Method for producing calcium coalized pellets by pyrolysis using a sliding arc plasma system

Abstract

The present application relates to the technical field of preparing calcium coal carbonized pellets, in particular to a method for preparing calcium coal carbonized pellets by pyrolysis using a sliding arc plasma system, comprising the following steps: S1, conveying quicklime and raw coal to a calcium coal pellet preparation unit, and conveying the formed calcium coal pellets to a pyrolysis chamber; S2, pyrolyzing the calcium coal pellets in the pyrolysis chamber to obtain and output calcium coal carbonized pellets; introducing the crude coal gas generated by pyrolyzing the calcium coal pellets in the pyrolysis chamber into the plasma zone of the sliding arc reforming oxidation system reactor, and introducing a preset volume of gas oxidant into the sliding arc reforming oxidation system reactor at the same time, so that the gas oxidant is mixed with the crude coal gas; S3, plasma inducing the crude coal gas and causing a reforming oxidation reaction to generate high-temperature crude synthesis gas, and the high-temperature crude synthesis gas is conveyed to a crude synthesis gas purification unit and the pyrolysis chamber, respectively; the method for preparing calcium coal carbonized pellets has the advantages of low cost, environmental protection and high added value.

Description

Technical Field

[0001] This invention relates to the technical field of preparing calcium coal oxide pellets, and more specifically, to a method for preparing calcium coal oxide pellets by pyrolysis using a sliding arc plasma system. Background Technology

[0002] Due to its structural characteristics, acetylene can be used to produce a variety of organic compounds. Currently, acetylene remains a chemical resource with huge production capacity, so in-depth research into acetylene chemical engineering is of great significance.

[0003] From the perspective of technological development and cost, acetylene has been replaced by ethylene in the production of some organic compounds and is no longer used. However, in the production of other organic compounds, acetylene remains an irreplaceable raw material. In modern acetylene chemistry, major industrial products prepared using acetylene include butadiene, vinyl chloride, or vinyl acetate.

[0004] calcium carbide (C a C2 is the main industrial raw material used to produce acetylene, and it can also be used as a reducing agent and desulfurizing agent in the steel industry. In recent years, due to the large fluctuations in international oil prices and the adjustment of domestic industry structure and policies, the traditional calcium carbide industry, which is characterized by high energy consumption, high pollution and low efficiency, is facing severe challenges. Therefore, my country's calcium carbide industry will develop towards intensification, large-scale production, energy conservation and environmental protection in the future.

[0005] Traditional calcium carbide production processes are costly, using bulk carbon raw materials and lime, and suffer from low mass and heat transfer efficiency, slow reaction rates, and overall energy consumption and product economics that fail to meet market demands. Meanwhile, traditional plasma arc technology has also been evaluated as a method for treating this type of organic waste through pyrolysis. This method utilizes continuous plasma arc technology to pyrolyze organic waste in a high-temperature pyrolysis chamber (e.g., 5000°C to 15000°C). However, high temperatures often require high power input, and the resulting gases need to be burned with air, producing toxic gases (e.g., nitrogen oxides).

[0006] The crude coal gas produced by the carbonization furnace at around 80°C requires an indirect cooling process. A circulating ammonia water pump is used to pump and spray the crude coal gas back for cooling and recycling. The tar and ammonia water separated by the gas / liquid separator enter the circulation pool, and the clarified ammonia water is injected into the ammonia water intermediate tank. The clarified tar flows by gravity to the tar intermediate tank and is pumped into the tar storage tank by the tar pump. The tar is heated and dehydrated and deammonified in the storage tank to form the finished tar. The finished tar is pumped out of the storage tank by the tar pump to the deep processing workshop or transported for sale. The coal gas drawn from the top of the gas / liquid separator enters the bottom of the primary cooling tower, where it is cooled to 25-30°C using circulating cooling water in two stages. It then enters the electrostatic precipitator to remove tar mist. The coal gas is pressurized by a gas blower and sent to a gas storage tank. 40% of the gas is returned to the hot blast stove for combustion, providing a heat source for lump coal production. The remaining 60% of the coal gas is sent to the tar hydrogenation workshop to extract hydrogen, which can also provide a heat source for the self-owned power plant to generate electricity or be sold to other enterprises for use as a heat source. The large amount of wastewater generated by the coal gas purification system is sent to the wastewater purification workshop for purification treatment.

