Shift Reaction Research Articles

Atmospheric oxidation of 1-butene initiated by OH radical: Implications for ozone and nitrous acid formations

The present study combines (i) field measurements of 1-butene over Xi'an and surrounding areas during a heavy ozone pollution episode with (ii) quantum chemical calculations on the photochemical transformation of 1-butene initiated by OH radical. The measurements show that the diurnal variation of both 1-butene and ozone exhibits a negative relationship during the sampling campaign. The concentrations of 1-butene vary from 0.04 to 0.67 ppbv, and the lowest and highest values emerge in the noon time (1 p.m.–3 p.m.) and in the night time (1 a.m.–3 a.m.). The concentrations of O3 range from 32.36 to 88.82 ppbv, and the high values appear in the noon time. Quantum chemical calculations show that the OH-addition pathways are more energetically preferable than H-abstraction channels, and the rate coefficient exhibits a negative T-dependence in the temperature range of 273–400 K. The autoxidation of peroxy radicals (RO2) formed from the addition of molecular oxygen to OH-addition products S2 and S3 leads to the formation of highly oxygenated molecules (HOMs), C4H9O5, in which the 1,5-H shift reaction is favoured. In the low-NOx regions, RO2 radicals mainly react with HO2 radical leading to hydroperoxide ROOH on both the singlet and triplet PESs, in which the triplet PES is preferable. In the high-NOx regions, RO2 radicals mainly react with NO leading to the formation of RO· + NO2, aldehyde + HONO and organic nitrate, in which the HONO formation appears to be previously unconsidered in the photochemical transformation of alkenes. The branching ratio of RO· + NO2 increases slowly with increasing temperature (from 51.3 to 52.7%), whereas aldehyde + HONO gradually decreases with the temperature rising (from 48.7 to 47.3%). The formation of organic nitrate is negligible over the temperature range of 273–400 K. These findings are expected to deepen our understanding the photochemistry oxidation of alkene under realistic atmospheric conditions.

Thermodynamic and techno-economic assessment of pure and zeotropic fluid ORCs for waste heat recovery in a biomass IGCC plant

The present study includes a thermodynamic and techno-economic assessment of Organic Rankine Cycle (ORC) for waste heat recovery (WHR) from three types of waste heat sources in biomass-fuelled integrated gasification combined cycle (BIGCC) plants equipped with carbon capture and storage (CCS). These include (1) the air separation unit (ASU) air compression intercoolers, (2) the CCS CO2 compression intercoolers and (3) syngas cooler at the water gas shift reactor outlet. The use of ORCs operating with pure working fluids and zeotropic mixtures is investigated. In each scenario, the optimal cycles that maximize plant efficiency improvement are determined and are subsequently economically evaluated. Among the three, the syngas cooling integration scenario leads to the highest plant efficiency improvement (2.81%) and best economic performance, showing a levelized cost of electricity (LCOE) and discounted payback period (DPP) of 35.42–35.67 €/MWhe and 5.7–5.8 years. Meanwhile, if all three heat sources are utilized, an efficiency improvement of 4.61% is achieved, while the corresponding LCOE and DPP are about 49.76–51.08 €/MWhe and 9.3–9.7 years. In all scenarios, the best thermodynamic and economic results are obtained by ORCs operating with mixtures. Despite their thermodynamic superiority, however, zeotropic ORCs have a relatively small economic advantage over pure fluid cycles.

