Shift Reaction Research Articles

Pressurized diesel fuel processing using hydrogen peroxide for the fuel cell power unit in low-oxygen environments

A novel concept for diesel fuel processing utilizing H2O2 is suggested to obtain the high-purity H2 required for air-independent propulsion using polymer electrolyte membrane fuel cells for use in submarines and unmanned underwater vehicles. The core components include 1) a diesel-H2O2 autothermal reforming (ATR) reactor to produce H2-rich gas, 2) a water-gas shift (WGS) reactor to convert CO to H2, and 3) a H2 separation membrane to separate only high-purity H2. Diesel and H2O2 can easily be pressurized as they are liquids. The application of the H2 separation membrane without a compressor in the middle of the process is thus advantageous. In this paper, the characteristics of pressurized ATR and WGS reactions are investigated according to the operating conditions. In both reactors, the methanation reaction is enhanced as the pressure increases. Then, permeation experiments with a H2 separation membrane are performed while varying the temperature, pressure difference, and inlet gas composition. In particular, approximately 90% of the H2 is recovered when the steam-separated rear gas of the WGS reactor is used in the H2 separation membrane. Finally, based on the experimental results, design points are suggested for maximizing the efficiency of the diesel-H2O2 fuel processor.

Guiding a divergent reaction by photochemical control: bichromatic selective access to levulinates and butenolides.

Allylic and acrylic substrates may be efficiently transformed by a sequential bichromatic photochemical process into derivatives of levulinates or butenolides with high selectivity when phenanthrene is used as a regulator. Thus, UV-A photoinduced cross-metathesis (CM) couples the acrylic and allylic counterparts and subsequent UV-C irradiation initiates E-Z isomerization of the carbon-carbon double bond, followed by one of two competing processes; namely, cyclization by transesterification or a 1,5-H shift and tautomerization. Quantum chemical calculations demonstrate that intermediates are strongly blue-shifted for the cyclization while red-shifted for the 1,5-H shift reaction. Hence, delaying the double bond migration by employing UV-C absorbing phenanthrene, results in a selective novel divergent all-photochemical pathway for the synthesis of fundamental structural motifs of ubiquitous natural products.

Dynamic operation of water gas shift reaction over Fe2O3/Cr2O3/CuO catalyst in Pd/Al2O3 membrane reactor

Hydrogen has been considered as promising energy carrier that can be produced from renewable resources, such as biomass through gasification. This process results in producer gas containing CO, CO2, H2, N2, and CH4. The conventional enhancement of hydrogen is typically conducted using several unit operations such as water gas shift reactor (WGSR) and separation unit such as Pressure Swing Adsorption (PSA). Process intensification offers a new method to integrate both WGSR and separation unit into single membrane reactor. This research aimed to investigate the influence of dynamic operation on membrane reactor performance. The steady state fixed bed reactor and membrane reactor were used as base case to judge the performance of dynamic membrane reactor. The water gas shift reaction over Fe2O3/Cr2O3/CuO was carried out at 350°C and 1 atm by varying the feed composition and gas residence time. The feed composition ratio of H2O/CO consisted of 2 and 3 on mole basis, while the gas residence times were 1.2 s and 2.3 s. The membrane reactor consists of shell and tube sides made of Pd/Al2O3 material with technical specification of 10 mm inner diameter, 20 μm Pd thickness supported by alumina, and 10 cm reactor length. The compositions of the feed gas and products were measured using gas analysers such CO gas detector (Bacharach PCA® 3) and H2 gas detector (Cosmos XP-3140). The dynamic operation was performed following the square wave perturbation of the feed gas at switching time of 15 s. The experiment results showed that increasing the feed composition ratio and gas residence time increased the conversion of CO and hydrogen production in the fixed bed reactor and membrane reactor. Higher production of hydrogen also improved the recovery of hydrogen in membrane reactor. The use of membrane reactor increased significantly the conversion of CO when compared to fixed bed reactor. Moreover, the dynamic membrane reactor would give much better performance in term of CO conversion and hydrogen recovery. The stability of the Pd/Al2O3 membrane reactor was proven for at least 10 h operation.