[0007] Meanwhile, traditional processes generate large amounts of phenol-containing wastewater and tar, which require further treatment with pollution reduction equipment, such as scrubbers, demisters, and bag filters for removing particulate matter. In addition, the tar is usually stored in warehouses, which poses certain risks to workers in the vicinity of the warehouses. Furthermore, there are potential transportation risks involved in transporting chemicals from the warehouses to the sales points. Summary of the Invention

[0008] This invention provides a method for preparing calcium coal carbonized pellets by pyrolysis using a sliding arc plasma system, thereby solving the problems of high cost, environmental unfriendliness, and low added value caused by the use of traditional methods to prepare calcium coal carbonized pellets in the prior art.

[0009] A method for preparing calcium coal pellets by pyrolysis using a sliding arc plasma system, wherein the sliding arc plasma system includes a calcium coal pellet preparation unit, a pyrolysis chamber, a sliding arc reforming oxidation system reactor, and a crude syngas purification unit, and the method includes the following steps:

[0010] Step S1: Quicklime and raw coal are transported to the calcium coal pellet preparation unit, and the formed calcium coal pellets are transported to the pyrolysis chamber;

[0011] Step S2: Pyrolyze calcium coal pellets in the pyrolysis chamber to obtain and output calcium coal oxidized pellets; introduce the crude coal gas generated from the pyrolysis of calcium coal pellets in the pyrolysis chamber into the plasma zone of the sliding arc reforming oxidation system reactor, and simultaneously introduce a preset volume of gaseous oxidant into the sliding arc reforming oxidation system reactor to mix the gaseous oxidant with the crude coal gas.

[0012] Step S3: Plasma induces the crude coal gas to undergo a reforming and oxidation reaction, producing high-temperature crude syngas, which is then transported to the crude syngas purification unit and the pyrolysis chamber, respectively.

[0013] Preferably, the sliding arc reforming oxidation system reactor includes a sliding arc plasma generator and a reforming oxidation system reactor, and step S2 includes:

[0014] Step S21: Pyrolyze calcium coal pellets in the pyrolysis chamber to obtain and output calcium coal pyrolysis pellets;

[0015] Step S22: Apply a high voltage to the electrodes in the sliding arc plasma generator to generate sliding non-thermal arc plasma, and transport the sliding non-thermal arc plasma to the plasma region;

[0016] Step S23: Introduce the crude coal gas generated from the pyrolysis of calcium coal pellets in the pyrolysis chamber into the plasma zone of the reforming oxidation system reactor, and simultaneously introduce a gaseous oxidant into the reforming oxidation system reactor so that the gaseous oxidant mixes with the crude coal gas.

[0017] Preferably, in step S23, before introducing the gaseous oxidant into the sliding arc reforming oxidation system reactor, the reforming oxidation system reactor is preheated to the operating temperature.

[0018] Preferably, the operating temperature is 750°C to 900°C.

[0019] Preferably, in step S3, the high-temperature crude syngas is transported to the crude syngas purification unit, purified into syngas, and then the syngas is used as a raw material for chemical products and transported to external equipment.

[0020] Preferably, in step S3, the high-temperature crude syngas is transported to the crude syngas purification unit, purified into syngas, and then the syngas is used as a raw material for chemical products and transported to external equipment. When the syngas is transported to the external equipment, its outlet temperature is 300°C to 450°C.

[0021] Preferably, in step S3, the temperature of the high-temperature crude syngas delivered to the pyrolysis chamber is 750°C to 900°C.

[0022] Preferably, the gaseous oxidant is air, oxygen, water vapor, or carbon dioxide.

[0023] Preferably, the oxygen content of the preset volume of gaseous oxidant is 5-100%.

[0024] Preferably, the high-temperature crude syngas is an oxide that does not contain nitrogen oxides.