Role of Carbon Dioxide Reforming Reaction Rate of Methane in Solid Oxide Fuel Cell Simulation: Effect of Inlet Fuel Related Parameters

ABSTRACT The present study assessed the reaction rate of methane carbon dioxide reforming (MCDR) in solid oxide fuel cells (SOFCs). This reaction rate was compared with the rates of the methane steam reforming (MSR), and the water-gas shift (WGS) reactions to evaluate its importance in simulating a SOFC. In addition, the effect of the system inlet parameters involving the Reynolds number, steam to carbon ratio (S/C), and CO2/CH4 on reaction rate variations was investigated. In this regard, a numerical model having axial symmetry was used to simulate the reaction of MCDR. Based on the results of the present study, the rate of this reaction was significant compared to that of the MSR, and WGS reaction and its ignoring cause inaccuracy in simulation results. According to the parameters investigated in this study, the change in S/C led to a low variation in the MCDR reaction rate. As the S/C increases from 0 to 0.5, the reaction rate increases from 8.9 to 12.5. Further, since the rate of CO2 absorption in the catalyst was very less compared to that of CH4, the effect of the molar ratio of CO2on the reforming reaction rate is much greater than the effect of the molar ratio of CH4. This can decrease the reaction rate of MCDR when the CO2 molar ratio reduces and CH4 molar ratio and the multiplication of the molar ratios of CH4 and CO2 increases. As the Reynolds number increases from 7.5 to 27.5, despite increasing the multiplication of the CH4 and CO2 molar ratios by 86%, this reaction rate decreases by 47% due to the decrease in CO2 molar ratio by 34%. Additionally, the greater impact of CO2 molar ratio led to an increase in the CO2/CH4 molar ratio possessed the greatest effect on the rate of this process. The addition of molar ratio from 0 to 0.5 resulted in increasing the rate of MCDR in the center of SOFC from 8.9 to 21.8 mol/m3/s.

Simulation and optimization of hydrogen production by steam reforming of natural gas for refining and petrochemical demands in Lebanon

Steam reforming of natural gas produces the majority of the world's hydrogen (H2) and it is considered as a cost-effective method from a product yield and energy consumption point of view. In this work, we present a simulation and an optimization study of an industrial natural gas steam reforming process by using Aspen HYSYS and MATLAB software. All the parameters were optimized to successfully run a complete process including the hydrogen production zone units (reformer reactor, high temperature gas shift reactor HTS and low temperature gas shift reactor LTS) and the purification zone units (absorber and methanator). Optimum production of hydrogen (87,404 MT/year) was obtained by fixing the temperatures in the reformer and the gas shift reactors (HTS & LTS) at 900 °C, 500 °C and 200 °C respectively while maintaining a pressure of 7 atm, and a steam to carbon ratio (S/C) of 4. Moreover, ~99% of the undesired CO2 and CO gases were removed in the purification zone and a reduction of energy consumption of 77.5% was reached in the heating and cooling units of the process.

Dynamic Modeling and Control of a Coupled Reforming/Combustor System for the Production of H2 via Hydrocarbon-Based Fuels

The present work aims to provide insights into the dynamic operation of a coupled reformer/combustion unit that can utilize a variety of saturated hydrocarbons (HCs) with 1–4 C atoms towards H2 production (along with CO2). Within this concept, a preselected HC-based feedstock enters a steam reforming reactor for the production of H2 via a series of catalytic reactions, whereas a sequential postprocessing unit (water gas shift reactor) is then utilized to increase H2 purity and minimize CO. The core unit of the overall system is the combustor that is coupled with the reformer reactor and continuously provides heat (a) for sustaining the prevailing endothermic reforming reactions and (b) for the process feed streams. The dynamic model as it is initially developed, consists of ordinary differential equations that capture the main physicochemical phenomena taking place at each subsystem (energy and mass balances) and is compared against available thermodynamic data (temperature and concentration). Further on, a distributed control scheme based on PID (Proportional–Integral–Derivative) controllers (each one tuned via Ziegler–Nichols/Z-N methodology) is applied and a set of case studies is formulated. The aim of the control scheme is to maintain the selected process-controlled variables within their predefined set-points, despite the emergence of sudden disturbances. It was revealed that the accurately tuned controllers lead to (a) a quick start-up operation, (b) minimum overshoot (especially regarding the sensitive reactor temperature), (c) zero offset from the desired operating set-points, and (d) quick settling during disturbance emergence.

