Effects Of Reaction Temperature Research Articles

Propanol isomers: Investigation of ignition and pyrolysis time scales

This study presents an investigation of the ignition and pyrolysis kinetics of the two propanol isomers. Experiments are carried out behind reflected shock waves at average pressures of 3.5, 5.0, and 11 atm over a temperature range of 1150–1550 K. Oxidation experiments are carried out using mixtures with equivalence ratios of 0.5, 1.0, and 2.0. Laser absorption measurement of CO is carried out near 4.6 µm on the basis of which a characteristic pyrolysis time scale is defined. By means of this pyrolysis time scale, the effects of reactor temperature, pressure, and fuel concentration on pyrolysis are established. Contrast is further made between the global kinetics of pyrolysis and purely oxidative kinetics during ignition. The measured ignition and pyrolysis time scales are also compared with predictions of three chemical kinetic models from the literature. The expected lower reactivity of iso-propanol relative to n-propanol during ignition and pyrolysis is observed. The study also reveals a distinctly higher global temperature sensitivity of the pyrolysis process (global activation energy > 60 kcal/mol) compared to the typical global activation energy of ignition (global activation energy in the range of 20–40 kcal/mol). This difference leads to a cross-over effect at a characteristic reactor temperature between ignition that is controlled by pyrolysis and one that is controlled by predominantly oxidative kinetics. While this is observed for the chosen molecular systems, the cross-over effect is a general feature of high-temperature fuel reaction kinetics. At lower temperatures the chemical time scales of predominantly pyrolytic reactions are much longer than the time scales of oxidative radical processes which dominate the ignition process whereas at higher temperatures the time scales of pyrolytic processes become shorter and dominate the global ignition kinetics. Selected CO concentration profiles obtained during pyrolysis are also compared with predictions of current chemical kinetic models, revealing varying degrees of agreement and discrepancies among the models. The study advances characterization of propanol combustion and demonstrates the use of global chemical time scales to characterize fuel pyrolysis kinetics.

Practical achievements on biomass steam gasification in a rotary tubular coiled-downdraft reactor.

Today, the impending stringent environmental norms and concerns about the depletion of fossil fuel reserves have added impetus on development of cutting edge technologies for production of alternative fuels from renewable sources, like biomass. The concept of biomass pyro-gasification offers a platform for production of (a) hydrogen, (b) hydrocarbons and (c) value added chemicals, etc. In this context, there exists potential for hydrogen production from biomass by superheated steam gasification. Apart from H2, gaseous products of biomass steam gasification contain CO, CH4 and other hydrocarbons that can be converted to hydrogen through cracking, steam reforming and water gas shift reactions. In the present work, the characteristics of biomass steam gasification in an indigenously designed rotary tubular coiled-downdraft reactor for high value gaseous fuel production from rice husk was studied through a series of experiments. The robust reactor system enhances biomass conversion to gaseous products by improved mass and heat transfer within the system induced by a coiled flow pattern with increased heat transfer area. Also, the system has improved upon the reliability of operation and offered greater continuity of the process and easier control in comparison with a conventional process by making use of an innovative gas cooler assembly and efficient venturi-mixing system for biomass and steam. Subsequently, the effects of reactor temperature, steam-to-biomass ratio and residence time on overall product gas yield and hydrogen yield were investigated. From the experimental results, it can be deduced that an optimum reactor temperature of 750 °C, steam-to-biomass ratio of 2.0 and a residence time of 3.0 min contributed highest gas yield (1.252 Nm3 kg-1 moisture-free biomass). Based on the obtained experimental results, a projected potential hydrogen yield of 8.6 wt% of the moisture-free biomass could be achieved, and is also practical for production of pure hydrogen.

Practical Achievements on Biomass Steam Gasification in a Rotary Tubular Coiled-downdraft Reactor

