A method for performing CO2 and VOCs collaborative resource treatment at normal temperature and pressure

Abstract

The application discloses a method for carrying out CO2 and VOCs collaborative resource treatment under normal temperature and pressure, comprising the following steps: taking CO2 and VOCs as reaction gas, and carrying out reaction in a DBD plasma reactor loaded with a Ni-based catalyst to prepare synthesis gas; the VOCs are benzene, toluene or xylene; and the Ni-based catalyst is at least one of Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2. The application combines the DBD plasma reactor with the Ni-based catalyst, utilizes the synergy between the plasma and the catalyst to improve the selectivity of different products of the carbon dioxide catalytic reforming and the energy utilization efficiency.

Description

Technical Field

[0001] This application relates to the field of CO2 resource utilization technology, and in particular to an efficient technology system that can achieve the synergistic resource utilization of CO2 and VOCs at room temperature and pressure. Background Technology

[0002] Rapid economic development has led to a surge in energy consumption, resulting in a continuous increase in greenhouse gas emissions and a worsening greenhouse effect. Statistics show that CO2 is the primary contributor to the greenhouse effect. From the perspective of emission sources, CO2 emissions mainly originate from two sources: energy consumption and industrial production. Energy consumption accounts for over 80% of total CO2 emissions, far exceeding the latter, indicating that carbon emissions primarily come from energy-intensive industries, exhibiting two main characteristics: large emissions and concentrated carbon sources.

[0003] Catalytic reforming of CO2 is a promising method in CO2 resource utilization technology. It not only converts CO2, but also indirectly utilizes hydrogen species generated after the breaking of CH bonds in VOCs (alkanes, alkenes, alcohols, benzene series compounds, etc.) to carry out catalytic reforming reactions with CO2 to produce syngas (CO+H2) products with high economic benefits.

[0004] Because of the high stability of CO2, traditional CO2 catalytic reforming reactions can only be carried out in a high-temperature and high-pressure environment. These harsh reaction conditions place extremely high demands on the thermal stability of the catalyst, and the reaction is accompanied by high energy consumption, which greatly limits the widespread application of this technology in industrial production. Summary of the Invention

[0005] The purpose of this application is to provide a method for the synergistic resource recovery of CO2 and VOCs under ambient temperature and pressure. By combining a DBD plasma reactor with a Ni-based catalyst, the synergistic effect between plasma and catalyst is used to improve the selectivity and energy utilization efficiency of different products of carbon dioxide catalytic reforming.

[0006] A method for the synergistic resource recovery of CO2 and VOCs at room temperature and pressure, characterized by comprising:

[0007] Syngas was prepared by reacting CO2 and VOCs in a DBD plasma reactor loaded with a Ni-based catalyst.

[0008] The VOCs are benzene, toluene, or xylene;

[0009] The Ni-based catalyst is at least one of Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2.

[0010] In recent years, plasma technology has been increasingly applied in the field of gas conversion. Dielectric barrier discharge (DBD) is a method of generating plasma, which has the main advantages of easy reaction initiation, flexible and simple operation, low reaction system cost, and easy scalability. However, using plasma alone still has two major drawbacks: poor product selectivity and low energy utilization efficiency.

[0011] DBD plasma synergistic catalysis technology can generate high-energy electrons and ions, and can achieve the dissociation and activation of CO2 and VOCs molecules through gas-phase excitation. By coupling plasma with catalyst, the synergistic effect between the two can be used to further improve the selectivity of products and energy utilization efficiency under normal temperature and pressure, so as to realize the efficient resource utilization of CO2 and VOCs.

[0012] Optionally, the DBD plasma reactor uses dielectric barrier discharge and includes a high-voltage electrode, a ground electrode, and a quartz tube. The ground electrode is covered on the outer surface of the quartz tube by a capacitor. The high-voltage electrode is placed inside the quartz tube and connected to the plasma power supply. The quartz tube has an inlet and an outlet at both ends. The gaps in the quartz tube are filled with all or part of the aforementioned Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2 catalysts. The inlet is used to introduce a mixture of toluene vapor and CO2 as reaction gas, and the outlet is connected to an in-situ mass spectrometer for detecting the composition of the gas after the reaction.