Reforming of diesel and jet fuel for fuel cells on a systems level: Steady-state and transient operation

The operation of fuel cell systems using liquid fuels widens the application possibilities of this promising energy conversion technology. However, systems utilizing diesel and jet fuel reforming are fairly complex and suffer from poor stability and limited dynamics. To address these challenges, this paper investigates the steady-state and transient operation of a 28 kWth fuel processor on the systems level. With the help of experiments that make use of the developed prototype, suitable operating parameters are sought to maximize the simultaneous fuel conversion in the reformer and CO conversion in the shift reactor. Furthermore, a load change strategy is developed with the aim of keeping the CO concentration at the fuel cell anode inlet below the target concentration of 1% of the wet product gas at all times. The identified parameters enable very high conversions (>99.95%) and CO concentrations even lower than the target during steady-state operation using three commercial fuels under full load. The developed load change strategy was validated during 90 min tests, including 16 load change cycles with loads between 40% and 100%. As well as providing excess steam during load change, the selection and control of optimal O2/C and H2O/C ratios and temperature levels proved to be of key importance. In order to minimize the CO concentration, it is recommended to operate the reformer at the identified parameters for each fuel and keep the shift outlet temperature between 295 and 300 °C by adjusting the water feed. The proposed fuel processor concept and the experimentally-validated operating strategies in this work can enable the successful implementation of fuel cell technology in different application areas, including auxiliary power units, remote power systems and range extenders.

The Demonstration of the Superiority of the Dual Ni-Based Catalytic System for the Adjustment of the H2/CO Ratio in Syngas for Green Fuel Technologies

A novel dual Ni-based catalytic process (DCP) to control the H2/CO ratio of 2 in the syngas product within one step at temperature <700 °C was created and constructed. With the sequence of the catalysts located in the single reactor, the endothermic combined steam and CO2 reforming of methane (CSCRM) reaction and the exothermic ultra-high-temperature water–gas shift (UHT-WGS) reaction work continuously. During the process, the H2/CO ratio is raised suddenly at UHT-WGS after the syngas is produced from CSCRM, and CSCRM utilizes the heat released from UHT-WGS. Due to these features, DCP is more compact, enhances energy efficiency, and thus decreases the capital cost compared to reformers connecting with shift reactors. To prove this propose, the DCP tests were done in a fixed-bed reactor under various conditions (temperature = 500, 550, and 600 °C; the feed mixture (CH4, CO2, H2O, and N2) with H2O/(CH4 + CO2) ratio = 0.33, 0.53, and 0.67). According to the highest CH4 conversion (around 65%) with carbon tolerance, the recommended conditions for producing syngas with the H2/CO ratio of 2 as a feedstock of Fischer–Tropsch synthesis include the temperature of 600 °C and the H2O/(CH4 + CO2) ratio of 0.53.

Integration of water electrolysis for fossil-free steel production

This study investigates the integration of water electrolysis technologies in fossil-free steelmaking via the direct reduction of iron ore followed by processing in an electric arc furnace (EAF). Hydrogen (H2) production via low or high temperature electrolysis (LTE and HTE) is considered for the production of carbon-free direct reduced iron (DRI). The introduction of carbon into the DRI reduces the electricity demand of the EAF. Such carburization can be achieved by introducing carbon monoxide (CO) into the direct reduction process. Therefore, the production of mixtures of H2 and CO using either a combination of LTE coupled with a reverse water-gas shift reactor (rWGS-LTE) or high-temperature co-electrolysis (HTCE) was also investigated. The results show that HTE has the potential to reduce the specific electricity consumption (SEC) of liquid steel (LS) production by 21% compared to the LTE case. Nevertheless, due to the high investment cost of HTE units, both routes reach similar LS production costs of approximately 400 €/tonne LS. However, if future investment cost targets for HTE units are reached, a production cost of 301 €/tonne LS is attainable under the conditions given in this study. For the production of DRI containing carbon, a higher SEC is calculated for the LTE-rWGS system compared to HTCE (4.80 vs. 3.07 MWh/tonne LS). Although the use of HTCE or LTE-rWGS leads to similar LS production costs, future cost reduction of HTCE could result in a 10% reduction in LS production cost (418 vs. 375 €/tonne LS). We show that the use of HTE, either for the production of pure H2 or H2 and CO mixtures, may be advantageous compared to the use of LTE in H2-based steelmaking, although results are sensitive to electrolyzer investment costs, efficiencies, and electricity prices.