Today, the impending stringent environmental norms and concerns about the depletion of fossil fuel reserves, have added impetus on development of cutting edge technologies for production of alternative fuels from renewable source, like biomass. Concept of biomass pyro-gasification offers platform for production a) of hydrogen b) hydrocarbons and c) value added chemicals etc. However, majority of these developments are either in nascent or in pilot/demonstration stage. In this context, there exists potential for hydrogen production from the raw gas of biomass steam gasification. In gaseous products of biomass steam gasification, there exist a lot of CO, CH4 and other hydrocarbons that can be converted to hydrogen through cracking, steam reforming and water gas shift reactions. In the present work, the characteristics of biomass steam gasification in an in-house designed rotary tubular coiled-downdraft reactor for high value gaseous fuel production from rice husk was studied through a series of experiments. The effects of reactor temperature, steam-to-biomass ratio and residence time on overall product gas yield and hydrogen yield were investigated. From the experimental results, it can be deduced that an optimum reactor temperature of 750oC, steam-to-biomass ratio (S/B) of 2.0 and a residence time (3.6min.) contributed highest gas yield (1.252 Nm3/kg-ash and moisture free biomass). Based on the obtained experimental results, a projected hydrogen purity of above 65 volume% at a potential hydrogen yield of 18.36 wt% of the biomass organic content is foreseen. Despite the fact that, the yield of hydrogen varies from biomass to biomass which depends on inherent composition of the species, this process opens up pathway for production of the cleanest fuel as compared to other liquid products from biomass, which require further treatments for making in final form.

유리생산공정 폐주석산화물에서 건식제련에 의한 주석회수기술

Abstract Most of the domestic need for tin rely on imports. In this work, a pyrometallurgical process was investigated to recover puretin from the tin oxides in tin bath which results from the production of flat glass and LCD panel. From the results on the effectof reaction temperature, the highest recovery percentage of tin was obtained at 1350 o C. The recovery percentage of tin wasimproved to 88% by employing the first and second smelting step. Electrorefining of the crude tin thus obtained led to pure tinwith purity higher than 99.9%. Key words : Tin oxide, Pyrometallurgy, Tin, Electrorefining, Recovery percentage 1. 서 론 주석은 유리공업, 전기전자 및 철강 산업 등에서 사용되고 있는 전략적인 위치를 차지하는 금속으로 용도가 1)급격히 늘어나고 있다. 국내주석 수요는 전량 수입에 의존하고 있으며, 국내에서 주석함량이 50% 이상인 · Received : December 19, 2014 · Revised : January 9, 2015 · Accepted : January 20, 2015Corresponding Author : Man-Seung Lee (E-mail : mslee@mokpo.ac.kr)Department of Advanced Materials Science & Engineering, Mokpo National University, 61 Dorim-ri, Chungkye-myun, Muan-gun, Chonnam, 534-729, KoreaTel : +82-62-450-2492 / Fax : +82-62-450-2498ⓒThe Korean Institute of Resources Recycling. All rights reserved. This is an open-access article distributed under the termsof the Creative Commons Attribution Non-Commercial License (http://creativecommons.org/licenses/by-nc/3.0/), which permitsunrestricted non-commercial use, distribution and reproduction in any medium, provided the original work is properly cited.

Biofuels Produced from Hydrothermal Liquefaction of Rice Husk

This research is conducted for getting and examining bio-fuel from the process of hydrothermal liquefaction (HTL) using rice husk as raw material. The HTL process used ethanol as a solvent with concentration of 96%. Properties of the produced light fuels were examined on parameter such as water content, viscosity, calorific value, density, flash point, and gas chromatography-mass spectroscopy (GC-MS). The optimum yield 36.3 wt% of light fuel from HTL process of rice husk occurred at reactor temperature of 325°C and holding time of 45 minutes. Meanwhile, the optimum production of bio-fuel (light fuel + heavy fuel) was 69.3 wt% at reactor temperature of 325 °C and holding time of 30 minutes. The resulted light fuel has the calorivic value from 12.1 to 20.2 MJ/kg, viscosity from 1.11 to 1.6 cSt, and flash point from 14 to 29 °C. For the yield of bio-fuel from HTL process, the effect of reactor temperature was more pronounced than the effect of holding time. Further, the light fuels from HTL process with low water content are interesting objects as a fuel in internal combustion engines.

Characterization of natural copper ore as oxygen carrier in chemical-looping with oxygen uncoupling of anthracite

Chemical-looping with oxygen uncoupling (CLOU) provides a novel route for CO2 capture with low energy penalty. In this paper, natural copper ore, known for its low cost and abundant supply, was examined as an oxygen carrier material for CLOU in a batch fluidized-bed reactor. The relations between oxygen release/uptake rates and reactor temperatures were first explored. It was found as a general trend that both the oxygen release and uptake rates increase with the reactor temperature. The CLOU thermo-chemical characteristics were further investigated comprehensively using a typical Chinese anthracite (GaoPing coal) as fuel. The effects of reactor temperature, superficial fluidization velocity, oxygen carrier to fuel ratio, coal particle size, and steam content in fluidization gas on carbon conversion rate, coal combustion efficiency, and gas yields were investigated. It was found that the following factors would lead to a higher carbon conversion rate: a higher reactor temperature, smaller superficial fluidization velocity, smaller coal particle size, larger ratio of oxygen carrier to fuel, and higher steam volume concentration in the fluidization gas. High combustion efficiency above 96% and CO2 yield above 0.95 were attained in these tests. The copper ore particles showed only slight agglomeration and sintering in the long-term operation.

