Oxy-combustion Conditions Research Articles

The structure of swirl-stabilized turbulent premixed CH4/air and CH4/O2/CO2 flames and mechanisms of intense burning of oxy-flames

The objective of this work is to examine the structure of lean turbulent premixed CH4/air (air-flames) and CH4/O2/CO2 (oxy-flames) in a swirl-stabilized combustor at the large (macro) and small (micro) scales, and to explain why the latter burns more intensely despite its lower laminar burning velocity. Measurements of the instantaneous flame front and flow field using OH-PLIF and PIV, respectively, are analyzed. The CO2 dilution in the oxy-flame was adjusted to achieve the same adiabatic temperature for both flames while keeping the equivalence ratio (=0.65) and Reynolds number (=20,000) the same. Results show that at the large scale, the overall length of the oxy-flame is notably shorter than that of the air-flame. We use a strained flame model with detailed kinetics to show that the strained consumption speed of oxy-flames is lower than that of air-flames, mainly due to the chemical role of CO2, and hence laminar flame properties cannot explain the difference between the two flames in the turbulent case. Instead, the turbulent dynamics properties such as the small scale wrinkling of the flame, its surface area density and radius of curvature are obtained from the data and used to explain the observed trends. Measurements show that the flame surface area density of oxy-flames is higher because more flame segments with smaller radius of curvature appear. This is particularly noticeable downstream, and is consistent with the Lewis number effects, i.e., the response for the flame to thermo-diffusive instability. The local average burning intensity, being high under oxy-combustion conditions, explain the shorter overall average flame length.

Effect of co-firing on emissions and deposition during fluidized bed oxy-combustion

The relevance of coal oxy-firing in fluidized bed reactors has increased during the last years as an alternative for the development of CO2 capture technologies. The addition of biomass in the fuel blend is well-known in conventional combustion, but few experiences are found under oxy-combustion conditions. This paper discusses the results obtained when oxy-firing anthracite and corn stover in a lab-scale fluidized bed, paying attention to pollutant emissions, deposition rates and composition of the ashes. While SO2 emissions are affected by the chlorine content supplied with the biomass, NOx are much more dependent on operating conditions in a similar way to conventional combustion. As concerns the ash composition, chlorine is detected in fly ashes while the bed solids are mostly composed by aluminosilicates. Oxy-firing increases the chlorine detected in fly ashes in comparison to the air-fired tests. Deposition rates are barely modified by the O2/CO2 atmosphere; severe deposition is only detected for the blend with the highest chlorine content. Mixed Ca-K sulfates are found in deposits, minimizing the risk of chlorine-induced corrosion.

Curtailing the generation of sulfur dioxide and nitrogen oxide emissions by blending and oxy-combustion of coals

This research examined the reduction of combustion-generated sulfur dioxide and nitrogen oxide emissions from a pulverized high-sulfur bituminous coal by co-firing it with a lignite coal and by substituting air with O2/CO2 gases, of compositions pertinent to dry once through oxy-fuel combustion conditions. Oxygen mole fractions were in the range of 21–30%. The neat bituminous and lignite coals as well as a 50–50wt% blend thereof were burned in a laboratory-scale electrically-heated drop-tube furnace under fuel-lean conditions. Coal particles were in the size range of 75–90μm and the furnace was operated at 1400K. Results showed that the SO2 emissions from the lignite coal were drastically lower than those from the bituminous coal, whereas the NOx emissions were only mildly lower. Co-firing the high-sulfur bituminous coal and the low-sulfur lignite coal reduced the SO2 emissions, under both air and oxy-combustion conditions, to values well-below those predicted by linear interpolation of the respective emissions of the two neat coals. This observation, in conjunction with ash analysis shows that the alkali-rich ashes of the lignite coal acted as sulfur sorbents for the copious SO2 emissions of the bituminous coal. This behavior was contrasted to SO2 sorption when the bituminous coal was co-injected with calcium- and sodium-based sorbents at analogous alkali to sulfur ratios. Co-firing of the coals reduced the NOx emissions only mildly, whereas the substitution of the background N2 gas with CO2 resulted in much more extensive NOx reductions.