Supporting Conversion Section of Hydrogen Production Unit by Membrane Modules to Produce Extra-Pure Hydrogen and Improving Equilibrium Conversion

The main object of this research is the modification of an industrial hydrogen production unit with palladium-based membrane modules to produce extra-pure hydrogen and shift reactions toward the hydrogen production side. The considered hydrogen production unit includes steam reformer, high and low temperature shift converters, carbon dioxide absorption tower, and methanator. The membrane modules are applied in the catalytic reactors and hydrogen is simultaneously penetrated from the reaction zone toward the sweep gas. In the first step, both conventional and membrane-supported processes are heterogeneously models based on the mass and energy balance equations at steady state condition. Then, the simulation results of conventional process are compared with the plant data to prove the validity of the developed model. Finally, the simulation results of conventional and membrane-supported processes are compared under the same operating condition. In general, applying the membrane module on the system increases hydrogen production rate from 63.95 to 67.21 mole s-1. Based on the simulation results, supporting the conventional with the membrane module increases hydrogen production rate by 5.1%.

The unusual migratory aptitude in a case of α-carbonyl cation-driven 1,2-migration

Abstract α-Carbonyl cations were found to drive 1,2-carbon shift reactions with excellent selectivity. As opposed to traditional guidelines, this selectivity is based not on the electronic and steric properties of the migrating substituent but determined by the nature of the substituent remaining in the migrant carrying remnant. Therefore, the selectivity trend is reversed, which allowed us to realize a first example for a cation-driven selective migration favoring an alkynyl over an aryl substituent

Comparative assessment of renewable energy-based hydrogen production methods

Hydrogen is acknowledged as a potential fuel as it can be used as an energy carrier, a storage medium, in fuel cells and as a fuel as well and offers carbon-free solutions. This paper investigates three renewable energy based configurations for hydrogen production. The renewable energy sources considered in this study are solar PV, geothermal power generation and biomass gasification. The proposed study also presents a novel configuration of biomass gasification for hydrogen production via multistage water gas shift reactors. The solar PV and geothermal energy based hydrogen production systems are analysed employing the EES software while the hydrogen production system employing biomass gasification is simulated employing Aspen Plus. All three designed configurations are proceeded through numerous parametric analyses to investigate the system behavior and effect on system efficiencies. The hydrogen production using biomass gasification technique provides with the energetic and exergetic efficiencies of 53.6% and 49.8% and the efficiencies for the geothermal power generation based hydrogen production system are found to be 10.4% and 10.2% respectively. The exergetic and energetic efficiencies of hydrogen production system employing solar PV system are found to be 17.45% and 16.95%, respectively and the system is designed to produce 1.13 mol/s of hydrogen. Furthermore, the results of the parametric studies and sensitivity analyses are presented and discussed.