Kinetic model of carbon nanotube production from carbon dioxide in a floating catalytic chemical vapour deposition reactor

The production of carbon nanostructures, including carbon nanotubes (CNTs), by chemical vapour deposition (CVD) occurs by thermally induced decomposition of carbon-containing precursors. The decomposition of the feedstock leading to intermediate reaction products is an important step, but rarely incorporated in rate equations, since it is generally assumed that carbon diffusion through or over the catalyst nanoparticles is the rate-limiting step in the production of CNTs. Furthermore, there is no kinetic model to date for the production of CNTs from carbon dioxide. These aspects are addressed in this study with the aid of a series of experiments conducted in a floating catalytic CVD reactor in which the effects of reactor temperature, concentration and flow rate of CO2 were investigated. A simple rate equation for the reductive adsorption of CO2 onto the catalyst surface followed by carbon diffusion leading to the production of CNTs is proposed as follows: d[CNT]/dt = K[CO2], where K is proportional to the diffusion coefficient of carbon. The derived kinetic model is used to calculate the amount of CNTs for a given concentration of CO2, and the experimentally measured data fits the simple rate equation very well at low carbon dioxide concentration.

Gasification of Raw and Torrefied Cotton Gin Wastes in an Auger System

Abstract. A 10 kW thermal externally heated auger gasification reactor was constructed and tested in the Rice Research and Extension Center, University of Arkansas, Stuttgart, Arkansas. The reactor was used to achieve thermal decomposition of cotton gin wastes (CGW) into producer gas and biochar. Raw and torrefied CGW were gasified to assess the effects of the torrefaction process on the producer gas composition and yield. The effects of reactor temperature (750°C, 850°C, and 950°C) and cotton wastes pretreatment (raw and torrefied) on the producer gas, biochar and condensable liquids quality and quantity were investigated. Torrefying cotton gin wastes reduced their moisture content and volatile solids by 39.0% and 6.7%, respectively whereas it increased their bulk density, heating value and stoichiometric air required for complete combustion from 390 to 426 kg m -3 , from 16.6 to 17.2 MJ kg -1 and from 4.28 to 4.74 kg kg -1 CGW , respectively. Increasing the reactor temperature resulted in an increase in the producer gas production rate and a decrease in char production rate. The maximum gas production rate reached 31 L min -1 at STP (standard temperature and pressure) during gasification of raw CGW at reactor temperature of 950°C. At the reactor temperature of 950°C, the biochar production rate decreased by 21% and 10% during gasification of raw and torrefied CGW, respectively as compared to those at the reactor temperature of 750°C. Gasification of torrefied CGW produced biochar with lower moisture content (46.3%), volatile solids (48.4%), fixed carbon (2.9%), and higher heating value (7.8%) as compared to those from gasification of raw CGW. The maximum higher heating value of gas reached 5.4 MJ m -3 from torrefied CGW. The values of the cold gas efficiency and carbon conversion did not exceed 43.0% and 55.3%, respectively. The potential green electricity generation from raw and torrefied CGW during the ginning season (1500 h) would be about 5.0 MWe and 4.7 MWe, respectively, based on a 40 bale per hour ginning facility.

Downdraft Gasification of Oil Palm Frond: Effects of Temperature and Operation Time

The last years saw a sharp increment in the interest laid on the renewable and the alternative energy sector, mainly due to the depletion of fossil fuel throughout the world for industrial and commercial use. Malaysia is the second largest producer of palm oil, currently holding up to 4.5 million hectares of palm oil plantation in its land. Currently produced at more than 40 million tons a year, only a small portion of Oil Palm Frond (OPF) is used as domestic animals forage and as raw material in small-scale furniture industry, while the rest is left at the plantation floor to naturally decompose. This study introduces OPF as a solid biomass fuel for gasification to produce synthesis gas that can be utilized for heat and energy generation in a cleaner and more efficient manner than direct combustion. OPF was gasified in the downdraft gasifier at 700-1000°C reactor temperature with a controlled air supply of 180 to 200 L min-1. The effects of reactor temperature and operation time to the quality of syngas produced from OPF downdraft gasification were investigated. At a calorific value at around 18 MJ kg-1, OPF was found to produce synthesis gas that sustainably burnt in air with a higher heating value of around 5 MJ Nm-3. OPF was found to be optimally producing syngas with desired energy content at a reactor temperature range of 700-900°C and within the first 45 min of gasifier operation.