Enrichment of trace elements in bottom ash from coal oxy-combustion: Effect of coal types

In this study, the enrichment of trace elements in two coals under air and oxy-combustion conditions was studied. Twenty-one trace elements were evaluated. The two coal samples had a different concentration for the 21 trace elements, which was due to differences in the maceral composition. Based on the Relative Enrichment (RE) values calculated for the 21 trace elements in this study, 16 of them are non-volatile and the rest (5) are semi-volatile and volatile elements. The non-volatile elements are Li, Cr, V, Mn, Sr, Ba, Cu, Rb, Co, Ni, Ga, Pb, Be, Mo and U. The semi volatile and volatile elements are Ag, Cd, Te, Bi and Ti.In air combustion, only 9 of the 16 non-volatile trace elements have the same enrichment behaviour in the two coals when the temperature was increased from 900°C to 1000°C. The 9 trace elements are Cr, Mn, Cu, Co, Ni, Mo, V, Zn and Pb. In oxy combustion, only 5 of the 16 non-volatile trace elements and they are Cr, Sr, Rb, Ni and Mo. Only 3 of the 16 non-volatile trace elements have the same enrichment behaviour under both air and oxy-combustion conditions. The three elements were Cr, Mn and Mo.For the 5 semi-volatile and volatile trace elements, only 3 had the same enrichment behaviour in air combustion in both coal samples when the temperature was increased from 900°C to 1000°C. The three are Bi, Te and Ti. In oxy-combustion, Bi had the same enrichment behaviour when the temperature was increased from 900°C to 1000°C.The results show that the difference in the enrichment behaviour for both coal samples at different combustion temperatures is more significant under oxy-combustion conditions.

Numerical investigation of syngas oxy-combustion inside a LSCF-6428 oxygen transport membrane reactor

The present work provides an investigation of the oxy-fuel combustion of syngas (mixture of CO and H2) inside an OTR (oxygen transport reactor) of tubular shape and surrounded by air in an annulus. The syngas is generated from solar thermal reforming of methane. CFD (Computational fluid dynamics) calculations were performed using FLUENT 14.0 commercial code, where a series of UDFs (user defined functions) that enable the transfer of oxygen across the membrane were written in VC++, then compiled and hooked to FLUENT software. The models of oxygen permeation and reaction kinetics are validated against the available experimental data under similar oxy-combustion conditions. Simulations were performed considering non-reactive and reactive flow conditions. The results showed that the reactive flow results in increase in oxygen permeation flux of about four times the case of non-reactive flow. Oxy-combustion characteristics of synthetic gas in a medium of recirculated CO2 are investigated. Considering reactive flow conditions, the effects of inlet temperature, CO2 circulation, fuel composition and sweep gas flux on oxygen permeation and combustion temperature are studied. It was found that increase in inlet temperature, inlet fuel concentration, inlet hydrogen concentration and sweep flow rate result in high combustion temperature and improved oxygen permeation flux.

An overview of coal rank influence on ignition and combustion phenomena at the particle level

Individual particles of pulverized coals exhibit strikingly different combustion phenomena depending on their rank (anthracite, semi-anthracite, bituminous, sub-bituminous and lignite). Herein a concise review is presented on pertinent findings in the literature to contrast ignition and combustion behavior of such fuels at the particle-level. Emphasis is given to recent investigations performed in the laboratory of the authors, where combustion of a variety of coal particles of the same size-cut took place in the same apparatus under identical operating conditions. Such behaviors were then compared to those reported in the literature to verify their replication under often different, but yet relevant, conditions. The objective has been to relate the effect of coal rank to a number of key qualitative and quantitative parameters, such as modes of ignition and combustion, ignition temperatures, ignition delay times, combustion temperatures and burnout times (both those encountered in the volatile and the char combustion phases), volatile flame sizes as well as extents of particle fragmentation. Besides reviewing combustion behaviors in air, analogous behaviors under simulated dry oxy-combustion conditions were also highlighted. Then the coal rank dependence of the required oxygen mole fraction in dry O2/CO2 blends to match the intensity of air-fired combustion was examined.

The effect of nitrogen content in oxy-natural gas combustion on the CO concentration in premixed flame

This paper shows the report results of experimental and numerical studies of the formation of CO in the kinetic natural gas flame in oxy-combustion conditions, when the completely nitrogen-free atmosphere cannot be ensured. The aim of these studies was to determine the effect of nitrogen addition to the furnace chamber on the variations in CO concentration. The addition of nitrogen to oxy-combustion reflects the sources of nitrogen in industrial furnaces, which can be: additives used to accelerate the charge melting in glass production, inadequate oxygen purity and a leaky chamber. It has been demonstrated experimentally that by adding nitrogen to an oxidizing atmosphere composed of 27 v/v % O2 and CO2, the CO concentration in the flame region was reduced. By using the program Chemked II and the detailed combustion mechanism created by Mendiara and Glarborg, an analysis of the rate of reactions having a significant effect on the CO concentration in the flame was made, and predominant reactions responsible for the formation of CO have also been listed. It was stated that both extending the combustion product residence time and increasing the nitrogen content of the combustible mixture lead to a reduction of CO concentrations in the flame.