[0013] Optionally, the construction of the reaction system includes:

[0014] 1) Construct a DBD reactor and fill the DBD reactor with the Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2 catalysts as described above, respectively;

[0015] 2) Argon gas is introduced into the DBD reactor as a carrier gas, and a mass flow controller is used to fix the gas flow rate. The argon gas is then introduced into the toluene vapor by passing through an ice bath bubbler containing liquid toluene. In a gas mixer, the toluene vapor is mixed with CO2. After the gas path stabilizes, the plasma power supply is turned on to carry out the carbon dioxide catalytic reforming reaction.

[0016] Optionally, the concentration of VOCs vapor in the reaction gas is 400–600 ppmv, and the concentration of CO2 gas is 3–6%.

[0017] Preferably, the concentration of benzene, toluene or xylene vapor in the reaction gas is 500 ppmv, and the concentration of CO2 gas is 5%.

[0018] Optionally, the flow rate of the reaction gas is 150-250 mL / min.

[0019] Optionally, the discharge voltage of the power supply in the plasma reactor is 7.5-9.5kV, and the discharge frequency is 22.5kHz.

[0020] Optionally, the content of Ni, the active component, in the Ni-based catalyst is 8–12 wt.%.

[0021] Preferably, the content of the active component Ni in the Ni-based catalyst is 10 wt.%.

[0022] Optionally, the Ni-based catalyst is filled in the plasma reactor at a rate of 2.5 mg / mL to 5.0 mg / mL.

[0023] Optionally, the Ni-based catalyst has a particle size of 40-60 mesh.

[0024] For the reaction gas, most preferably, the reaction gas is a mixture of CO2 and toluene; the toluene vapor concentration in the mixture is 500 ppmv, and the CO2 gas concentration is 5%. Correspondingly, for the catalyst, most preferably, the Ni-based catalyst is Ni / MnO2; in the Ni / MnO2, Ni is the active component and MnO2 is the support, and the content of the active component in the Ni / MnO2 is 10 wt.%; for the reaction conditions, most preferably, the flow rate of the reaction gas is 200 mL / min; the discharge voltage of the power supply in the plasma reactor is 8.5 kV, and the discharge frequency is 22.5 kHz.

[0025] Compared with the prior art, this application has at least one of the following beneficial effects:

[0026] (1) The method described in this application realizes the efficient conversion of CO2 and VOCs (benzene, toluene or xylene) into syngas (CO+H2) under normal temperature and pressure conditions. The process is simple and the method is green. By establishing the high-efficiency technology system in this application, the DBD plasma reactor is combined with the catalyst. By utilizing the synergistic effect between low temperature plasma and catalyst, the CO selectivity is as high as 89.7%, the CO production energy efficiency is as high as 38.4 g / kWh, the CO2 conversion energy efficiency is as high as 46.6 g / kWh, and the H2 production energy efficiency is 0.62 g / kWh, realizing the efficient and stable conversion of CO2 and VOCs under normal temperature and pressure.

[0027] (2) Compared with the NTP-MnOx@13X system for catalyzing CO2-toluene reforming disclosed by Xiao K et al. in the published paper "Synergistic effect of dielectric barrier discharge plasma and Mn catalyst on CO2 reforming of toluene, 2021; 285:119057", the CO2 conversion efficiency is significantly improved.

[0028] (3) Compared to Liu L et al.'s published paper "Plasma-Catalytic CO2 Reforming of Toluene over Hydrotalcite-Derived NiFe / (Mg,Al)O", x The NiFe / (Mg,Al)O3 disclosed in Catalysts, 2023 x The system catalyzes the CO2-toluene catalytic reforming reaction, significantly improving the CO2 conversion efficiency. Attached Figure Description

[0029] Figure 1 The graph shows the relationship between toluene and CO2 conversion rates for empty tube, Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2 catalysts.

[0030] Figure 2 The graph shows the selectivity of CO, H2, and CH4 for empty tube, Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2 catalysts.

[0031] Figure 3 The graph shows the relationship between CO2 conversion efficiency and CO production efficiency for empty tube, Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2 catalysts;

[0032] Figure 4 The energy efficiency relationship between CH4 and H2 generation for empty tube, Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2 catalysts is shown in the figure.

[0033] Figure 5 This is a comparison chart showing the CO2 conversion efficiency of Example 1 of this application with that of Comparative Example 1 and Comparative Example 2.