[0025] The advantages and beneficial effects of the method of this invention are as follows: 1. Using low-priced raw coal to replace coke, semi-coke or other carbonaceous raw materials (including petroleum coke, etc.) has the advantage of low cost due to its cheapness and availability; 2. It does not require processes such as tar separation and water purification, thus improving environmental friendliness; 3. The crude coal gas from pyrolysis is rich in hydrogen, which is beneficial for comprehensive chemical utilization with the tail gas of the calcium carbide furnace (mainly CO), realizing multi-product production and increasing added value. Attached Figure Description

[0026] Figure 1 This is a flowchart of the method of the present invention;

[0027] Figure 2 This is a detailed flowchart of step S2 in the method of the present invention;

[0028] Figure 3 This is a structural block diagram of the sliding arc plasma system of the present invention.

[0029] in,

[0030] 1. Calcium coal pellet preparation unit; 2. Pyrolysis chamber; 3. Sliding arc reforming oxidation system reactor; 4. Crude syngas purification unit; 3.1. Sliding arc plasma generator; 3.2. Reforming oxidation system reactor. Detailed Implementation

[0031] The preferred embodiments of the present invention will be described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are for illustration and explanation only and are not intended to limit the present invention.

[0032] A method for preparing calcium coal pellets by pyrolysis using a sliding arc plasma system, wherein the sliding arc plasma system includes a calcium coal pellet preparation unit 1, a pyrolysis chamber 2, a sliding arc reforming oxidation system reactor 3, and a crude syngas purification unit 4, and the method includes the following steps:

[0033] Step S1: Quicklime and raw coal are transported to calcium coal pellet preparation unit 1, and the formed calcium coal pellets are transported to pyrolysis chamber 2;

[0034] Step S2: Pyrolysis chamber 2 pyrolyzes calcium coal pellets to obtain and output calcium coal pyrolysis pellets; the crude coal gas generated by pyrolysis of calcium coal pellets in pyrolysis chamber 2 is introduced into the plasma zone of the sliding arc reforming oxidation system reactor 3, and at the same time, a preset volume of gaseous oxidant is introduced into the sliding arc reforming oxidation system reactor 3 to mix the gaseous oxidant with the crude coal gas.

[0035] Step S3: Plasma induces crude coal gas to undergo reforming and oxidation reaction, producing high-temperature crude syngas, which is then transported to crude syngas purification unit 4 and pyrolysis chamber 2 respectively.

[0036] Specifically, quicklime and raw coal enter the calcium coal pellet preparation unit 1 to form calcium coal pellets. The calcium coal pellets are then transferred to the pyrolysis chamber 2 for pyrolysis, releasing combustible crude coal gas. Combustible crude coal gas is an environmentally harmful gas, so it must be transported from the pyrolysis chamber 2 to the sliding electric arc reforming oxidation system reactor 3. After pyrolysis, the calcium coal pellets are processed into calcium coal oxidized pellets.

[0037] The chemical composition of the pyrolysis crude coal gas (a gaseous composition of 35% hydrogen, 20% carbon monoxide, 19% nitrogen, 8% methane, 8% carbon dioxide, 4% tar, and 6% water) can be in gaseous form when it is fed to the sliding arc reforming oxidation system reactor 3. The combustible material crude coal gas can be directly processed by the sliding arc reforming oxidation system reactor 3 without any prior incineration, combustion, or other treatment.

[0038] In a preferred embodiment of the present invention, the sliding arc reforming oxidation system reactor 3 includes a sliding arc plasma generator 3.1 and a reforming oxidation system reactor 3.2, and step S2 includes:

[0039] Step S21: Pyrolysis chamber 2 pyrolyzes calcium coal pellets to obtain and output calcium coal pyrolysis pellets;

[0040] Step S22: Apply a high voltage to the electrodes inside the sliding arc plasma generator 3.1 to generate sliding non-thermal arc plasma, and transport the sliding non-thermal arc plasma to the plasma region;

[0041] Step S23: The crude coal gas generated from the pyrolysis of calcium coal pellets in the pyrolysis chamber 2 is introduced into the plasma zone of the reforming oxidation system reactor 3.2, and a gaseous oxidant is introduced into the reforming oxidation system reactor 3.2 at the same time to mix the gaseous oxidant with the crude coal gas.