Is torrefaction of polysaccharides-rich biomass equivalent to carbonization of lignin-rich biomass?

Waste biomass species such as lignin-rich hazelnut shell (HS) and polysaccharides-rich sunflower seed shell (SSS) were subjected to torrefaction at 300°C and carbonization at 600°C under nitrogen. The structural variations in torrefied and carbonized biomasses were compared. Also, the burning characteristics under dry air and pure oxygen (oxy-combustion) conditions were investigated. It was concluded that the effects of carbonization on HS are almost comparable with the effects of torrefaction on SSS in terms of devolatilization and deoxygenation potentials and the increases in carbon content and the heating value. Consequently, it can be proposed that torrefaction does not provide efficient devolatilization from the lignin-rich biomass while it is relatively more efficient for polysaccharides-rich biomass. Heat-induced variations in biomass led to significant changes in the burning characteristics under both burning conditions. That is, low temperature reactivity of biomass reduced considerably and the burning shifted to higher temperatures with very high burning rates.

Mercury oxidation in catalysts used for selective reduction of NOx (SCR) in oxy-fuel combustion

Emissions of mercury (Hg) and their control are a well-known problem for conventional coal combustion power plants but they still represent a challenge for relatively new technologies such as the oxy-combustion. In oxy-fuel combustion systems it is important that Hg be in its oxidized form (Hg2+) because in the form of elemental mercury (Hg0), it can damage the CO2 compression units. In conventional air combustion some catalysts used in selective catalytic reduction (SCR) of NOx could also co-benefit Hg oxidation. This study evaluates the oxidation of Hg in the presence of several SCR catalysts under an oxy-combustion atmosphere focusing on the main differences with conventional air coal combustion. In the experimental conditions of this study, a higher mercury oxidation was observed in the CO2-enriched atmosphere due to the fact that in this atmosphere the conversion of NOx was lower, which resulted in a higher concentration of NO and NO2 free to homogeneously oxidize mercury. In oxy-combustion conditions the high amount of CO2 and H2O present may block the active sites for mercury adsorption. Moreover, the differences between the active sites of catalysts based on V/W/TiO2 and Fe/Zeolite with/without Mn as doping agent were eclipsed by the effect of the flue gas composition.

Ash formation and deposition during oxy-coal combustion in a 100 kW laboratory combustor with various flue gas recycle options

Fouling and slagging processes are important in oxy-coal combustion processes because they greatly influence heat transfer and boiler performance. Ash partitioning processes are precursors to deposition processes and so in order to predict the latter one must have a good understanding of the former. This work involves a 100kW rated down-fired oxy-fuel combustor outfitted with sophisticated ash aerosol and ash deposit sampling equipment. The work differs from that previously published, in that here we focus on the effects of changes in the composition and amounts of actual recycled flue gas (RFG) streams used in oxy-coal combustion, not using once through CO2, as before. Conditions examined here included oxy-coal combustion with three different RFG cleanup options and two different RFG amounts, and results consist of size segregated compositions of the ash aerosol and spatially resolved compositions within the deposits. In general, results suggested that oxy-combustion conditions did not cause major changes in ash partitioning, fouling and slagging. There are, however, changes in both the compositions of the ultrafine particles and in that of the inner layer of the deposits, and these were due to higher flame temperatures, when these occurred. These results are discussed and interpreted in detail.