Downdraft Gasification of Oil Palm Frond: Effects of Temperature and Operation Time

The last years saw a sharp increment in the interest laid on the renewable and the alternative energy sector, mainly due to the depletion of fossil fuel throughout the world for industrial and commercial use. Malaysia is the second largest producer of palm oil, currently holding up to 4.5 million hectares of palm oil plantation in its land. Currently produced at more than 40 million tons a year, only a small portion of Oil Palm Frond (OPF) is used as domestic animals forage and as raw material in small-scale furniture industry, while the rest is left at the plantation floor to naturally decompose. This study introduces OPF as a solid biomass fuel for gasification to produce synthesis gas that can be utilized for heat and energy generation in a cleaner and more efficient manner than direct combustion. OPF was gasified in the downdraft gasifier at 700-1000°C reactor temperature with a controlled air supply of 180 to 200 L min-1. The effects of reactor temperature and operation time to the quality of syngas produced from OPF downdraft gasification were investigated. At a calorific value at around 18 MJ kg-1, OPF was found to produce synthesis gas that sustainably burnt in air with a higher heating value of around 5 MJ Nm-3. OPF was found to be optimally producing syngas with desired energy content at a reactor temperature range of 700-900°C and within the first 45 min of gasifier operation.

Decomposition of trifluoromethane in a dielectric barrier discharge non-thermal plasma reactor

The decomposition of trifluoromethane (CHF3) was carried out using non-thermal plasma generated in a dielectric barrier discharge (DBD) reactor. The effects of reactor temperature, electric power, initial concentration and oxygen content were examined. The DBD reactor was able to completely destroy CHF3 with alumina beads as a packing material. The decomposition efficiency increased with increasing electric power and reactor temperature. The destruction of CHF3 gradually increased with the addition of O2 up to 2%, but further increase in the oxygen content led to a decrease in the decomposition efficiency. The degradation pathways were explained with the identified by-products. The main by-products from CHF3 were found to be COF2, CF4, CO2 and CO although the COF2 and CF4 disappeared when the plasma were combined with alumina catalyst.

Characteristics of hydrogen-rich gas production of biomass gasification with porous ceramic reforming

In the present study, an updraft biomass gasifier combined with a porous ceramic reformer was used to carry out the gasification reforming experiments for hydrogen-rich gas production. The effects of reactor temperature, equivalence ratio (ER) and gasifying agents on the gas yields were investigated. The results indicated that the ratio of CO/CO2 presented a clear increasing trend, and hydrogen yield increased from 33.17 to 44.26gH2/kg biomass with the reactor temperature increase, The H2 concentration of production gas in oxygen gasification (oxygen as gasifying agent) was much higher than that in air gasification (air as gasifying agent). The ER values at maximum gas yield were found at ER=0.22 in air gasification and at 0.05 in oxygen gasification, respectively. The hydrogen yields in air and oxygen gasification varied in the range of 25.05–29.58 and 25.68–51.29gH2/kg biomass, respectively. Isothermal standard reduced time plots (RTPs) were employed to determine the best-fit kinetic model of large weight biomass air gasification isothermal thermogravimetric, and the relevant kinetic parameters corresponding to the air gasification were evaluated by isothermal kinetic analysis.

Energy recovery from pyrolysis and gasification of mangrove

Mangrove is a biomass material that grows in wetland sea waters and is often used to produce charcoal due to its unique characteristics of long and sustained burning and negligible residue. High temperature pyrolysis has been conducted for mangrove biomass in a laboratory scale semi-batch reactor. The effect of reactor temperature on syngas yield and syngas characteristics has been investigated. Reactor temperature was varied from 600 to 900 °C in 100 °C intervals. The increase in reactor temperature resulted in increased syngas yield, hydrogen yield and energy yield. Evolutionary behavior of the syngas characteristics has also been investigated. The increase in reactor temperature increased the peak value of syngas flow rate, hydrogen flow rate and output power. The increase in reactor temperature decreased the time duration of pyrolysis. Cumulative yield of syngas, hydrogen and energy was calculated based on the time dependent relationship. Higher reactor temperatures shortened the time duration required for 99% release of syngas, hydrogen and energy. For example, time duration required for 99% yield of hydrogen was approximately 73 min at 600 °C and only about 26 min at 900 °C. Required time duration for 99% yield of energy was ∼62 min at 600 °C and ∼15 min at 900 °C. The gasification of the same material at 900 °C has been carried out to determine the role of gasifying agent on the fate of material and resulting syngas properties. The results showed gasification yielded more syngas, hydrogen and energy than that obtained from pyrolysis.