[0042] Among them, the sliding arc plasma generator 3.1 is a high-energy plasma arc system, which is called a non-thermal plasma system because the process used by the sliding arc plasma generator 3.1 does not provide a large amount of heat input for the oxidation reaction.

[0043] The gaseous oxidant and the combustible raw gas can be mixed in the reforming oxidation system reactor 3.2, or the combustible raw gas and gaseous oxidant can be premixed before being injected into the reforming oxidation system reactor 3.2.

[0044] Generally, the reforming oxidation system reactor 3.2 reforms and oxidizes combustible crude gas, producing oxidation products free of or substantially free of harmful substances. The oxidation process is described in more detail below with reference to the following equations. It should be noted that the oxidation process depends at least in part on the amount of gaseous oxidant combined with the combustible crude gas and the temperature generated by the heat released during the reaction; partial oxidation or reforming of the combustible crude gas produces reforming products, such as syngas; reforming occurs when the oxygen content is less than the stoichiometric level. In some embodiments, a 30-40% stoichiometric oxygen level is used to achieve the reforming process; a typical reforming equation is:

[0045]

[0046] Another typical renormalization equation is:

[0047]

[0048] In contrast, complete oxidation (simply referred to as oxidation of combustible materials) produces oxidation products and occurs when the oxygen content exceeds a stoichiometric amount. In some embodiments, the oxidation process is achieved using a 5-100% excess stoichiometric oxygen level, and the oxidation equation is as follows:

[0049]

[0050] Other equations can also be used to describe other types of reforming and oxidation processes.

[0051] While reforming processes may be endothermic or exothermic, oxidation processes are exothermic. Therefore, the reactants used in oxidation processes may not require preheating. Nevertheless, it is useful to keep some or all of the reforming-oxidation system reactor 3.2 within its operating temperature range to maintain the operating temperature of the sliding arc pyrolysis reforming-oxidation system in the range of approximately 700°C to 1000°C; other embodiments may use different operating temperature ranges.

[0052] The sliding arc reforming oxidation system reactor 3 shown includes a sliding arc plasma generator 3.1 and a reforming oxidation system reactor 3.2, which includes a plasma zone, a post-plasma reaction zone, and a heat transfer zone. Although three separate functional zones are described, some embodiments can achieve the functions of different zones at approximately the same time and / or near the same physical proximity; for example, heat transfer corresponding to the heat transfer zone can occur during the plasma generation process corresponding to the plasma zone; similarly, heat transfer corresponding to the heat transfer zone can also occur at approximately the same location as the post-plasma reaction zone. For example, a sliding arc plasma generator acts as a catalyst to initiate the oxidation process; more specifically, the plasma can ionize or decompose one or more reactants to produce reactive elements.

[0053] After ionization, the reactants enter the post-plasma reaction zone, which is beneficial for the homogenization of the oxidizing composition. Within the post-plasma reaction zone, the reactants are provided with space and time for mixing to help the reaction continue. In some embodiments, the post-plasma reaction zone also promotes the balance of gas species and heat transfer.

[0054] The heat transfer zone also facilitates the transfer of heat from the oxidation products to the pyrolysis chamber 2. As another example, the active flow of the cooling medium can be used to rapidly cool the oxidation products.

[0055] The sliding arc plasma generator 3.1 includes a pair of electrodes. However, other embodiments may include more than two electrodes. For example, some embodiments of the sliding arc plasma generator 3.1 may include three electrodes. Other embodiments of the sliding arc plasma generator 3.1 may include six electrodes or other numbers of electrodes. Each electrode is coupled to an electrical conductor to provide an electrical signal to the corresponding electrode. In the case of implementing multiple electrodes, some electrodes may be coupled to the same electrical conductor, placing them on the same phase of a single-phase or multi-phase power distribution system.

[0056] A high electric field gradient is generated between each pair of electrodes. For example, if there is a 2 mm gap between a pair of electrodes, the potential between the electrodes is approximately 6-9 kV.