Hydrogen production by steam methane reforming in a membrane reactor equipped with a Pd composite membrane deposited on a porous stainless steel

With the aim of producing hydrogen at low cost and with a high conversion efficiency, steam methane reforming (SMR) was carried out under moderate operating conditions in a Pd-based composite membrane reactor packed with a commercial Ru/Al2O3 catalyst. A Pd-based composite membrane with a thickness of 4–5 μm was prepared on a tubular stainless steel support (diameter of 12.7 mm, length of 450 mm) using electroless plating (ELP). The Pd-based composite membrane had a hydrogen permeance of 2.4 × 10−3 mol m−1 s−1 Pa−0.5 and an H2/N2 selectivity of 618 at a temperature of 823 K and a pressure difference of 10.1 kPa. The SMR test was conducted at 823 K with a steam-to-carbon ratio of 3.0 and gas hourly space velocity of 1000 h−1; increasing the pressure difference resulted in enhanced methane conversion, which reached 82% at a pressure difference of 912 kPa. To propose a guideline for membrane design, a process simulation was conducted for conversion enhancement as a function of pressure difference using Aspen HYSYS®. A stability test for SMR was conducted for ∼120 h; the methane conversion, hydrogen production rate, and gas composition were monitored. During the SMR test, the carbon monoxide concentration in the total reformed stream was <1%, indicating that a series of water gas shift reactors was not needed in our membrane reactor system.

Cu‐Decorated ZnO Nanorod Array Integrated Structured Catalysts for Low‐Pressure CO2 Hydrogenation to Methanol

AbstractCO2 conversion into valuable chemicals and fuels, such as methanol, is one of the most practical routes for utilizing emitted CO2 and mitigating global warming. Herein, a 3D Cu‐decorated ZnO nanorod array based structured catalysts for efficient thermochemical CO2 hydrogenation to methanol at relatively low pressures (&lt;10 atm) is successfully fabricated and demonstrated. This new type of nanorod array integrated structured catalysts has yielded a methanol formation rate of 1.9 mol h−1 kg−1 with a methanol selectivity of 56%, rivaling the state‐of‐the‐art powder‐form catalysts. The well‐dispersed copper species on the array structure as well as the array‐structure‐enhanced interfacial effect are key factors that improve the activity of the nanorod array catalysts in CO2 hydrogenation. The Cu‐ZnO nanorod array interface also suppresses reverse water‐gas shift reaction, reducing the selectivity to CO. Further improvement of the performance of the nanorod array based catalysts is demonstrated by tuning the ZnO nanorod array length. The developed nanorod array integrated monolithic catalysts also exhibit good stability during a long‐time continuous operation, demonstrating the potential and the feasibility of their practical implementation in industrial situation.

Pressurized gasification of lignite in a pilot scale bubbling fluidized bed reactor with air, oxygen, steam and CO2 agents

In this study, 80 h continuously operated gasification experiment was carried out with pilot scale pressurized bubbling fluidized bed gasifier which was operated with the coal feed capacity of 500–520 kWth (80–83 kg/h coal feed rate). The mixture of air, steam, oxygen and CO2 was used as gasification agent with different ratios. The operating pressure of gasifier in this experiment was between 2.4 and 2.7 barg. The effects of ER, steam/carbon ratios and CO2/carbon ratios on syngas composition, carbon conversion ratios and cold gas efficiencies were investigated. According to the results, using CO2 or H2O as gasification agent, may have both advantages and disadvantages for the operation. If CO2 was increased in gasification agent, shift reaction was effected negatively and H2 products were decreased. If steam was increased, cold gas efficiency was slightly decreased.

Modeling and simulation of water-gas shift in a heat exchange integrated microchannel converter

The aim of this study is to analyze the operation of a heat exchange integrated, Pt-CeO2/Al2O3 washcoated microchannel water-gas shift (WGS) reactor under fuel processing conditions by mathematical modeling techniques. In this context, operation of a single microchannel is modeled, whose outcomes are compared with experimental data obtained from the literature. Simulations show good agreement with the experimental data, with an error below 4%. Upon its validation, single channel model is used to simulate a heat exchange integrated microchannel reactor, which involves periodically located groups of reaction and air-fed cooling channels. The integrated reactor is modeled by 2D Navier-Stokes equations together with reactive transport of heat and mass. Incorporation of heat exchange function minimizes the impact of thermodynamic limitations on WGS by precise regulation of reaction temperature and gives 77.6% CO conversion, which is 67.4% in the absence of cooling. Improvement in conversion from 69.2% to 77.6% is observed upon increasing feed temperature of the reaction stream from 565 to 595 K, above which the reaction is controlled by equilibrium. Coolant feed temperature, however, changes conversion only by <1%. Isothermal conditions are obtained upon feeding reaction and coolant channels at 595 K and 587 K, respectively. Changes in the thickness and material of the wall between the channels give limited deviations in conversion. An integrated reactor with 2.37 L volume is sufficient for supplying H2 necessary to drive a 1 kW PEMFC unit.

