Packed-bed Membrane Reactor Research Articles

Comparative analysis of hydrogen production from ammonia decomposition in membrane and packed bed reactors using diluted NH3 streams

Ammonia decomposition is a key technology for its use as a hydrogen carrier and in the recovery of H2 from waste streams containing ammonia. The coupling of the catalytic decomposition of ammonia with an H2 permeoselective membrane improves the process by mitigating thermodynamic constraints and producing a flux of high-purity hydrogen, not requiring further separation/purification. In this study, we compare the behaviour of an eggshell catalyst 1.3 wt % Ru/Al2O3 catalyst in a packed bed reactor (PBR) and a packed bed membrane reactor (PBMR) using an ultrathin Pd membrane (3.4 μm). Tests were made at 11 bar(a) with a weight hourly space velocity of NH3 in the 0.560–1.68 Lꞏg−1ꞏh−1 range and temperatures of 350–400 °C, e.g. milder conditions than the conventional ammonia cracking catalysts. Under optimised conditions (0.56 Lꞏg−1ꞏh−1, 400 °C, sweep gas flow 0.55 L min−1), the PBMR shows excellent performance, achieving NH3 conversion, H2 productivity and recovery factor of 99%, 47 mmolH2·gRu−1·min−1, and 94.9%, respectively. PBMR increases by ∼50% the conversion rate compared to PBR. Without a sweep gas, PBMR performances are lower, even still higher than in PBR. For the first time, superior or comparable performance was demonstrated compared to similar systems using pure ammonia in terms of conversion, hydrogen recovery, H2 productivity, and Ru utilisation. These results can be further enhanced with vacuum systems to convert diluted ammonia streams into high-purity hydrogen for small-scale distributed systems and can be extended to other reactions.

Enhanced H2S decomposition using membrane reactor

H2S is a toxic gas released during many industrial processes, especially oil and gas refining. Currently, H2S is converted to sulfur using Claus process, but it leads to loss of another valuable product, i.e., hydrogen, in the form of water. Thermal decomposition of H2S in a membrane reactor is a promising route for recovering both hydrogen as well as sulfur in an efficient manner. In the present work, the authors report H2S decomposition studies with packed-bed membrane reactor (PBMR) using in-house developed clay-alumina ceramic membrane. In order to have a comparative evaluation, these studies were conducted in packed bed reactor (PBR) as well as in single-tube PBMR at different operation parameters. In PBMR, conversion of ∼90% was obtained at 1573 K and 0.5 bar, whereas a conversion of ∼50% was obtained in PBR. CFD simulations for H2S decomposition using ceramic PBMR were carried out and validated using experimental results. 3D simulations for parametric optimisation of multi-tube PBMR were also carried out by extrapolation of validated model. This is for the first time, CFD studies on H2S decomposition and its validation using ceramic PBMR are being reported in this work.

Modeling and simulation of biodiesel synthesis in fixed bed and packed bed membrane reactors using heterogeneous catalyst: a comparative study

In this study, modeling and simulation of biodiesel synthesis through transesterification of triglyceride (TG) over a heterogeneous catalyst in a packed bed membrane reactor (PBMR) was performed using a solid catalyst and compared with a fixed bed reactor (FBR). The kinetic data for the transesterification reaction of canola oil and methanol in the presence of solid tungstophosphoric acid catalyst was extracted from the published open literature. The effect of reaction temperature, feed flow rate, disproportionation of the reactants, and reactor length on the product performance was investigated. Two-dimensional and heterogeneous modeling was applied to PBMR and the resultant equations were solved by the Matlab software. Moreover, the velocity profile in the membrane reactor was obtained. The results showed the best conditions for this reaction are 180 °C, the molar ratio of methanol to oil equal 15:1, and the input flow rate of 0.5 mL/min. In this condition, a conversion of 99.94% for the TG can be achieved in the PBMR with a length of 86 cm while a length of 2.75 m is required to achieve this conversion of the FBR. Finally, the energy consumption for the production of 8000 ton/y biodiesel in a production plant using the PBMR and the FBR was obtained as is 1313.24 and 1352.44 kW, respectively.