[0057] Through plasma (in the direction indicated by the arrow). The high voltage between the electrodes ionizes the working gas mixture, which allows current to flow between the electrodes in the form of an electric arc. This movement of ions in the working gas mixture in an electric field with a high potential gradient causes collisions, thereby generating free radicals. The free radicals trigger a chain reaction that ignites the combustible material.

[0058] As an operational example of the reforming oxidation system reactor 3.2, the volatile crude coal gas from the pyrolysis of calcium coal pellets, containing a gaseous composition of 35% hydrogen, 20% carbon monoxide, 19% nitrogen, 5% methane, and 8% carbon dioxide, can be used as a flammable material. The pyrolysis operating temperature is maintained in the range of approximately 700°C to 1000°C.

[0059] Initial heating is achieved by introducing a mixture of gaseous hydrocarbons and air into the reforming oxidation system reactor 3.2. Examples of such gases include natural gas, liquefied petroleum gas (LPG), propane, methane, and butane. Once the temperature of the reforming oxidation system reactor 3.2 reaches its operating temperature of approximately 800°C, the flow of gaseous hydrogen and carbon is shut off, and raw coal gas is introduced. The flow rates of both air and raw coal gas are adjusted to maintain an appropriate stoichiometric ratio, while the total flow rate is adjusted to keep the sliding arc plasma generator 3.1 at a specific operating temperature or within its operating temperature range.

[0060] As an alternative, oxygen can be used instead of air to reduce the total amount of oxidizing gases. Furthermore, air can be used to cool the reforming oxidation system reactor 3.2, while oxygen is introduced along with the combustible material to complete the reforming oxidation of the combustible material.

[0061] To further optimize the above scheme, in step S23, before introducing the gaseous oxidant into the sliding arc reforming oxidation system reactor 3, the reforming oxidation system reactor 3.2 is preheated to the operating temperature.

[0062] To further optimize the above scheme, the operating temperature is 750℃ to 900℃.

[0063] In a preferred embodiment of the present invention, in step S3, the high-temperature crude syngas is transported to the crude syngas purification unit 4, purified into syngas, and then the syngas is used as a raw material for chemical products and transported to external equipment.

[0064] To further optimize the above scheme, in step S3, after the high-temperature crude syngas is transported to the crude syngas purification unit 4, it is purified into syngas and then used as a raw material for chemical products to be transported to external equipment. When the syngas is transported to the external equipment, its outlet temperature is 300°C to 450°C.

[0065] Specifically, the volatile syngas outlet temperature is 300℃ to 450℃. It is a mixture of crude coal gas and coal tar (steam state) generated during the pyrolysis of calcium coal pellets, and carries a small amount of dust. After passing through the dust removal system of the two-stage cyclone dust collector and the high-temperature crude coal gas ejector, it can be introduced as a combustible material into the sliding electric arc reforming oxidation system reactor 3.

[0066] In a preferred embodiment of the present invention, in step S3, the temperature of the high-temperature crude syngas delivered to the pyrolysis chamber 2 is 750°C to 900°C.

[0067] In a preferred embodiment of the present invention, the gaseous oxidant is air, oxygen, water vapor, or carbon dioxide.

[0068] The gaseous oxidant can be air, oxygen, water vapor, or carbon dioxide, or other types of gaseous oxidants. The gaseous oxidant controller includes a manual control valve, an electronic control valve, a pressure regulator, an orifice plate of a specified size, or other types of flow controllers. Embodiments of the controller include a gaseous oxidant position sensor feedback system.

[0069] In a preferred embodiment of the present invention, the oxygen content of the gaseous oxidant in the preset volume is 5-100%.

[0070] In a preferred embodiment of the present invention, the high-temperature crude syngas is an oxide that does not contain nitrogen oxides.