A generalized model of SO2 emissions from large- and small-scale CFB boilers by artificial neural network approach Part 2. SO2 emissions from large- and pilot-scale CFB boilers in O2/N2, O2/CO2 and O2/RFG combustion atmospheres

Since sulfur release and capture processes during solid fuel combustion in circulating fluidized bed (CFB), especially in oxy-fuel conditions are very complex, the development of a simple SO2 emissions model for a wide range of operating conditions both for large- and pilot-scale boilers is of practical significance.Previously established and validated [16-1-6-1] ANN model, which was published in the Part 1 of this paper was employed to predict SO2 emissions from coal combustion in a large-scale 261 MWe CFB COMPACT-type boiler as well as in a pilot-scale 0.1 MWth OxyFuel–CFB test rig.The simulations are carried out using artificial neural network approach for different combustion environments, both in atmospheric and pressurized conditions. The study is conducted for air-firing, oxygen-enriched and oxy-fired combustion conditions. Therefore, four different combustion atmospheres are considered in the paper, where combustion runs in air and air enriched with oxygen (O2/N2 mode) as well as in oxycombustion (oxygen-fired combustion) conditions, which mean the mixture of oxygen with CO2 or recycled flue gas (RFG) with various fractions of oxygen (O2/CO2 mode and O2/RFG mode, respectively).The obtained results show that the ANN model makes it possible to predict the SO2 emissions from coal combustion in CFB boilers of different sizes and in different combustion environments.

A generalized model of SO2 emissions from large- and small-scale CFB boilers by artificial neural network approach: Part 1. The mathematical model of SO2 emissions in air-firing, oxygen-enriched and oxycombustion CFB conditions

Since the complexity of sulfur capture and release during solid fuel combustion in circulating fluidized bed (CFB) boilers, especially in the oxycombustion conditions is still not sufficiently recognized, the development of a simple SO2 emission model for wide range of operating conditions is of practical significance.The paper introduces the artificial neural network (ANN) approach for the prediction of SO2 emissions from CFB boilers. The model considers a wide range of parameters influencing SO2 emissions. The [16-1-6-1] ANN model was successfully applied to predict SO2 emissions from coal combustion in several large- and small-scale CFB boilers, over a wide range of operating conditions, both in air-firing as well as oxygen-enriched and oxycombustion conditions.Since the method constitutes a quick and easy to run technique this approach makes a complementary tool in relation to the experimental procedures and the programmed computing approach. Therefore, the model can be easily applied by scientists and engineers for simulations and optimizations of CFB units.

Soot loading, temperature and size of single coal particle envelope flames in conventional- and oxy-combustion conditions (O2/N2 and O2/CO2)

A fundamental laboratory study on the volatile-phase combustion of pulverized coal was conducted at the particle level. A primary goal has been to simultaneously assess soot volume fraction, fv, and soot temperature, T, in the diffusion flame (soot mantle) forming around a single burning bituminous coal particle, upon ignition of its volatile matter. This assessment was conducted with emission-based pyrometric methods. A secondary goal of this study has been to compare these radiative parameters, fv and T, in conventional air- and in simulated dry oxy-fuel combustion. Both fv, and T measurements were spatially averaged in the flame but temporally resolved throughout the combustion history of single particles. In addition, the size of the volatile envelope flames was assessed both pyrometrically and cinematographically. Combustion of three different bituminous coals took place with various oxygen partial pressures in nitrogen and in carbon dioxide background gases. Single particles, 75–90μm, were injected and burned in a transparent drop-tube furnace (DTF) at laminar-flow atmospheric-pressure and a wall temperature of 1400K. The free-falling bituminous coal particles heated up and devolatilized, their volatile matter ignited and formed bright envelope flames, often with distinctive soot contrails in the wakes of the flames. The radiative parameters fv, T and flame size, of these luminous envelope flames were assessed using different emission-based models for the analysis of the three-color pyrometric intensities. The particle envelope flames of all three coals were found to contain comparable to each other soot volume fractions, in the range of 20–90ppm. At identical furnace gas temperatures and identical O2 mole fractions, when the background N2 gas was replaced with CO2, the particle envelope flames of the bituminous coals were characterized by lower soot volume fractions, lower temperatures and bigger sizes. As the O2 mole fraction increased in either N2 or CO2 background gases, soot volume fractions increased to a maximum and then decreased, temperatures increased monotonically and flame sizes decreased. In CO2-based combustion, an oxygen mole fraction in the neighborhood of 35% was necessary to elevate the measured flame temperature to match that of conventional air-based combustion; however, the soot volume fraction was lower than that in air-based combustion regardless of the oxygen mole fraction.