[0034] Figure 6 This is a schematic diagram of a specific structure of the reaction system of this application.

[0035] Figure 6 The reference numerals in the accompanying drawings are as follows:

[0036] 1. Gas cylinder; 2. Mass flow controller; 3. Mixer; 4. Ice bath bubble flask; 5. DBD reactor; 6. External electrode; 7. Internal electrode; 8. High voltage power supply; 9. Current probe; 10. High voltage probe; 11. Oscilloscope; 12. Capacitor; 13. Mass spectrometer. Detailed Implementation

[0037] The technical solution of this application will be clearly and completely described below with reference to specific embodiments. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. Based on the embodiments in this application, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the scope of protection of this application.

[0038] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application.

[0039] A highly efficient technology system for the synergistic resource recovery of CO2 and VOCs under ambient temperature and pressure is proposed, comprising a DBD plasma reactor and Ni-based catalysts. The Ni-based catalysts have the chemical formulas Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2. The designed highly efficient technology system for the synergistic resource recovery of CO2 and VOCs exhibits excellent reaction performance under ambient temperature and pressure conditions. The Ni / BaTiO3 and Ni / ZrO2 catalyst supports in this system have high dielectric constants, which can increase the electric field energy density in the DBD plasma reactor, thereby improving the CO2 conversion rate. The Ni / CeO2 catalyst support has the characteristic of easily changing the valence state of metal ions; the decrease in the valence state of its metal ions is accompanied by the generation of a large number of oxygen vacancies, thus effectively promoting the adsorption and activation of CO2. The Ni / MnO2 catalyst, due to its strong metal-support interaction, forms NiMnO2. x Solid solutions, with their strong chemical bonds, give Ni species higher dispersion and stability, effectively suppressing catalyst deactivation caused by the aggregation and growth of Ni species during the reaction process.

[0040] In one implementation method, the steps for establishing an efficient technology system for the synergistic resource utilization of CO2 and VOCs are as follows:

[0041] The fabrication of a DBD reactor (conventional equipment) includes:

[0042] In one specific embodiment, the schematic diagram of the constructed reaction system structure is as follows: Figure 6 As shown:

[0043] DBD reactor 5 discharges via dielectric barrier and includes a high-voltage electrode (i.e., inner electrode 7), a ground electrode (i.e., outer electrode 6), and a quartz tube. The ground electrode is covered on the outer surface of the quartz tube by a capacitor. The high-voltage electrode is placed inside the quartz tube and connected to a plasma power source (i.e., high-voltage power source 8). The quartz tube has an inlet and an outlet at both ends. The gaps in the quartz tube are filled with at least one of the aforementioned Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2 catalysts. The inlet is used to introduce a mixture of VOC vapor (e.g., toluene) and CO2 (from mixer 3). The outlet is connected to an in-situ mass spectrometer 13 for detecting the composition of the gas after the reaction.

[0044] The preparation of Ni-based catalysts includes:

[0045] Preparation of catalyst support:

[0046] 1) Prepare a precursor solution by placing hexadecyltrimethylammonium bromide and manganese nitrate aqueous solution in deionized water;

[0047] 2) Quickly add the ammonium bicarbonate aqueous solution to the mixed solution while stirring continuously;

[0048] 3) Wash the resulting precipitate with deionized water and dry it;

[0049] 4) Granulate and dry to prepare the required powder;

[0050] 5) The obtained powder is calcined to complete the preparation of the MnO2 support;

[0051] 6) Commercial BaTiO3, CeO2 and ZrO2 were selected as supports for Ni / BaTiO3, Ni / CeO2 and Ni / ZrO2 catalysts.

[0052] Catalyst preparation:

[0053] 1) Place the mixture of nickel nitrate hexahydrate and the support (BaTiO3, CeO2, ZrO2 and MnO2, respectively) in deionized water and stir continuously;

[0054] 2) Add an aqueous solution of sodium carbonate as a precipitant to the mixed solution dropwise;

[0055] 3) After aging the obtained suspension, separate it using a centrifuge;

[0056] 4) Granulate and dry to prepare the required powder;

[0057] 5) The obtained powder is calcined to complete the preparation of the catalyst;

[0058] 6) Before evaluating the catalyst, reduce it in an H2 / Ar atmosphere.