[0071] Specifically, (1) using low-priced raw coal and quicklime to replace coke, semi-coke or other carbonaceous raw materials (including petroleum coke, etc.) has the advantage of low cost due to its cheapness and availability; (2) the high temperature of the calcium carbide furnace charge, the high resistivity of the carbonaceous raw materials, and the high density of the carbonaceous raw materials and lime powder (C a (2) The close contact reaction speed is accelerated, and the unit power consumption of calcium carbide is greatly reduced; (3) There is no need for tar separation, water purification and other processes, which improves environmental protection; (4) The synthesis gas output after pyrolysis is rich in hydrogen, which is conducive to the comprehensive chemical utilization of calcium carbide furnace tail gas (mainly CO), realizing multi-product production and increasing added value. Therefore, the development of a new process for preparing calcium coal pellets (for calcium carbide production) by pyrolysis using a sliding arc plasma system will have a breakthrough significance for the entire calcium carbide industry, and also provide a new way for the clean and efficient utilization of low-priced pulverized coal.

[0072] The terms “comprising” and “having”, and any variations thereof, in the specification, claims, and accompanying drawings of this application are intended to cover non-exclusive inclusion, for example, a process, method, system, product, or apparatus that includes a series of steps or units is not necessarily limited to those steps or units explicitly listed, but may include other steps or units not explicitly listed or inherent to such process, method, product, or apparatus.

[0073] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system, characterized in that, The sliding arc plasma system includes a calcium coal pellet preparation unit (1), a pyrolysis chamber (2), a sliding arc reforming oxidation system reactor (3), and a crude syngas purification unit (4). The method includes the following steps: Step S1: Quicklime and raw coal are transported to the calcium coal pellet preparation unit (1), and the formed calcium coal pellets are transported to the pyrolysis chamber (2); Step S2: The pyrolysis chamber (2) pyrolyzes calcium coal pellets to obtain and output calcium coal oxidized pellets; the crude coal gas generated from the pyrolysis of calcium coal pellets in the pyrolysis chamber (2) is introduced into the plasma zone of the sliding arc reforming oxidation system reactor (3), and a preset volume of gaseous oxidant is introduced into the sliding arc reforming oxidation system reactor (3) to mix the gaseous oxidant with the crude coal gas; the sliding arc reforming oxidation system reactor (3) includes a sliding arc plasma generator (3.1) and a reforming oxidation system reactor (3.2), and step S2 includes: Step S21: Pyrolysis chamber (2) pyrolyzes calcium coal pellets to obtain and output calcium coal pyrolysis pellets; Step S22: Apply a high voltage to the electrodes in the sliding arc plasma generator (3.1) to generate sliding non-thermal arc plasma, and transport the sliding non-thermal arc plasma to the plasma region; Step S23: Introduce the crude coal gas generated from the pyrolysis of calcium coal pellets in the pyrolysis chamber (2) into the plasma zone of the reforming oxidation system reactor (3.2), and simultaneously introduce a gaseous oxidant into the reforming oxidation system reactor (3.2) so that the gaseous oxidant mixes with the crude coal gas; Step S3: Plasma induces the crude coal gas to undergo a reforming and oxidation reaction to generate high-temperature crude syngas. The high-temperature crude syngas is then transported to the crude syngas purification unit (4) and the pyrolysis chamber (2), respectively. The temperature of the high-temperature crude syngas transported to the pyrolysis chamber (2) is 750°C to 900°C.

2. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 1, characterized in that, In step S23, before introducing the gaseous oxidant into the sliding arc reforming oxidation system reactor (3.2), the reforming oxidation system reactor (3.2) is preheated to the operating temperature.

3. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 2, characterized in that, The operating temperature is 750°C to 900°C.

4. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 1, characterized in that, In step S3, the high-temperature crude syngas is transported to the crude syngas purification unit (4) for purification into syngas, and the syngas is then used as a raw material for chemical products and transported to external equipment.

5. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 4, characterized in that, In step S3, the high-temperature crude syngas is transported to the crude syngas purification unit (4) and purified into syngas. The syngas is then used as a raw material for chemical products and transported to external equipment. When the syngas is transported to the external equipment, its outlet temperature is 300°C to 450°C.

6. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 1, characterized in that, The gaseous oxidant is air, oxygen, water vapor, or carbon dioxide.

7. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 1, characterized in that, The oxygen content of the gaseous oxidant in the preset volume is 5-100%.

8. The method for preparing calcium coal pyrolysis pellets using a sliding arc plasma system according to claim 1, characterized in that, The high-temperature crude synthesis gas is an oxide that does not contain nitrogen oxides.

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