Mass Spectrometric Mechanistic Investigation of Ligand Modification in Hafnocene-Catalyzed Olefin Polymerization

We recently reported evidence that a cyclometalated intermediate can facilitate the polymerization of 1-hexene to append polymer chains to the termini of propyl groups of the Me2Hf(Cpn-Propyl)2 catalyst precursor. Herein we provide further mechanistic details on the activation of Me2Hf(Cpn-Propyl)2 by B(C6F5)3 and the polymerization of 1-hexene mainly by applying a battery of mass spectrometry-based techniques. First, a combination of MALDI and CID fragmentation is used to characterize the high molecular mass region (up to 6 kDa) of the isolated poly(1-hexene) material with attached metallocene. The CID fragmentation patterns are explained by relatively low-energy ligand losses and higher energy hydrocarbon chain degradation via C–C bond cleavage and 1,3-hydrogen shift reactions. Further mechanistic insights are gained by investigating 1-hexene polymerization reaction employing a properly 13C-labeled catalyst activated by B(C6F5)3. Mass spectrometry analyses, along with supporting NMR experiments, indicat...

Characterization of High Temperature PEM Fuel Cells for Electrochemical Hydrogen Pumping

High temperature proton exchange membrane fuel cells (HT-PEMFCs) based on phosphoric acid doped polybenzimidazole operate at a temperature range between 140°C and 200°C. Due to their high operating temperature, HT-PEMFCs can tolerate a relatively high concentration of impurities in the anodic fuel stream. This makes HT-PEMFCs suitable for stationary applications where hydrogen is generated on site by steam reforming of hydrocarbons such as methane or oil derivatives. In particular, the preferential oxidation stage (PROX), which is typically required to reduce the CO concentration to ≈10 ppm after the reforming and water gas shift (WGS) reactors, is no longer necessary. Thus, fuel treatment units are simpler and cheaper with HT-PEMFCs [1]. The proven robustness of HT-PEMFCs against fuel impurities has recently attracted interest to operate the HT-PEMFC as a ‘hydrogen pump’ for hydrogen purification applications. In this configuration, a hydrogen rich gas stream is supplied to the cell’s anode compartment and a current is externally applied through the cell. Different from a typical fuel cell, no oxygen is supplied on the cathode side. During this process, hydrogen is electrochemically ‘pumped’ from the anode to the cathode in the form of protons through the electrolyte membrane. The ‘pump effect’ is highly selective and a pure hydrogen stream is obtained at the cathode outlet of the cell (≈10 ppm). Compared with low temperature Nafion based fuel cells, HT-PEMFCs are much more promising for purification of hydrogen streams that contain considerable amounts of impurities, as proven by preliminary studies [2, 3]. In this work, an investigation of the HT-PEMFC operated as an electrochemical hydrogen pump is carried out. The impact of hydrogen dilution and CO poisoning is studied as well as the effects of hydrogen stoichiometry, gas humidification, and electrolyte resistance. The cell is characterized with various techniques including polarization curves, electrochemical impedance spectra (EIS), and distribution of relaxation times (DRT) analysis (Fig. 1). Complementary to the equivalent circuit approach, DRT maps the EIS data to a function that contains the characteristic time scales of the system [4]. These results are important for the assessment of the HT-PEMFC’s potential for hydrogen purification. Although this application is distinctly different from that of a typical fuel cell, the electrochemical process at the anode is actually the same as in a normal HT-PEMFC. Therefore, the study also helps us gain valuable insight into the hydrogen oxidation reaction process in the presence of impurities.