Highly efficient and stable hydrogen permeable membrane reactor for propane dehydrogenation

The synthesis of SAPO-34 hollow fiber membranes employs the ball-milling assistant method to enhance membrane yield and quality. These membranes are then combined with CrOx/Al2O3 catalyst to create a packed bed membrane reactor (PBMR) for propane dehydrogenation (PDH). The study investigates the impact of operating temperatures, weight hourly space velocities (WHSV), and sweep gas flow rates on the SAPO-34 zeolite membrane reactor's performance, comparing it to a traditional packed bed reactor (PBR). The removal of hydrogen from the reaction side significantly improves propane conversion, surpassing thermodynamic equilibrium. In PBMR, propylene selectivity slightly exceeds that in PBR, influenced by side reactions like hydrogenolysis and cracking after hydrogen removal. Furthermore, the SAPO-34 zeolite membrane reactor undergoes a prolonged stability test with frequent regeneration using pure propane as feedstock to simulate industrial conditions. It exhibits consistent performance over 120 regeneration cycles within 240 h, maintaining similar H2 permeability and H2/C3H8 selectivity as the fresh membrane post long-term testing.

Cross-flow inducing structured catalyst for reduced concentration polarization in packed bed membrane reactors

3D printed baffled logpile structures were recently identified as promising structured catalyst geometries for intensified heat transfer in chemical reactors. In this work, the potential of these structures for intensification of the mass transfer is studied by addressing concentration polarization in membrane-assisted steam methane reforming in a packed bed membrane reactor. Through pseudo-2D OpenFOAM computational fluid dynamics simulations, the performance was assessed using the hydrogen recovery and the conversion of methane as performance indicators. The results show that the integration of baffles into the logpile structure significantly reduces the degree of concentration polarization over a range of operating conditions, thanks to the convection-driven radial mass transport. Furthermore, it was found that the cross-flow regime characteristic of the baffled logpile structures scales effectively with the reactor diameter, demonstrating potential for scalability. Combined with the demonstrated heat transfer intensification, these findings lay the foundation for value-added application of 3D printed catalyst structures.

Modeling of an ammonia decomposition membrane reactor including purity with complex geometry and non-isothermal behavior

A fully coupled mass, momentum, and heat balance model was constructed in axisymmetric 2D for an ammonia decomposition packed bed membrane reactor using computational fluid dynamics and compared to experimental results for a Pd/YSZ membrane surrounded by Ru/Al2O3 catalyst. In addition to the complex geometry of the fittings used to seal the membrane, a total of 16 design variables were found to be required to fully specify the tubular integrated membrane reactor. Aside from emissivity, all input variables were experimentally determined or obtained from tabulated material property data, and no correlation fitting was performed. Experimental data were obtained for temperatures of 450 °C–530 °C, trans-membrane pressures of 0 MPa–0.4 MPa, and gas hourly space velocity feed rates of 375 h−1 to 620 h−1, chosen such that the ammonia conversion and hydrogen recovery spanned a broad range with maximum values of 99.9 % conversion or 88 % recovery with greater than 99.8 % purity. The model was able to successfully determine the ammonia conversion and hydrogen recovery of the experimental results to within an average error of −0.31 % and −2.4 %, respectively. The purity was determined within +0.0071 %, but experimental detection limitations of the impurities affected the fit between experiment and model of the N2 and NH3 in the permeate. The sensitivity of the model to various assumptions and input variables was explored. Notably, the inclusion of purity is a rarity in published models and this study adds to the discussion on the ability of modeling to predict high purity results. Compared to the relatively minimal effects of using the full geometry, the inclusion of heat transfer and radial diffusion were critical in successfully predicting the experimental results.

Evaluation of the relevant mass and heat transfer phenomena in a packed bed membrane reactor for the direct conversion of CO2 to dimethyl ether

