⁻⁶. 4 K / s, the temperature of the product after the first quench is 1100K, the quenching rate of the second quench is 500K / s, and the quenching method is to use argon gas as a cooling medium to be radially injected into the plasma reactor for direct heat exchange.

[0058] The pyrolysis products obtained after quenching were subjected to gas-solid separation using a ceramic separator to obtain gaseous and solid products, respectively.

[0059] Gas chromatography analysis revealed that the main components of the gaseous products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 20.59%, 18.16%, and 46.92%, respectively. The yield of ethylene was 42.11%, and the yield of acetylene was 37.15%. The solid products were mainly a mixture of nano-carbon black particles and graphene.

[0060] Example 3

[0061] Chlorine-containing organic waste (solid hexachlorobenzene waste provided by a chemical plant) is transported into a magnetic rotating arc thermal plasma reactor via a solid feed system using a carrier gas. The hexachlorobenzene feed rate is 100 kg / h, and the working gas is dry gas with a flow rate of 175 Nm³. 3 / h, carrier gas dry gas flow rate is 75Nm 3 The plasma reactor operates at a temperature of 3000 K / h, with a hydrogen to carbon molar ratio of 5.6 in the plasma atmosphere. Following a millisecond-level pyrolysis reaction, the resulting pyrolysis products undergo a first and second quenching process until their temperature drops below 600 K. The quenching rate for the first quenching is 1.5 × 10⁻⁶. 4 K / s, the temperature of the product after the first quench is 1200K, the quenching rate of the second quench is 400K / s, and the quenching method is to use argon gas as a cooling medium to be radially injected into the plasma reactor for direct heat exchange.

[0062] The obtained pyrolysis products were subjected to gas-solid separation using a ceramic separator to obtain gaseous and solid products, respectively.

[0063] Gas chromatography analysis revealed that the main components of the gas phase products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 21.81%, 14.43%, and 41.51%, respectively. The yield of ethylene was 43.05%, and the yield of acetylene was 28.49%. The solid phase products were mainly a mixture of nano-carbon black particles and graphene.

[0064] Example 4

[0065] Chlorine-containing organic waste (liquid tetrachloroethylene waste provided by a chemical plant) is transported into a magnetic rotating arc thermal plasma reactor using a carrier gas via a peristaltic pump. The tetrachloroethylene feed rate is 1000 kg / h, the working gas is dry gas, and the flow rate is 2000 Nm³. 3 / h, carrier argon flow rate is 550Nm 3 The plasma reactor operates at a temperature of 2500 K / h, with a hydrogen to carbon molar ratio of 6.5 in the plasma atmosphere. Following a millisecond-level pyrolysis reaction, the resulting pyrolysis products undergo a first quench and a second quench until the temperature of the pyrolysis products is below 600 K. The quenching rate for the first quench is 1.5 × 10⁻⁶. 4K / s, the temperature of the product after the first quench is 1200K, the quenching rate of the second quench is 400K / s, and the quenching method is to use argon gas as a cooling medium to be radially injected into the plasma reactor for direct heat exchange.

[0066] The obtained pyrolysis products were subjected to gas-solid separation using a ceramic separator to obtain gaseous and solid products, respectively.

[0067] Gas chromatography analysis revealed that the main components of the gaseous products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 15.92%, 15.84%, and 54.14%, respectively. The yield of ethylene was 41.24%, and the yield of acetylene was 41.01%. The flow rates of ethylene and acetylene in the gaseous products were 158.75 and 157.88 Nm³, respectively. 3 / h. The solid products are mainly a mixture of nano-carbon black particles and graphene.

[0068] Comparative Example 1

[0069] Ethylene was prepared according to the method in Example 3, except that the quenching process was different. Specifically, the resulting pyrolysis products were quenched at 1.5 × 10⁻⁶. 4 Quenching is carried out at a quenching rate of K / s until the temperature of the pyrolysis products is below 600K. The quenching method is to use argon gas as a cooling medium to be radially injected into the plasma reactor for direct heat exchange.

[0070] Gas chromatography analysis revealed that the main components of the gaseous products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 7.41%, 41.71%, and 47.08%, respectively. The yield of ethylene decreased to 12.91%, and the yield of acetylene was 72.58%.