[0059] Taking the preparation of Ni / MnO2 catalyst as an example, the entire preparation process includes:

[0060] 1) Prepare a precursor solution by placing hexadecyltrimethylammonium bromide and manganese nitrate aqueous solution in deionized water;

[0061] 2) Quickly add the ammonium bicarbonate aqueous solution to the mixed solution while stirring continuously;

[0062] 3) Wash the resulting precipitate with deionized water and dry it;

[0063] 4) Granulate and dry to prepare the required powder;

[0064] 5) The obtained powder is calcined to complete the preparation of the MnO2 support;

[0065] 6) The mixture of nickel nitrate hexahydrate and MnO2 support was placed in deionized water according to different loading amounts and stirred continuously;

[0066] 7) Add an aqueous solution of sodium carbonate as a precipitant to the mixed solution dropwise;

[0067] 8) After aging the obtained suspension, separate it using a centrifuge;

[0068] 9) Granulate and dry to prepare the required powder;

[0069] 10) The obtained powder is calcined to complete the preparation of the Ni / MnO2 catalyst;

[0070] 11) Before evaluating the catalyst, reduce the catalyst in an H2 / Ar atmosphere.

[0071] In the specific embodiments of this application, the cetyltrimethylammonium bromide, manganese nitrate, ammonium bicarbonate, nickel nitrate hexahydrate, and sodium carbonate used are all of analytical grade AR; the capacitance of deionized water is required to be less than 1 μs / cm; the commercial BaTiO3, CeO2, and ZrO2 supports used are required to be 99.99% (metal basis) and 50 nm.

[0072] Preferably, the DBD plasma discharge is generated by a plasma power source in a coaxial quartz tube with an outer diameter of 10 mm and a wall thickness of 1 mm. The plasma power source is a CTP 2000K, the high-voltage electrode is a stainless steel rod with a diameter of 2 mm, the grounding electrode is made of stainless steel mesh, the length of the discharge area is 50 mm, and the power during the reaction is calculated from the Lissajous curve.

[0073] The in-situ mass spectrometer is a Tilon LC-D200, which simultaneously detects and calibrates signals at m / z = 2, 16, 28, 44 and 91 to determine the concentrations of H2, CH4, CO, CO2 and toluene.

[0074] To calculate the discharge power, an external capacitor and an oscilloscope are also connected in the circuit. The external capacitor is connected in series in the circuit, and a current detector and a voltage probe are connected in series across the two ends of the capacitor. The oscilloscope is connected between the current detector and the voltage probe and is connected in parallel with the external capacitor.

[0075] Preferably, the catalyst is filled in the discharge region of the quartz tube, and the inlet and outlet are plugged with quartz wool.

[0076] To obtain a high-performance, efficient technology system for the synergistic resource utilization of CO2 and VOCs, it is necessary to adjust the discharge voltage and gas flow rate of the DBD reactor. The specific adjustment process is as follows:

[0077] 1) Prepare Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2 catalysts with 10 wt.% Ni loading; construct a DBD reactor and fill the above Ni / BaTiO3, Ni / CeO2, Ni / ZrO2 and Ni / MnO2 catalysts into the DBD reactor respectively;

[0078] 2) H2 / Ar gas was introduced into the DBD reactor to activate the Ni / BaTiO3, Ni / CeO2, Ni / ZrO2, and Ni / MnO2 catalysts by raising the temperature. After activation, the temperature was lowered to room temperature and switched to the reaction atmosphere. After the gas path stabilized, the plasma power supply was turned on, and the discharge voltage was adjusted sequentially to 7.5kV, 8.5kV, and 9.5kV. The initial concentrations of toluene and CO2 in the reactor were 500 ppmv and 5%, respectively. The flow rates of the reaction atmosphere were adjusted to 150 mL / min, 200 mL / min, and 250 mL / min, respectively. mL / min. During the evaluation process, the gaseous products at the DBD reactor outlet were analyzed by in-situ mass spectrometry. At the same time, the signals at m / z = 2, 16, 28, 44 and 91 were detected and calibrated to determine the concentrations of H2, CH4, CO, CO2 and toluene. CO selectivity, CO2 conversion efficiency, CO production efficiency and H2 production efficiency were used as performance evaluation indicators for DBD reactors with different discharge voltages under a fixed reaction atmosphere. Through this step, the discharge voltage with the highest CO selectivity, CO2 conversion efficiency, CO production efficiency and H2 production efficiency was obtained.