This study investigates the relevant heat and mass transfer phenomena occurring at the different scales in a packed bed (membrane) reactor for the direct conversion of CO2 to dimethyl ether (DME) via the implementation of 2D heterogeneous reactor models. Intra-particle diffusion limitations were found to be relevant for particle diameters larger than 1 mm and temperature above 220 ⁰C, such that the catalyst efficiency drops down to 50% and 5% for the Cu/ZnO/Al2O3 and the HZSM-5, respectively, in the most critical conditions (i.e., 270 ⁰C and Dp of 10 mm). A component-specific Thiele modulus-efficiency correlation was developed based on the results of the rigorous particle model to account for pore-diffusion limitations without having to solve a complex heterogeneous reactor model. This correlation shows the typical behavior reported in literature for power law kinetics and accurately predicts the reaction performance with deviation of less than 5% for values of the Thiele modulus lower than 2. In the packed bed membrane reactor (PBMR), the concentration polarization (CP) also showed to affect the reactor performance. The concentration of water at the surface of the membrane selective layer was found to be up to 64% lower than the concentration in the bulk phase, hindering the effectiveness of the membrane separation. To account for this phenomenon via a simplified approach, a Sherwood-type correlation was developed to determine a CP mass transfer coefficient, based on the results obtained via the rigorous 2D PBMR model. Such correlation showed to predict with high accuracy (i.e., errors lower than 5%) the effect of the CP on the PBMR performance. Differently from the pore diffusion and CP phenomena, the intra-particle heat transfer, the particle–fluid mass and heat transfer as well as the axial dispersion were found to have a negligible effect on the reactor behavior. Finally, given the relevant mass/heat transfer phenomena, this study proposes further reactor optimization strategies, such as the reduction of the zeolite loading in the bifunctional catalyst bed by ca. 90% with respect to what is reported in literature.

Experimental investigation of a packed bed membrane reactor for the direct conversion of CO2 to dimethyl ether

In this study, the performance of a packed bed membrane reactor (PBMR) based on carbon molecular sieve membranes for the one-step CO2 conversion to dimethyl ether (DME) is experimentally compared to that of a conventional packed bed reactor (PBR) using a CuO-ZnO-Al2O3/HZSM-5 bifunctional catalyst. The PBMR outperforms the PBR in most of the experimental conditions. The benefits were greater at lower GHSV (i.e., conditions that approach thermodynamic equilibrium and water formation is more severe), with both XCO2 and YDME improvements of +35–40 % and +16–27 %, respectively. Larger sweep gas-to-feed (SW) ratios increase the extent of water removal (ca. 80 % at SW=5), and thus the performance of the PBMR. Nevertheless, alongside the removal of water, a considerably amount of all products are removed as well, leading to a greater improvement in the CO yield (+122 %) than the DME yield (+66 %). Higher temperatures selectively improve the rWGS reaction, leading to a lower YDME with respect to the PBR at 260 °C, due to the significant loss of methanol. Furthermore, larger transmembrane pressures (∆P) were not beneficial for the performance of the PBMR due to the excess reactant loss (i.e., 98–99 % at ∆P = 3 bar). Finally, the reactor models developed in our previous studies accurately describe the performance of both the PBR and PBMR in the range of tested conditions. This result is of high relevance, since the reactor models could be used for further optimization studies and to simulate conditions which were not explored experimentally.

Modeling of reverse water–gas shift reaction in a membrane integrated microreactor

CO2 hydrogenation to syngas via reverse water–gas shift (RWGS) is modeled in a membrane decorated microchannel reactor. Coated CuO/ZnO/Al2O3 catalyst exists in the reaction channel which is physically separated from the neighboring permeate channel by a layer of supported sodalite (SOD) membrane selective to H2O and H2 transport. Pure H2 is used as the sweep gas. Two–dimensional, steady state, isothermal operation of the reactor is quantified by the momentum and mass conservations in the entire flow domain, membrane material transfer and catalytic reaction. Upon its benchmarking with the literature–based experimental data, the reactor model is used to study the effects of inlet velocities and partitioning of the reactive mixture and sweep streams, reactor pressure, and molar inlet H2:CO2 ratio. At 523 K, 15 bar and H2:CO2 = 3, the per cent CO2 conversion exceeds the thermodynamic limit of 16.8% and can be maximized to 52% when the inlet velocity of the H2 + CO2 mixture is minimized. Decreased dosing of the reactive mixture, however, limits the molar amount of CO2 converted and reduces reactor capacity. Both metrics are positively correlated with reactor pressure and the inlet velocity of the sweep gas but remain insensitive to flow direction. Syngas composition (molar exit (H2 – CO2)/(CO + CO2) ratio) can be varied between 1.7 and 9.8. The proposed reactor can deliver ∼2.5 times higher volume and catalyst mass–based productivity and ∼33% higher CO2 conversion than an equivalently operated packed–bed membrane reactor.