Potassium‐catalyzed steam gasification of ash‐free lignite coal with CO2 capture

AbstractThe purpose of this research was to study steam gasification of ash‐free coal integrated with CO2 capture in the presence of a K2O catalyst for enhancement of the key water‐gas shift reaction and promotion of hydrogen production. To achieve this goal, gasification experiments on ash‐free coal (AFC) were carried out at varying temperatures (600, 650, 675, 700, and 750 °C) with a sorbent‐to‐carbon (CaO/C) ratio of 2 and a catalyst (K2O) loading of 0.2 g/g (20 weight percent (wt%)) in a fixed‐bed reactor equipped with a gas chromatography analyzer. The sorbent‐to‐carbon (CaO/C) ratio of 2 is based on dry and ash‐free basis. The CaO/C ratio and K2O wt% were chosen to maximize hydrogen production based on our previously determined optimal values. The AFC was originally extracted from raw lignite coal using organic solvents, which allowed the sorption‐enhanced gasification to be conducted with minimal ash‐catalyst interactions. The effect of temperature on the yield and the initial reaction rate were investigated. The optimal reaction temperature of 675 °C was determined. Carbon balance and final carbon conversions were calculated based on the residue analysis. Activation energy was also calculated using intrinsic kinetics of the reaction. In this study, using AFC offered the potential advantage of operating the gasification process with catalyst recycle.

Review of Hydrogen Production by Catalytic Aqueous‐Phase Reforming

AbstractCatalytic aqueous‐phase reforming (APR) produces higher quality hydrogen (with less carbon monoxide) and carbon dioxide from weak solutions of bio‐carbohydrates in a single reactor at low temperatures. It provides a good opportunity for the effective valorisation of biomass‐derived products. It is advantageous than steam reforming because it saves energy by avoiding vaporization of the biofeed and lowers cost by precluding an extra water gas shift reactor. As evident from the numerous published works during the past decade, there is growing academic and industrial interest in the APR process. This review updates recent literature on APR of many biomass surrogates such as glycerol, ethylene glycol, sorbitol, ethanol and glucose. Most works focused on the development of efficient catalysts for selective hydrogen production and they were deliberated comprehensively. Key insights into improved catalysts and reaction conditions were highlighted. New inferences on the thermodynamic, kinetic and reactor engineering aspects of the APR process were analysed too. This thorough appraisal of the current literature, which is hitherto missing, will surely contribute to the development of the next generation of catalysts and reactors for commercial applications of the APR process.

Gasification characteristics of glass fiber-reinforced plastic (GFRP) wastes in a microwave plasma reactor

The effects of plasma power (1–1.8 kW), oxygen/fuel (0–2.5) and steam/fuel ratios (0–1) on the gasification characteristics of glass fiber-reinforced plastic (GFRP) wastes have been determined in a microwave plasma reactor. GFRP, which is thermosetting plastic composed of glass fibers embedded within a polymer matrix, was used as an experimental sample. While carbon conversion increased with oxygen/fuel ratio, syngas heating value and cold gas efficiency decreased with oxygen supply due to the onset of combustion. With increasing steam/fuel ratio, water-gas shift and ion-reforming reaction favored higher concentration of H2. Increasing the plasma power was found to promote the conversion of carbon dioxide to carbon monoxide. The char surfaces of GFRP that were subjected to variable power and oxygen supplies were analyzed by scanning electron microscopy.

Co-gasification of biomass and municipal solid waste for hydrogen-rich gas production

ABSTRACTGasification is a high-temperature thermochemical process to generate a clean syngas which can be used as an alternative method for fuel conversion. In this article, a kinetic model of co-gasification of biomass and municipal solid waste (MSW) was developed to study the influence of several critical parameters such as biomass/MSW ratio, reactor temperature, and steam/fuel ratio on gas composition, hydrogen yield, and tar content. Results showed that the H2 concentration significantly varies in the produced syngas with changing the MSW/biomass ratio may be due to limited water gas shift and tar cracking reactions. Also, it was found that the tar content does not change significantly with average values of steam/fuel ratio probably due to the slow kinetics of the hydrocarbon steam reforming reactions at a constant temperature.

Hydrogen Production from Bioethanol: Behavior of a Carbon Oxide Preferential Oxidation Catalyst

AbstractHydrogen is recognized as a promising green energy source, particularly when used to feed a polymer electrolyte membrane fuel cell (PEMFC). Here, hydrogen was obtained by bioethanol steam reforming with CO and CO2 as primary sub products. Since the cell anode is extremely sensitive to poisoning with CO, water‐gas shift (WGS) and carbon oxide preferential oxidation (COPROX) reactors were employed for hydrogen purification. Catalysts prepared by our lab were tested at pilot plant scale in both the reformer and COPROX unit, where different active phase distributions, stoichiometric excess of air, and reaction temperatures were tested. The use of two different COPROX units with intermediate air injection was also considered. The as‐prepared catalysts showed good stability and performance.