[0071] Comparative Example 2

[0072] Ethylene was prepared according to the method of Example 4, except that hydrogen was used as the working gas instead of dry gas.

[0073] Gas chromatography analysis revealed that the main components of the gaseous products (excluding the working gas and carrier gas) were ethylene, acetylene, and hydrogen chloride, with volume fractions of 8.09%, 7.50%, and 78.16%, respectively. The yield of ethylene was 41.38%, and the yield of acetylene was 38.39%. However, the flow rates of ethylene and acetylene in the gaseous products were 55.84 and 51.80 Nm³, respectively. 3 The flow rate is significantly lower than that of ethylene and acetylene in Example 4, which demonstrates that the method provided in this application can further increase the production of ethylene and acetylene.

[0074] Although the above embodiments have provided a detailed description of this application, they are only some embodiments of this application, not all embodiments. Other embodiments can be obtained based on these embodiments without creative intent, and these embodiments all fall within the protection scope of this application.

Claims

1. A method for producing ethylene using a chlorine-containing organic waste, characterized by, Includes the following steps: A plasma atmosphere is formed by a working gas, and chlorine-containing organic waste is subjected to a pyrolysis reaction and staged quenching in the plasma atmosphere to obtain pyrolysis products; the staged quenching includes a first quenching and a second quenching in sequence, and the quenching rate of the first quenching is greater than that of the second quenching; the working gas contains hydrogen and carbon elements; the molar ratio of hydrogen to carbon elements in the plasma atmosphere is greater than 2:1; The pyrolysis products are subjected to gas-solid separation to obtain gaseous products and solid products, wherein the gaseous products include ethylene.

2. The method of claim 1, wherein, The first quenching rate is greater than or equal to 1 x 10 4 K / s, and the temperature of the first quenched product is 1100 to 1300 K.

3. The method of claim 2, wherein, The quenching rate of the second quenching is 300-1000 K / s, and the temperature of the pyrolysis products is below 600 K.

4. The method of claim 1, wherein, The working gas includes one or more of dry gas, coke oven gas, and natural gas.

5. The method of claim 4, wherein, The dry gas includes one or more of the following: reformed dry gas, hydrocracking dry gas, catalytic cracking dry gas, and coking dry gas.

6. The method of claim 1, wherein, The chlorinated organic waste includes carbon and chlorine.

7. The method of claim 6, wherein, The chlorinated organic waste includes solid hexachlorobenzene waste or liquid tetrachloroethylene waste.

8. The method of claim 1, wherein, The temperature of the pyrolysis reaction is 1800–3500 K.

9. The method according to claim 1 or 2 or 3, characterized in that, The graded quenching method includes indirect quenching and / or direct quenching; The direct quenching includes physical quenching and / or chemical quenching; The cooling medium used in the indirect wall quenching includes water, liquid nitrogen, cooling oil, or refrigerant. The cooling medium used in the direct quenching includes one or more of argon, nitrogen, propane, and the working gas.

10. The method of claim 1 or 7, wherein, The pyrolysis reaction is carried out in a plasma reactor; The plasma reactor includes a radio frequency plasma reactor, a microwave plasma reactor, or an electric arc plasma reactor.

11. The method of claim 10, wherein, The electric arc plasma reactor is a direct current electric arc plasma reactor; The DC arc plasma reactor is a magnetic rotating arc thermal plasma reactor.

12. The method of claim 10, wherein, When the chlorinated organic waste is solid hexachlorobenzene waste, it is fed into the plasma reactor through a solid feed system; When the chlorinated organic waste is liquid tetrachloroethylene waste, it is pumped into the plasma reactor by a peristaltic pump.

13. The method of claim 1 or 11, wherein, The flow rate of the working gas is 0.5-1500 Nm 3 / h; The treatment capacity of the chlorinated organic waste is 0.5–1000 kg / h.

14. The method of claim 1 or 11, wherein, The chlorinated organic waste is introduced into the plasma reactor using a carrier gas, which includes one or more of dry gas, coke oven gas, hydrogen, and argon.

15. The method of claim 1, wherein, The solid product is elemental carbon.

16. The method of claim 1, wherein, The conversion rate of the chlorine-containing organic waste is greater than 98%, and the ethylene yield in the cracked gas is greater than 40%.

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