Biodiesel production from acid oils and ethanol using a solid basic resin as catalyst

In the search of an alternative fuel to substitute diesel fuel, biodiesel appears as one of the most promising sources of energy for diesel engines because of its environmental advantages and also due to the evolution of the petroleum market. Refined oil is the conventional raw material for the production of this biofuel; however, its major disadvantage is the high cost of its production. Therefore, frying oils, waste oils, crude oils and/or acid oils are being tested as alternative raw materials; nevertheless, there will be some problems if a homogeneous basic catalyst (NaOH) is employed due to the high amount of free fatty acid present in the raw oil. In this work, the transesterification reaction of acid oil using solid resin, Dowex monosphere 550 A, was studied as an alternative process. Ethanol was employed to have a natural and sustainable final product. The reaction temperature's effects, the initial amount of free fatty acid, the molar ratio of alcohol/oil and the type of catalyst (homogeneous or heterogeneous) over the main reaction are analyzed and their effects compared. The results obtained show that the solid resin is an alternative catalyst to be used to produce fatty acid ethyl esters (FAEEs) by a transesterification reaction with a final conversion over 90%. On the other hand, the time required to achieve this conversion is bigger than the one required using conventional technology which employs a homogeneous basic catalyst. This reaction time needs to be optimized.

Characteristics of cardboard and paper gasification with CO 2

Evolutionary behavior of syngas chemical composition and yield have been examined for paper and cardboard at three different temperatures of 800, 900 and 1000 °C using CO 2 as the gasifying agent at constant flow rate. Specifically the evolution of syngas chemical composition with time has been investigated. Pyrolysis of the sample was dominant at the beginning of the gasification process as observed from the high initial devolatilization of the sample followed by char gasification of material to form syngas for a long period of time. Results provided the role of gasification temperature on kinetics of the CO 2 gasification process. Increase in gasification temperature provided increased conversion of the sample material to syngas. Thus the sample conversion to syngas was low at the low temperature of 800 °C while at elevated temperatures of 900 and 1000 °C substantial enhancement of the kinetics process occurred. The evolution of extensive reaction rate of carbon-monoxide was calculated. Results show that increase in temperature increased the extensive reaction rate of carbon-monoxide. The global behavior of syngas chemical composition examined at three different temperatures revealed a peak in concentration of H 2 to exhibit after few minutes into the gasification that changed with gasification temperature. At 800 °C gasification temperature peak in H 2 was displayed at 3 min into gasification while it decreased to only 2 min, approximately, at gasification temperatures of 900 and 1000 °C. The effect of reactor temperature on CO mole fraction has also been examined. Increase in the gasification temperature enhances the mole fraction of CO yields. This is attributed to the increase in forward reaction rate of the Boudouard reaction ( C + CO 2 ⇔ 2CO ). The results show important role of CO 2 gas for the gasification of wastes and low grade fuels to clean syngas.

NUMERICAL SIMULATION OF Si NANOPARTICLE FORMATION BY SILANE PYROLYSIS

This paper presents a numerical model of silicon nanoparticle formation process during silane ( SiH 4) pyrolysis. Aerosol dynamics model, which includes particle growth by surface reaction, coagulation, and transport, was coupled with a chemical kinetics model using CHEMKIN 4.1.1 with particle tracking module (PTM). The general dynamic equation (GDE) was solved by using the method of moment (MOM). The effect of reactor temperature, pressure, total flow rate, and initial silane concentration was successfully investigated under conditions typically used for atmospheric-pressure silane pyrolysis system and we compared the calculated results on particle formation with published experimental data. The simulation results show that particle formation is very sensitive to temperature and initial silane concentration. We observed that numerical simulation results showed a good agreement with experimental data for parameters such as particle concentration, diameter, growth rate, and total volume concentration.