Total Integrated Operation of Gasifier, Hot Gas Desulfurizer, and SEWGS Process for Pre-combustion CO2 Capture Using Real Syngas from Coal

SEWGS (Sorption Enhanced Water Gas Shift) process is one of options for pre-combustion CO2 capture using dry absorbent and water gas shift catalyst. In this process, the thermodynamic equilibrium in the shift reaction can be enhanced to give more hydrogen yield by adding a CO2 absorbent into the shift reactor. Total integrated system consists of coal gasifier, hot gas clean-up process (two interconnected fluidized bed desulfurizer), and one loop SEWGS process. In this presentation, continuous operation results of the hot gas clean-up process and one loop SEWGS process using dry absorbents at high temperature and pressure conditions were discussed. Dry absorbents (for desulfurization, CO2 absorption) were produced by KEPCO RI (Korea Electric Power Corporation Research Institute) by means of spray-drying method. Continuous operation was performed at high pressure (21bar for gasifier, 20bar for hot gas clean-up process, and 18bar for SEWGS process) and reaction temperature was 550oC for desulfurizer and 236oC for SEWGS reactor. Totally integrated operation was maintained up to 50hours. We could get high sulfur capture efficiency (99.6%) in the desulfurizer, high CO conversion (98.9%) and CO2 capture efficiency (98.0%) in the SEWGS reactor.

Development of a Segmented Single SOFC Test Equipment to Simulate Stack-Like Operating Conditions

A common problem when it comes to stack CFD modelling is the lack of detailed local information about temperatures and gas compositions. For the calibration and validation of the CFD models local measurements of these parameters are required. However, it is fairly difficult implementing such measurements in commercial stacks without changing the stack design to allow for additional thermocouples or gas extraction channels. Furthermore, such implementations would automatically change the stack behavior compared to a stack without additional instrumentation due to heat and gas losses caused by the measurement itself. On the other hand standardized single cell tests do not represent stack like conditions due to typically very homogenous temperature distributions. Therefore, a new single cell test equipment based on a segmented single SOFC which enables an operation of the cell under stack like conditions was developed. The aim of this development is to provide a single cell test equipment which provides comprehensive data about temperature distribution, cell voltage distribution and local gas compositions to be used for the calibration of a commercial CFD code [1]. The complete test equipment was simulated by means of CFD and the results were compared with experimental data. The single cell consists of a commercial anode supported SOFC with 4 segmented cathodes (40.5x44 mm2 each) and 1 anode (120x120 mm2). The segmented cathode allows the measurement of local cell voltages. Furthermore, several gas extraction channels along the anode flow channels were implemented to measure the gas conversion with respect to the electrochemical and steam reforming reactions taking place. As the steam reforming reaction has a significant impact on the temperature profile, in real stacks it is important to consider the conversion rate properly along the anode to allow for a correct simulation of the temperature distribution. The temperature profile was measured with 34 thermocouples which were distributed along the anode flow field below the anode surface. Several test cases to calibrate the CFD model regarding the thermal behavior were carried out by placing the test equipment in an electric oven and heating it up to 600 °C. The cell test equipment was additionally equipped with 4 electrical heaters placed below the anode channels to produce temperature profiles similar to real stack operating conditions. Therefore, also inhomogeneous temperature profiles can be produced. The 4 electrical heaters can be controlled individually to heat each of the 4 segments differently. The electrical heaters provide enough heat to increase the temperature of the cell up to 800 °C. Therefore, temperature profiles along the cell with gradients of 150 K between the hottest and coldest spot along the active cell area were achieved. By changing the set oven temperature this gradient can be further modified. Existing stack temperature profiles were used to calibrate the test equipment which enables similar temperature distributions as they occur for a stack under real operation. The CFD simulation meets the measured temperature profile within 10 K which is seen to be a very accurate result. Furthermore, this work will show the comparison of experimental and CFD simulation results for the operation of the cell at 700, 750 and 800 °C in H2 and CH4/H2O operation. The comparison covers local cell voltages, the temperature distribution and the gas compositions. For both gas feed mixtures a fitting of the CV curve within the CFD software was carried out. It can be seen that the electrochemical behavior can be simulated fairly accurately by the software. The software allows also for the consideration of steam reforming and shift reactions along the complete anode flow path. By adjusting the activation energy as well as the rate-constant for both reactions, the same behavior as it was measured in the experiment could be achieved. As expected it can be seen that the conversion of methane by steam reforming is higher at the inlet of the single cell. This effect correlates very well with the observed temperature decrease in this region caused by endothermic steam reforming which is in the range of 10 K. It has been proven that this kind of test equipment is a very powerful tool to calibrate the CFD simulation models as basis for further full scale stack simulations. A further potential utilization of this approach is the possibility to transfer the validated temperature profiles into a FE simulation to enable an experimentally supported investigation of thermo-mechanical stresses within the cell or sealing. [1] FIRETM v2017, User Manual, AVL List GmbH, 2017.