Selective Oxidation of Methanol to Green Oxygenates – Feasibility Study of Fixed‐Bed and Membrane Reactors

AbstractA feasibility study of a conventional fixed‐bed reactor and a packed‐bed membrane reactor (PBMR) in distributor configuration is carried out for the selective oxidation of methanol to the oxygenates dimethoxymethane and methyl formate on a VOx/TiO2 catalyst. Kinetic experiments provided the reaction network and a reliable kinetic model of six main reactions involved. The PBMR offers significant advantages and potential for the formation of both target products due to an effective kinetic coupling of the oxidative dehydrogenation of methanol and the consecutive reaction steps to dimethoxymethane and methyl formate in a broad range of operation conditions.

Production of linear alpha olefin 1-octene through 1-octanol dehydration in packed-bed membrane reactors with large mesoporous membranes (PMRL) for remarkable improvement in 1-octanol conversion and 1-octene yield

In this study, we report a packed-bed membrane reactor with large mesoporous membranes (PMRL) as a solution to remarkable improvement in 1-octanol conversion and 1-octene yield of 1-octanol dehydration. Compared to the conventional packed-bed reactors (PR), 1-octanol conversion and 1-octanol yield of the PMRL increased by up to 21.3% and 16.4% in the temperature range of 340 °C–380 °C. The PMRL has simultaneously advantages of packed-bed reactors and membrane reactors. As the PMRL is equipped with large mesoporous membranes under a catalyst bed in the existing packed-bed reactors to achieve conversion enhancement like membrane reactors, the PMRL can be operated under ambient pressure without autogenous pressure in spite of the absence of a retentate side and sweeping gas which should be needed in the existing packed-bed membrane reactor equipped with dense, microporous, and mesoporous membranes because of autogenous pressure. Therefore, the PMRL can be easily applied to any existing packed-bed reactors for dehydration or dehydrogenation reaction regardless of types of heterogeneous catalysts, because the catalysts can be easily loaded on the membranes in the PMRL without the retentate side and sweeping gas.

Design and operational considerations of packed-bed membrane reactor for distributed hydrogen production by methane steam reforming

Methane steam reforming will still account for most of hydrogen production in the coming decades. Membrane reactor can play a key role in both energy saving and process/equipment compactness, particularly for its decentralized applications. Here we design a particles-based packed-bed membrane reactor and explore the operational window and design challenges by conducting systematic study experimentally and computationally, particularly emphasizing geometrical scale of membrane reactor and catalyst activity. The results show that membrane reactor presents maximum hydrogen flux by consuming unit methane under the optimized operation conditions of GHSV (i.e., 1134 hr−1) and steam-to-carbon ratio (i.e., 2), and computational study shows that optimal operation window is around 30 atm and 773.15 K. Moreover, the design criteria of “Catalyst activity – Membrane performance – Radial depth” is revealed quantitatively and catalyst activity is identified as the key limiting factor for further process intensification. Briefly, these results shed some lights on operation, optimal design, and further improvement of membrane reactor in methane steam reforming.

Integrated microsphere-packed bed enzymatic membrane reactor for enhanced bioconversion efficiency and stability: A proof-of-concept study

Fabricating high-performance enzyme reactors is requested for achieving efficient and stable bioconversions, but remains challenging, because few of them can possess high enzyme loading, sufficient mixing, and efficient mass transfer at the same time. Herein, we propose to develop a novel enzymatic packed bed membrane reactor (EPBMR) by integrating the advantages of both packed bed reactor (PBR) and enzymatic membrane reactor (EMR). A prototype study is conducted with the simplified enzyme-loaded microsphere-ultrafiltration EMR model (Mic-UF EMR). Invertase and dextranase are used in this work to produce glucose and oligodextran by hydrolysis of sucrose and dextran, respectively. Specifically, the use of microspheres can enlarge the contact area between enzymes and substrates and mitigate membrane fouling induced by free enzymes. Thus, Free&Mic-UF EMR (with both free and immobilized enzymes) exhibits a higher sucrose conversion rate (84%) than the EMR with free invertase (34%) and a negligible decline in sucrose conversion for 36 h continuous operation. Membrane fouling is ameliorated by alkaline cleaning and implementation of covalent bonding strategy. In addition, commercial resins with larger sizes are employed to replace konjac glucomannan microspheres (KGM) which reduce the pressure drop of EMR. Finally, by selecting the UF membrane with proper molecular weight cut-off (MWCO), the dextranase-based Mic-UF EMR system successfully produces oligodextran with desired molecular weight (Mw) and narrow Mw distribution. The outcome of this work not only offers a novel enzyme reactor construction strategy but also provides guidance for regulating the performance of EMR.

