Simulation of Acetylene Formation from Methane in a Plasma Jet

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Abstract

This work is devoted to the numerical modeling of the reaction of methane conversion to acetylene under plasma-jet pyrolysis conditions and a comparison of the obtained results with the available experimental data. The calculations were performed within the framework of the ideal plug-flow reactor model for atmospheric pressure. The analysis of the main processes of methane decomposition and acetylene formation was carried out in cases where either hydrogen or methane was used as a plasma-forming gas. The results of calculations of the main products of methane decomposition (hydrogen and acetylene) agree quite well with the experimental data.

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About the authors

I. V. Bilera

A.V. Topchiev Institute of Petrochemical Synthesis of the Russian Academy of Sciences

Email: lebedev@ips.ac.ru
Russian Federation, Moscow

Yu. A. Lebedev

A.V. Topchiev Institute of Petrochemical Synthesis of the Russian Academy of Sciences

Author for correspondence.
Email: lebedev@ips.ac.ru
Russian Federation, Moscow

A. Yu. Titov

A.V. Topchiev Institute of Petrochemical Synthesis of the Russian Academy of Sciences

Email: lebedev@ips.ac.ru
Russian Federation, Moscow

I. L. Epstein

A.V. Topchiev Institute of Petrochemical Synthesis of the Russian Academy of Sciences

Email: lebedev@ips.ac.ru
Russian Federation, Moscow

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Supplementary files

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2. Fig. 1. Scheme of plasma chemical reactor. 1 - plasmatron, 2 - reactor, 3 - quenching zone, 4 - hydrogen or methane (natural gas) supply, 5 - additional methane (natural gas) supply, 6 - water quenching, 7 - flow of reaction products into the separation unit

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3. Fig. 2. Mechanism of soot particle nucleation molecule formation

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4. Fig. 3. Dependence of gas temperature (a), volume concentrations of methane (b), molecular hydrogen (c) and acetylene (d) on gas residence time in the reactor at different values of cold methane flow rate F2 for the case F1 = 50 l/min, T1 = 3500 K, T2 = 300 K, p = 1 atm. F2 /F1 = 1.0 (1), F2 /F1 = 1.2 (2), F2 /F1 = 1.4 (3), F2/F1 = 1.6 (4), F2/F1 = 2.0 (5)

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5. Fig. 4. Dependence of experimental [27] (symbols and thin solid lines) and calculated (thick solid lines) values of concentrations of methane and its main decay products on the ratio of cold and hot methane flows for the case F1 = 50 l/min, T1 = 3500 K, T2 = 300 K, p = 1 atm. Thick dashed lines - calculation taking into account mixing of cold and hot streams. 1, 2 - N2; 3, 4 - C2H2; 5, 6, 11 - CH4; 7, 8, 12 - C4H2; 9, 10, 13 - C4H4

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6. Fig. 5. Dependence of soot yield on gas residence time in the reactor at different values of cold methane flow rate F2 for the case M1 = 50 l/min, T1 = 3500 K, T2 = 300 K, p = 1 atm. F2/F1 = 1.0 (1), F2/F1 = 1.2 (2), F2/F1 = 1.4 (3), F2/F1 = 1.6 (4), F2/F1 = 2.0 (5)

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7. Fig. 6. Dependence of experimental [26] (symbols and thin solid lines) and calculated (thick solid lines) yields of main components: (a) on methane volume flow rate at hydrogen flow rate of 50 l/min, (b) on hydrogen volume flow rate at methane flow rate of 80 l/min. 1, 2 - H2; 3, 4 - C2H2; 5, 6 - CH4; 7, 8 - C2H4

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8. Fig. 7. Time dependence of methane content and its pyrolysis products for optimal conditions of Table 2. 1 - CN4, 2 - N2, 3 - C2N4, 4 - C2N2

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