Hydrogen-Rich Gas Production from Pyrolysis of Biomass in an Autogenerated Steam Atmosphere

Hydrogen-rich gas production from pyrolysis of biomass in an autogenerated steam atmosphere was proposed. The scheme aims to utilize steam autogenerated from biomass moisture as a reactant to react with the intermediate products of pyrolysis to produce additional hydrogen. In the present Article, the effect of reactor temperature, moisture content, heating rate, and sweeping gas flow rate on the process was investigated experimentally. Measurement of the atomic structures of chars produced from pyrolysis of wet/predried biomass was carried out with XRD. The results show that heating rate is a key role in the process. Under fast-heating conditions, drying and pyrolysis occurred in a relatively shorter time, which enhances the interactions between the autogenerated steam and the intermediate products and hence produces more hydrogen. Under slow-heating conditions, however, the autogenerated steam from moisture will be partially purged away from the reaction zone, leading to a weakened effect on the subseque...

Synthesis gas production by biomass pyrolysis: Effect of reactor temperature on product distribution

This paper describes mass, C, H, and O balances for wood chips pyrolysis experiments performed in a tubular reactor under conditions of rich H 2 gas production (700–1000 °C) and for determined solid heating rates (20–40 °C s −1). Permanent gases (H 2, CO, CH 4, CO 2, C 2H 4, C 2H 6), water, aromatic tar (10 compounds from benzene to phenanthrene and phenols), and char were considered in the balance calculations. Hydrogen (H) from dry wood is mainly converted into CH 4 (more than 30% mol. of H at 900 °C), H 2 (from 9% to 36% mol. from 700 to 1000 °C), H 2O, and C 2H 4. The molar balances showed that the important yield increase of H 2 from 800 to 1000 °C (0.10 Nm 3 kg −1 to 0.24 Nm 3 kg −1 d.a.f. wood) cannot be solely explained by the analyzed hydrocarbon compounds conversion (CH 4, C 2, aromatic tar). Possible mechanisms of H 2 production from wood pyrolysis are discussed.

Low temperature gasification of olive kernels in a 5-kW fluidized bed reactor for H 2-rich producer gas

Air gasification of olive kernels in a 5 kW bench scale, bubbling fluidized bed gasifier, aimed at H 2 enrichment of the producer gas, was the target of this study. The effects of reactor temperature ( T = 750–850 °C) and equivalence ratio (ER = 0.2–0.4), representing the under stoichiometric amount of air inserted into the reactor to that necessary for complete combustion, on producer gas quality were determined. The experimental results revealed that producer gas H 2 content increased at the temperature of T = 750 °C and ER = 0.2, resembling the high-temperature pyrolysis conditions that favour H 2 and CO production. Further increase in ER deteriorated producer gas quality, decreased H 2 content and favoured CO 2, thus lowering producer gas heating value. The data obtained from several experiments indicate that olive kernels produced a medium heating value gas (LHV = 6.54 MJ/Nm 3) at 750 °C and ER = 0.2, while H 2 and CO production were maximized at the same conditions (H 2: 24%vv, CO: 14.3%vv).

Production of hydrogen by unmixed steam reforming of methane

Unmixed steam reforming is an alternative method of catalytic steam reforming that uses separate air and fuel–steam feeds, producing a reformate high in H 2 content using a single reactor and a variety of fuels. It claims insensitivity to carbon formation and can operate autothermally. The high H 2 content is achieved by in situ N 2 separation from the air using an oxygen transfer material (OTM), and by CO 2 capture using a solid sorbent. The OTM and CO 2 sorbent are regenerated during the fuel–steam feed and the air feed, respectively, within the same reactor. This paper describes the steps taken to choose a suitable CO 2 -sorbent material for this process when using methane fuel with the help of microreactor tests, and the study of the carbonation efficiency and regeneration ability of the materials tested. Elemental balances from bench scale experiments using the best OTM in the absence of the CO 2 sorbent allow identifying the sequence of the chemical reaction mechanism. The effect of reactor temperature between 600 and 800 ∘ C on the process outputs is investigated. Temperatures of 600 and 800 ∘ C under the fuel–steam feed were each found to offer a different set of desirable outputs. Two stages during the fuel–steam feed were characterised by a different set of global reactions, an initial stage where the OTM is reduced directly by methane, and indirectly by hydrogen produced by methane thermal decomposition, in the second stage, steam reforming takes over once sufficient OTM has been reduced. The implications of these stages on the process desirable outputs such as efficiency of reactants conversion, reformate gas quality, and transient effects are discussed.