Integrated electrocatalytic packed-bed membrane reactor for nitrate removal

Nitrate pollution has become a widespread problem that poses a potential risk for public health. Although electrochemical reduction can be an effective and environmentally friendly strategy for nitrate removal, obtaining non-polluting products (nitrogen) in a short hydraulic retention time via this electrocatalytic process is still challenging. This work features an efficient reactor design that integrates an electrocatalytic packed-bed reactor with a membrane. Granular activated carbon (GAC) loaded with bimetal catalysts (Pd and Cu) was used as the bed packing material (Pd-Cu/GAC). The carbon membrane loaded Pd-Cu, served as cathode, filter, and current collector. The inner core packed with the Pd-Cu/GAC material functioned as an extended three-dimensional electrocatalytic cathode and catalyst. This carbon membrane system can remove 100% nitrate with the packed-bed catalyst in Na2SO4 electrolyte, but only 79.38% without the packed-bed catalyst. The packed-bed configuration can also enhance the nitrogen (N2) selectivity from 39.66 to 78.31%, increasing the NO3– removal rate from 1.72 × 10−4 to 3.62 × 10−4 mmol min−1 cm−2, respectively. Notably, when NaOH electrolyte was used, the single-pass nitrate removal can achieve 100% with a 94.25 % N2 selectivity. These excellent performances highlight the potential to apply the integrated electrocatalytic packed-bed membrane reactor system reported here for large-scale nitrate remediation.

Dimensionless analysis of reverse water gas shift Packed-Bed membrane reactors

A dimensionless analysis was performed on the reverse water gas shift packed-bed membrane reactors (RWGS PBMRs) to shift the equilibrium of the RWGS reaction by in-situ H2O removal at low temperatures. Using Damköhler, Péclet, and Stanton dimensionless numbers, the effects of sweep to reactor flow and pressure ratios, flow configuration, temperature, and H2O/H2 perm-selectivity were studied for CuO/ZnO/Al2O3 and Ru-Cu/ZnO/Al2O3 catalysts. The counter-current configuration resulted in higher CO2 conversions at milder sweep pressures when compared to the co-current configuration. It was determined that the application of RWGS PBMRs had to be limited to temperatures below 300 °C to shift the reaction equilibrium. It was concluded that to meaningfully intensify the RWGS reaction by PBMRs, weight hourly space velocities should be lowered to values below 1 hr-1 using membranes with H2O/H2 perm-selectivities greater than 100 and H2O permeance in the range of 10-6-10-5 mol m-2 s-1 Pa-1.

Process Intensification of the Propane Dehydrogenation Considering Coke Formation, Catalyst Deactivation and Regeneration—Transient Modelling and Analysis of a Heat-Integrated Membrane Reactor

A heat-integrated packed-bed membrane reactor is studied based on detailed, transient 2D models for coupling oxidative and thermal propane dehydrogenation in one apparatus. The reactor is structured in two telescoped reaction zones to figure out the potential of mass and heat integration between the exothermic oxidative propane dehydrogenation (ODH) in the shell side, including membrane-assisted oxygen dosing and the endothermic, high selective thermal propane dehydrogenation (TDH) in the inner core. The developing complex concentration, temperature and velocity fields are studied, taking into account simultaneous coke growth corresponding with a loss of catalyst activity. Furthermore, the catalyst regeneration was included in the simulation in order to perform an analysis of a periodic operating system of deactivation and regeneration periods. The coupling of the two reaction chambers in a new type of membrane reactor offers potential at oxygen shortage and significantly improves the achievable propene yield in comparison with fixed bed and well-established membrane reactors in the distributor configuration without inner mass and heat integration. The methods developed allow an overall process optimization with respect to maximum spacetime yield as a function of production and regeneration times.

A review on mathematical modeling of packed bed membrane reactors for hydrogen production from methane

The most widely used process for hydrogen production is steam methane reforming. It can be carried out using a membrane reactor in which simultaneous hydrogen production and purification occur. Mathematical modeling of these reactors plays a key role in the selection of the design and operating parameters that yield high performance for the reactor. This review study discusses, synthesizes, and compares different mathematical modeling studies on the packed bed membrane reactors for hydrogen production from methane found in the literature. Different approaches used in these modeling studies for the hydrogen permeation steps, reaction kinetic expressions, phases involved (pseudo-homogeneous and heterogeneous), and spatial dimensions (one, two, and three dimensional) are given.