Conversion of sulfur and nitrogen to gaseous components from sewage sludge combustion under oxy-firing conditions

The article presents the results of sulfur and nitrogen conversion to flue gas components during the oxy-combustion of municipal sewage sludge. In Poland, some dynamic changes in the implementation of thermal treatment methods in sewage sludge management have been observed over recent years. A few new installations have been commissioned with a fluidized bed technology under air-firing conditions. Until 30th December 2012, there were in Poland, 11 municipal sewage sludge incineration plants that had jointly a total capacity amounting to 160,000 Mg/y. Since the oxy-combustion technology has been researched widely mainly in coal combustion, the experiments carried out at 0.1 MWth CFB combustor have focused on sewage sludge combustion and sulfur, nitrogen conversion to flue gas components in the conditions of increased oxygen concentration and different process temperatures. The oxygen concentration in a feed gas was increased from 21 to 35% per volume. An increase in sulfur and nitrogen conversion ratios was found under the oxy-combustion conditions.

Thermo-oxidation characteristics of oil shale and oil shale char under oxy-fuel combustion conditions

The current research involves characteristics of pyrolysis and thermo-oxidation of Estonian oil shale (OS) and its char. Non-isothermal and isothermal thermal analysis methods were used to characterise and compare the specifics of these processes under air and oxy-combustion conditions using Ar, CO2, O2 and their mixtures. The study of reaction kinetics including pyrolysis and oxidation characteristics is crucial to understand the complex mechanism of OS oxy-fuel combustion. The experimental results showed that the pyrolysis behaviour is highly similar in Ar and CO2 until the end of decomposition of organic part. There is no visible char carbon and CO2 reaction during the char oxidation stage under oxy-fuel conditions. The release of CO related to the char carbon and CO2 reaction in 100 % CO2 atmosphere increases notably at temperatures above 650–700 °C. The role of inorganic minerals in the oxidation and gasification of char was described as well as the effect of oxy-fuel conditions on gaseous emissions. It was found that the rate constants for char oxidation in CO2/O2 are approximately 1.2–1.3 times higher as compared to Ar/O2 atmosphere and that char oxidation under oxy-fuel conditions takes place with lower activation energies as compared to Ar/O2.

Direct Numerical Simulation of combustion near a carbonaceous surface in a quiescent flow

In this work, unsteady gasification and oxidation of carbonaceous materials with gas-phase combustion under oxy-combustion conditions is studied. An original analytical solution is derived to validate the numerical species boundary condition for the heterogeneous surface reactions with frozen gas-phase. Direct Numerical Simulations accounting for multi-species diffusion and detailed chemistry with both species and energy boundary conditions taking into account the Stefan flux were subsequently performed to study combustion near a carbonaceous wall. Transition from gasification to solid carbon oxidation and gas-phase ignition is evidenced. The competition between homogeneous and heterogeneous reactions is discussed based on the analysis of the time-dependent surface and gas-phase species consumption and production rates. Transient histories of surface species as well as spatial profiles of gas-phase species, heat release and temperature are presented for two identified structures of gas-phase CO/O2 reaction zone. In order to quantify the error induced by the Hirschfelder &Curtiss approximation for the multi-species diffusion and to evaluate the importance of the Dufour and Soret terms, a library dedicated to the computation of complex diffusion phenomena has been used to rebuild a priori, species and Soret fluxes for mass diffusion as well as Fourier, species and Dufour diffusion heat fluxes. Eventually, characteristic times of gas and surface reactions and those corresponding to the switch between the two structures of the gas-phase reaction zone are obtained over a wide range of initial O2/CO2 concentrations.

Evaluation of the potential of retrofitting a coal power plant to oxy-firing using CFD and process co-simulation

A new approach has been developed in order to estimate the potential of retrofitting an existing power plant to oxy-firing and the safe operation regime of the retrofitted boiler under oxy-combustion condition has been determined. Computational Fluid Dynamics (CFD) techniques have been employed to simulate the coal combustion and heat transfer to the furnace water walls and heat exchangers under air-firing and oxy-firing conditions. A set of reduced order models (ROM) has been developed to link the CFD predictions to the whole plant process model in order to simulate the performance of the power plant under different load and oxygen enrichment conditions in an efficient manner. Simulation results of a 500° MWe power plant unit indicate that it is possible to retrofit it to oxy-firing without affecting its overall performance. Further, the feasible range of oxygen enrichment for different power loads is identified to be between 25% and 27%. However, the peak temperature on the superheater platen 2 may increase in the oxy-coal mode at a high power load beyond 450° MWe.