[0079] 3) By adjusting and changing the discharge voltage and gas flow rate of the DBD reactor, the optimal discharge voltage and optimal gas flow rate in the DBD reactor can be determined.

[0080] The energy efficiency (EE) parameter is calculated as shown in equation (1) below:

[0081]

[0082] Where i can be a reactant (CO2) and a product (CO, CH4, H2), F i Converted or Produced M is the molar flow rate of substance i transformed or produced. i (g / mol) is the molar mass of substance i; P is the discharge power in the plasma.

[0083] The following is a description using specific embodiments:

[0084] Example 1

[0085] Preparation of catalyst support:

[0086] 1) Prepare a precursor solution by placing 0.5 g of cetyltrimethylammonium bromide and 7.16 g of manganese nitrate aqueous solution in 100 mL of deionized water;

[0087] 2) Quickly add 100 mL of ammonium bicarbonate aqueous solution to the precursor solution and stir continuously for 12 h;

[0088] 3) Wash the generated precipitate with deionized water and dry it at 80℃ for 12 hours;

[0089] 4) The obtained powder was calcined in air at 400℃ for 4 hours at a heating rate of 2℃ / min to obtain MnO2 support;

[0090] 5) Commercial BaTiO3, CeO2 and ZrO2 were selected as supports for Ni / BaTiO3, Ni / CeO2 and Ni / ZrO2 catalysts.

[0091] Catalyst preparation:

[0092] 1) A mixture of nickel nitrate hexahydrate and 4.0 g of support (BaTiO3, CeO2, ZrO2 and MnO2, respectively) was placed in 150 mL of deionized water with a loading of 10 wt.% Ni and stirred continuously for 1 h.

[0093] 2) Use a 0.2M sodium carbonate aqueous solution as a precipitant, adding it dropwise until the pH of the solution reaches 9-10;

[0094] 3) After aging the obtained suspension at 90℃ for 2 hours, it was separated using a centrifuge;

[0095] 4) The obtained material was dried at 110℃ for 12 hours, ground, and then calcined in dry air at 500℃ for 4 hours.

[0096] 5) Before evaluating the catalyst, it was reduced for 2 h in a 10 vol.% H2 / Ar (40 mL / min) atmosphere at 400 °C, with a heating rate of 5 °C / min.

[0097] Construction of a synergistic reaction system:

[0098] 1) Ni / MnO2 catalyst was prepared by the above method, and a DBD reactor was built. The above Ni / MnO2 catalyst was filled into the DBD reactor. The catalyst loading amount was calculated as 0.5g of catalyst filled into a coaxial quartz tube with an outer diameter of 10mm and a wall thickness of 1mm.

[0099] 2) In the DBD reactor, H2 / Ar gas is introduced to raise the temperature for Ni / MnO2 catalyst reduction. After the reduction is completed, the temperature is lowered to room temperature and switched to the reaction atmosphere. After the gas path is stabilized, the plasma power supply is turned on to carry out carbon dioxide catalytic reforming reaction.

[0100] In this embodiment, the optimal reaction system in the DBD reactor is determined:

[0101] For a Ni / MnO2 catalyst with a Ni loading of 10 wt.%, the discharge parameters of the DBD reactor were optimized. The effects of three different discharge voltages (7.5 kV, 8.5 kV, and 9.5 kV) and three gas flow rates (150 mL / min, 200 mL / min, and 250 mL / min) on CO selectivity, CO2 conversion efficiency, CO production efficiency, and H2 production efficiency were investigated.

[0102] The results of the treatment of the Ni / MnO2 catalyst with a Ni loading of 10 wt.% are as follows:

[0103] 1) The effect of discharge voltage on catalyst performance is shown in Table 1 below:

[0104] Table 1:

[0105]

[0106] As shown in Table 1, when the gas flow rate is stable at 200 mL / min, the Ni / MnO2 catalyst exhibits the highest CO selectivity of 89.7%, the highest CO2 conversion efficiency of 46.6 g / kWh, and the highest H2 production efficiency of 0.62 g / kWh when the discharge voltage is 8.5 kV; and the highest CO production efficiency of 39.7 g / kWh when the discharge voltage is 9.5 kV.

