Direct catalytic methanation of biogas – Part II: Techno-economic process assessment and feasibility reflections

Witte, Julia; Künz, Andreas; Biollaz, Serge M.A.; Schildhauer, Tilman J.

doi:10.1016/j.enconman.2018.09.079

Cited by 50 publications

(41 citation statements)

References 11 publications

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“…Data for the methanation process are obtained from the work of Witte et al and Zhang et al . 22,50 Two types of system variations are considered: 1) bubbling fluidized bed with fixed bed methanation; and 2) bubbling fluidized bed methanation followed by membrane gas separation (Fig. 1, middle).…”

Section: Methanationmentioning

confidence: 99%

Life cycle assessment of power-to-gas with biogas as the carbon source

Zhang

Witte

Schildhauer

et al. 2020

Sustainable Energy Fuels

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Section: Methanationmentioning

confidence: 99%

Life cycle assessment of power-to-gas with biogas as the carbon source

Zhang

Witte

Schildhauer

et al. 2020

Sustainable Energy Fuels

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“…Biogas plants have been identified as well‐suited and economically attractive CO 2 source for the application of the methanation reaction , . Therefore, a plant concept was developed for this case which is illustrated in Fig.…”

Section: Development Of An Innovative Plant Concept For Co2methanationmentioning

confidence: 99%

CO₂ Methanation in Microstructured Reactors – Catalyst Development and Process Design

et al. 2019

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The sulfur tolerance of mono‐ and bimetallic ruthenium catalysts for CO2 hydrogenation was investigated in microchannel reactors. H2S was selected as a model compound. It was found that a Ru/CeO2 catalyst deactivates rapidly. Ni was a much better additive to improve the catalyst stability compared to Rh and serves as a sulfur trap. The influence of the support was evaluated showing that a SiO2‐supported catalyst has a higher stability and better selectivity compared to CeO2 and TiO2. A plant concept was developed comprising two‐step methanation with a first adiabatic reactor stage followed by a plate heat‐exchanger reactor with integrated cooling which allows more than 97 % CO2 conversion. A pilot plant will be put into operation in connection with a biogas plant and an electrolyser of 50 kW power consumption.

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“…At higher pressures, the reactor becomes narrower but higher to keep the volume and mass of the catalyst constant. [ 31 ] For fluidizing bigger particles, the reactor could operate at lower pressures, which reduces the operating costs associated with the compression, whereas at higher values of pressure, smaller particles are required. In this case, the particle size needs to be chosen carefully so the catalyst can be fluidized.…”

Section: Resultsmentioning

confidence: 99%

Working diagrams to identify the operating range of a bubbling fluidized bed reactor for the CO₂ methanation

Martin-del-Campo

Kopyscinski

2020

Can J Chem Eng

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Fluidized bed reactors for the catalytic CO 2 methanation is a promising concept within the power-togas (methane) process. Due to the intermittency of renewable electricity generation and thus hydrogen production, the subsequent methanation reactor should also be able to operate at lower feed flow rates, while maintaining fluidized bed conditions. Bubbling fluidized bed reactors offer the required flexibility as shown with the new type of working diagrams. These working diagrams visualize a decision window for (a) determining the reactor diameter and (b) operating the fluidized bed reactor with a turndown ratio of 0.5-1.1. Reducing the turndown ratio (ie, inlet flow rate) could lead to defluidization, thus increasing temperature or reducing the pressure are alternatives to maintain fluidization conditions. The former method is not desired, as a temperature increase would significantly reduce the CH 4 yield due to thermodynamic constraints and therefore reduce the overall efficiency. An industrial CO 2 methanation reactor, for example, that is designed for 10 bara (1 bara = 100 kPa) and 340 C with a total inlet flow rate of 5000 m 3 N Á h −1 (H 2 /CO 2 = 4) can be operated at a turndown ratio of 0.5 (2500 m 3 N Á h −1) at the same temperature and the same u 0 /u mf ratio by reducing the pressure to 5 bara with only a slight decrease in the CO 2 equilibrium conversion from 96.7% to 94.6%.

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Direct catalytic methanation of biogas – Part II: Techno-economic process assessment and feasibility reflections

Cited by 50 publications

References 11 publications

Life cycle assessment of power-to-gas with biogas as the carbon source

Life cycle assessment of power-to-gas with biogas as the carbon source

CO₂ Methanation in Microstructured Reactors – Catalyst Development and Process Design

Working diagrams to identify the operating range of a bubbling fluidized bed reactor for the CO₂ methanation

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Direct catalytic methanation of biogas – Part II: Techno-economic process assessment and feasibility reflections

Cited by 50 publications

References 11 publications

Life cycle assessment of power-to-gas with biogas as the carbon source

Life cycle assessment of power-to-gas with biogas as the carbon source

CO2 Methanation in Microstructured Reactors – Catalyst Development and Process Design

Working diagrams to identify the operating range of a bubbling fluidized bed reactor for the CO2 methanation

Contact Info

Product

Resources

About

CO₂ Methanation in Microstructured Reactors – Catalyst Development and Process Design

Working diagrams to identify the operating range of a bubbling fluidized bed reactor for the CO₂ methanation