Geometrical parameter evaluation of a 0.5 MWth bench-scale oxy-combustion burner

Carbon capture and storage (CCS) technologies are one of the most relevant energy pathways to mitigate medium-term climate change effects. They will contribute up to 20% of the total CO2 emission reduction by 2035. Oxy-combustion is considered a promising CCS technology applicable in fossil-fuel power plants. Much effort has been made to develop oxy-combustion at large scale. However, there are still fundamental issues and technological challenges that must be addressed before this technology can be considered for commercialization. Recent research on coal oxy-combustion experimental facilities indicates stabilization problems and ignition delays when combustion occurs in CO2-rich environments. Advanced burner designs are required to ensure technological and economic feasibility of the process. Computational Fluid-Dynamics tools were used to evaluate the behaviour of a 0.5MWth bench-scale oxy-burner. Key geometrical parameters were analysed, such as combustion chamber diameter, chamber length and angle of the quarl. Simulations showed that a length of 6m ensures complete coal combustion. The results indicated that the combustion chamber diameter and the quarl angle have an influence on coal ignition, stability, flame shape and CO concentration. Higher values of those parameters produced greater hot recycled flow, which means higher temperatures and greater flame stability. Coal ignition was also improved. A 1500-mm chamber diameter and a 50° quarl angle were selected as optimal values for both parameters. CFD modelling makes it possible to analyse the behaviour of different oxy-burner configurations and to optimize the combustion process under oxy-combustion conditions.

Devolatilization of a single fuel particle in a fluidized bed under oxy-combustion conditions. Part A: Experimental results

Devolatilization of a single fuel particle and the related flame combustion were studied in a two-dimensional fluidized bed with a quartz wall, allowing visual observation of the conversion process. The aim was to evaluate the devolatilization behavior (ignition, flame temperature, flame life-time, devolatilization time) of different fuels (4 ranks of coal from lignite to anthracite and wood) when replacing O2/N2 by O2/CO2 in O2 volume concentrations from 0% to 40%, at a fixed bed temperature of 1088K using 6mm spherical fuel particles. The volatiles’ flame was recorded by a color video camera to analyze ignition and extinction. The flame temperature was estimated by two-color pyrometry. Two thermocouples were inserted in the fuel particle to measure the temperature at the center and near the surface. Homogeneous and heterogeneous ignition modes, times of devolatilization, and flame duration (flame-life) under different gas atmospheres were analyzed. Results indicate that the mode of ignition of bituminous coal, lignite coal and wood changes when N2 is replaced by CO2. The ignition-delay time is much longer, and the flame temperature is lower in the O2/CO2 atmosphere than in an O2/N2 atmosphere for all the tested fuels. The devolatilization time of the anthracite particle is almost unaffected by the surrounding atmosphere, while for the other fuels this time is generally longer in O2/CO2 than in O2/N2 at the same O2 concentration. The presence of a flame during the volatiles combustion did not accelerate the particle heating, not even at the highest O2 concentration tested (40vol%), however, after the extinction of the flame, the rate of particle heating is significantly affected by the oxygen concentration.

Oxygen Permeation Improvement under CO2‐Rich Environments through Catalytic Activation of Hierarchically Structured Perovskite Membranes

AbstractCatalytic activation of a highly porous La0.6Sr0.4Co0.2Fe0.8O3−δ (LSCF) freeze‐cast asymmetric membrane has been realized by screen‐printing a 30 μm thick LSCF porous layer over the dense top layer of the asymmetric membrane. Membrane activation leads to a noticeable improvement of the oxygen permeation flux (JO2) in the low‐temperature region (<700 °C), at which catalytic gas exchange is the most limiting process. An enhancement of 54 % in JO2 is obtained (JO2=0.17 mL min−1 cm−2) in air at 600 °C thanks to the addition of the LSCF catalytic porous layer, whereas the maximum oxygen permeation is reached when pure oxygen is fed to the membrane at 1000 °C with a high value of 16.3 mL min−1 cm−2. The most appealing effect of the catalytic layer is its protective feature under oxycombustion conditions, that is, under a CO2‐rich atmosphere at high temperature. Indeed, the oxygen permeation drop in the presence of CO2 is significantly lower in the presence of a catalytic porous layer. Interestingly, the full recovery of JO2 flux after CO2 removal in the sweep flux evidences the absence of a carbonation process. Finally, the stability of the functionalized membrane was evaluated at 850 °C and under a 50 % CO2‐containing atmosphere; this revealed a linear degradation rate for oxygen permeation of 4.27×10−2 mL min−1 cm−2 per day.