[0107] 2) The effect of gas flow rate on catalyst performance is shown in Table 2 below:

[0108] Table 2:

[0109]

[0110]

[0111] As shown in Table 2, when the discharge voltage stabilizes at 8.5 kV, the CO selectivity, CO production efficiency, and H2 production efficiency of the Ni / MnO2 catalyst first increase and then decrease with increasing gas flow rate as the gas flow rate increases, indicating that a higher gas flow rate promotes CO production. When the reaction gas flow rate is 250 mL / min, the Ni / MnO2 catalyst exhibits higher CO2 conversion efficiency.

[0112] This embodiment also calculates the toluene conversion rate and energy efficiency under different catalyst treatments:

[0113] Ni / BaTiO3: Toluene conversion rate is 100%, energy efficiency is 0.20 mmol / kJ;

[0114] Ni / CeO2: Toluene conversion rate is 100%, energy efficiency is 0.21 mmol / kJ;

[0115] Ni / ZrO2: Toluene conversion rate is 100%, energy efficiency is 0.25 mmol / kJ;

[0116] Ni / MnO2: Toluene conversion rate is 100%, and energy efficiency is 0.30 mmol / kJ.

[0117] Comparative Example 1

[0118] Xiao K et al. investigated the CO2-toluene catalytic reforming performance of the NTP-MnOx@13X system in their published paper, "Synergistic effect of dielectric barrier discharge plasma and Mn catalyst on CO2 reforming of toluene, 2021; 285:119057". The results showed that the NTP-MnOx@13X system achieved a maximum CO2 conversion rate of 29.5%, corresponding to a CO2 conversion efficiency of 0.038 mmol / kJ. In contrast, the highest CO2 conversion efficiency of the DBD plasma-Ni catalyst system in this application is 0.29 mmol / kJ, significantly higher than the parameters described in that paper.

[0119] Comparative Example 2

[0120] Liu L et al., in their publicly available paper "Plasma-Catalytic CO2 Reforming of Toluene over Hydrotalcite-Derived NiFe / (Mg,Al)O", [discussed the following:] x The study of NiFe / (Mg,Al)O was conducted in Catalysts, 2023. x The performance of the CO2-toluene catalytic reforming reaction of the system. In this system, the Ni4Fe1 / (Mg,Al)Ox catalyst has the highest CO2 conversion rate of 44%, and its CO2 conversion efficiency is 0.09 mmol / kJ, which is much lower than the CO2 conversion efficiency in this application.

[0121] The comparison results of the CO2 conversion efficiency of the Ni / MnO2 catalyst system in Example 1 of this application with the CO2 conversion efficiency of Comparative Examples 1 and 2 are as follows: Figure 5 As shown.

[0122] In summary, by comparing the CO selectivity, CO2 conversion efficiency, CO production efficiency, and H2 production efficiency of the Ni / MnO2 catalyst with a Ni loading of 10 wt.% under different discharge voltages and gas flow rates, the optimal reaction conditions for converting CO2 and toluene into CO and H2 within the research scope are as follows: discharge voltage = 8.5 kV, reaction gas flow rate = 200 mL / min, CO selectivity = 89.7%, CO2 conversion efficiency = 46.6 g / kWh (0.29 mmol / kJ), CO production efficiency = 38.4 g / kWh, and H2 production efficiency = 0.62 g / kWh.

[0123] The embodiments described above are merely illustrative of several implementation methods of this application, and while the descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the invention patent. It should be noted that those skilled in the art can make various modifications and improvements without departing from the concept of this application, and these all fall within the protection scope of this application. Therefore, the protection scope of this patent application should be determined by the appended claims.

Claims

1. A method for the synergistic resourceful treatment of CO2 and VOCs at room temperature and pressure, characterized in that, The application relates to a method for preparing syngas. The reaction is carried out in a DBD plasma reactor loaded with a Ni-based catalyst under normal temperature and pressure, with CO2 and VOCs as reaction gases. The VOCs are toluene. The Ni-based catalyst is Ni / MnO2, wherein Ni is an active component and MnO2 is a carrier. The discharge voltage of the power supply in the DBD plasma reactor is 7.5-9.5 kV, and the discharge frequency is 22.5 kHz.

2. The method of claim 1, wherein, The filling amount of the Ni-based catalyst in the plasma reactor is 2.5 mg / mL-5.0 mg / mL.

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