Simulation of Water Gas Shift Zeolite Membrane Reactor

The search of alternative energy sources keeps growing from time to time. Various alternatives have been introduced to reduce the use of fossil fuel, including hydrogen. Many pathways can be used to produce hydrogen. Among all of those, the Water Gas Shift (WGS) reaction is the most common pathway to produce high purity hydrogen. The WGS technique faces a downstream processing challenge due to the removal hydrogen from the product stream itself since it contains a mixture of hydrogen, carbon dioxide and also the excess reactants. An integrated process using zeolite membrane reactor has been introduced to improve the performance of the process by selectively separate the hydrogen whilst boosting the conversion. Furthermore, the zeolite membrane reactor can be further improved via optimizing the process condition. This paper discusses the simulation of Zeolite Membrane Water Gas Shift Reactor (ZMWGSR) with variation of process condition to achieve an optimum performance. The simulation can be simulated into two consecutive mechanisms, the reaction prior to the permeation of gases through the zeolite membrane. This paper is focused on the optimization of the process parameters (e.g. temperature, initial concentration) and also membrane properties (e.g. pore size) to achieve an optimum product specification (concentration, purity).

Development of a Segmented Single SOFC Test Equipment to Simulate Stack-Like Operating Conditions

This work presents a new single cell test equipment based on a segmented single SOFC to perform cell tests under stack like conditions. The setup provides comprehensive data about temperature distribution, cell voltage distribution and local gas compositions to be used for the calibration of a commercial CFD code (1). Results from experiments will be compared with CFD simulations for operating temperatures at 700, 750 and 800 °C using H2/N2 or CH4/H2O as fuel, respectively. The CFD simulation meets the measured temperature profiles within 10 K. The simulation also includes steam reforming and shift reactions along the complete anode flow path. For both gas feeds, a fitting of the CV curve within the CFD model was carried out. It has been proven that this kind of test equipment is a very powerful tool to calibrate the CFD simulation models as a basis for further full scale stack simulations.

A Vinyl-Cation-Induced 1,3-Aryl Shift.

A net insertion of an unactivated, internal alkyne into a sp2 -sp3 C-C bond of simple benzylic alcohols was achieved using the rearrangement of a highly reactive vinyl cation intermediate to a stabilized allyl cation as the driving force for an unusual 1,3-carbon shift reaction. In the presence of 10 mol % of Al(OTf)3 as a simple, inexpensive, and abundant catalyst, high selectivity for the rearrangement was achieved. The reaction scope proved general with regard to both the alkyne and the benzylic alcohol and a range of 1,2-dihydroquinolines as well as 2H-chromenes were obtained.

A diesel fuel processor for fuel-cell-based auxiliary power unit applications

Producing a hydrogen-rich gas from diesel fuel enables the efficient generation of electricity in a fuel-cell-based auxiliary power unit. In recent years, significant progress has been achieved in diesel reforming. One issue encountered is the stable operation of water-gas shift reactors with real reformates. A new fuel processor is developed using a commercial shift catalyst. The system is operated using optimized start-up and shut-down strategies. Experiments with diesel and kerosene fuels show slight performance drops in the shift reactor during continuous operation for 100 h. CO concentrations much lower than the target value are achieved during system operation in auxiliary power unit mode at partial loads of up to 60%. The regeneration leads to full recovery of the shift activity. Finally, a new operation strategy is developed whereby the gas hourly space velocity of the shift stages is re-designed. This strategy is validated using different diesel and kerosene fuels, showing a maximum CO concentration of 1.5% at the fuel processor outlet under extreme conditions, which can be tolerated by a high-temperature PEFC. The proposed operation strategy solves the issue of strong performance drop in the shift reactor and makes this technology available for reducing emissions in the transportation sector.