Syngas production with CO2 utilization through the oxidative reforming of methane in a new cermet-carbonate packed-bed membrane reactor

A series of γ-LiAlO2-Ag cermets was studied to be integrated into a packed-bed membrane reactor with potential application in the selective separation of CO2 and O2; and simultaneous syngas production through the coupling of the oxidative CO2 reforming of methane process.The γ-LiAlO2 was chemically synthesized and incorporated into an Ag matrix, in different amounts, by powder metallurgy using ball milling and uniaxial pressing techniques. The obtained cermets exhibit excellent wettability properties against molten carbonates, facilitating their infiltration and forming dense dual-phase membranes with the molten salts. Moreover, the cermet supports show corrosion resistance against the alkaline molten carbonates and superior thermal stability due to the γ-LiAlO2 suppresses the sintering of the metallic phase.The membrane's performance was evaluated in the selective gas separation at high temperatures. The membranes exhibit simultaneous CO2 and O2 permeation with a flux of 0.78 and 0.43 ml·min-1·cm-2, at 850 °C, respectively. Besides, during the oxidative reforming process, the membrane reactor shows conversion of about 100 % of CO2 under the studied separation and reaction conditions. The syngas (H2+CO) production reaches values of 4.94 ml·min-1·cm-2 at 825 °C using a 10 % Ni/CeO2 catalyst.A long-term permeation test was conducted for 225 h, during which the membrane exhibits excellent thermal and chemical stability properties under continuous reaction conditions of syngas production. This fact is attributed to its outstanding chemical inertness against carbonates as well as the observed sinterability properties of the used cermet support.

Experimental implementation of a catalytic membrane reactor for the direct synthesis of DME from H2+CO/CO2

The direct synthesis of dimethyl ether (DME) by the hydrogenation of CO2 and CO2/COx mixtures has been studied in an original packed bed membrane reactor (PBMR). The role of the hydrophilic LTA zeolite membrane is to remove H2O from the reaction medium, reducing therefore the thermodynamic limitations of methanol synthesis and dehydration stages. LTA zeolite has the best permeation properties among the studied zeolites (LTX and SOD). The experiments were carried out using a CuO-ZnO-ZrO2/SAPO-11 catalyst at 275–325 °C, 10–40 bar, space time of 10 gcat h (molC)−1 and using in the permeate section a sweeping gas flowrate of the same composition as that fed to the reaction section. The results (DME yield, CO2 conversion and product distribution) of the PBMR are compared with those obtained in PBR without membrane. In the hydrogenation of CO2, a DME yield of 12% and a CO2 conversion of 20% are obtained at 275 °C, 40 bar and space time of 10 gcat h (molC)−1 with a great catalyst stability.

Stability of electroless pore-plated Pd-membranes in acetic acid steam membrane-reformers for ultra-pure hydrogen production

Electroless Pore-Plated (ELP-PP) membranes were successfully incorporated for the first time into a membrane reactor to produce hydrogen by acetic acid steam reforming (AASR), exhibiting adequate resistance against harsh operating conditions. Membranes were prepared onto tubular PSS supports modified with Pd/CeO2 particles and scaled-up around four times in length with high reproducibility respect previous studies. H2 permeances from 4.49 to 5.67·10−4 mol m−2 s−1 Pa-0.5 were found for pure H2 at 350–450 °C, decreasing for mixtures due to concentration-polarization at higher pressures but also certain inhibition caused by CO2 at pressures below 50 Pa0.5. The combination of membranes with Ni/SBA-15 catalysts in packed-bed membrane reactors (PBMR) evidenced the simultaneous improvement of acetic acid conversion and hydrogen yield respect to analogous experiments in traditional packed-bed reactors (PBR). A very similar product distribution was obtained for both configurations, PBR and PBMR, when using fresh catalysts, although marked deviations were found in case of regenerating the catalysts. Then, higher selectivity towards coke reached for PBMR, which lead to around 30% for the most elevated pressure under investigation. However, even at these harsh conditions, the mechanical integrity of ELP-PP membranes was maintained. Thus, the benefits of combining catalysts and ELP-PP membranes in a PBMR for AASR were demonstrated.