Thermo-economic analyses of isothermal water gas shift reactor integrations into IGCC power plant

Thermodynamic performance and economics of integrating three different types of isothermal water gas shift (WGS) reactors into integrated gasification combined cycle (IGCC) power plants have been analyzed and compared to an IGCC with adiabatic WGS reactors. Isothermal shifting has shown to shift the steam generation from intermediate pressure (IP) steam towards high pressure (HP) steam. More HP steam generation leads to increased power output of the Rankine cycle and ultimately increases efficiency. Another factor impacting the efficiency is the amount of shift steam added to the WGS reactor. By lowering the amount of shift steam needed, more power is generated by the Rankine cycle. Shift steam requirement is reduced at higher temperatures which is favorable for HP steam generation. Integrating an isothermal WGS reactor into an IGCC remains challenging in cases of high carbon capture as thermodynamic equilibrium favors CO conversion at lower temperatures. The relatively low cooling density when HP boiler feedwater is used in the isothermal reactor poses economic challenges as it increases reactor size and catalyst requirement. Using the Ro-number to optimize the isothermal WGS reactor offers the best economic results with reduced capital cost, operating cost and cost of electricity.

Progress through synergistic effects of heterojunction in nanocatalysts ‐ Review

AbstractThere are major advances in the development of the nanostructured materials to enhance the reaction performance in catalytic field. Recent efforts have shown that high conversion efficiency and stability of efficient nanocatalysts can be achieved by combining the intrinsic properties of single components into heterostructures. The unprecedented combination affords the integrated nanocatalysts capable of overcoming the limitations of single components and addressing the issues of the assessment of the efficiency of the catalytic converters. The present review gives a concise overview of the heterostructured nanoarchitectures with a focus of the tailoring of their structural geometry, self‐construction and surface chemistry to effectively create integrated catalysts with multi‐functionalities. The novel integrated catalysts present in the critical review were emphasized these concepts by undergoing inherent synergistic effects in their heterojunction structures to emerge superior catalytic performance and high selectivity for promising applications. Various types of the integrated nanocatalysts including coupled particles, porous composites, organized hybrids, assembled films, and biomimetic replicas are presented in respect to the discussion of expressive statements for widespread emerging applications in artificial photosynthesis, graphene‐based catalysts, electrochemical gas sensing, water‐gas shift reaction, and methane fuel generation.

Synthesis and highly efficient light-induced rearrangements of diphenylmethylene(2-benzo[b]thienyl)fulgides and fulgimides.

2-Benzo[b]thienyl fulgides and fulgimides containing bulky diphenylmethylene substituents were synthesized in the form of their ring-opened E- or Z-isomers. In contrast to the majority of known fulgides/fulgimides, that form colored ring-closed structures under UV irradiation, the obtained compounds undergo an irreversible transformation leading to decoloration of their solutions. This rearrangement with the formation of the dihydronaphthalene core appeared to be by 2–3 orders of magnitude more efficient than for the known diphenylmethylene(aryl(hetaryl))fulgides. The molecular structures of E- and Z-isomers and of products of the photoinduced rearrangement completed by 1,5-H shift reaction, 3a,4-dihydronaphtho[2,3-c]furans(pyrroles) C, were established based on the data of 1H and 13C NMR spectroscopy and X-ray diffraction studies.

Integration of gas switching combustion and membrane reactors for exceeding 50% efficiency in flexible IGCC plants with near-zero CO2 emissions

• Gas switching combustion and membrane reactors are integrated in an IGCC plant. • The proposed plants produce flexible electricity/H 2 with CCS to balance renewables. • IGCC benchmarks with/without CCS incorporate hot gas clean-up and H-class turbines. • Electric/H 2 LHV efficiencies up to 50.3%/62.4% with >98% CO 2 capture are achieved. • The energy penalty is less than 2%-points relative to the unabated IGCC plant. Thermal power plants face substantial challenges to remain competitive in energy systems with high shares of variable renewables, especially inflexible integrated gasification combined cycles (IGCC). This study addresses this challenge through the integration of Gas Switching Combustion (GSC) and Membrane Assisted Water Gas Shift (MAWGS) reactors in an IGCC plant for flexible electricity and/or H 2 production with inherent CO 2 capture. When electricity prices are high, H 2 from the MAWGS reactor is used for added firing after the GSC reactors to reach the high turbine inlet temperature of the H-class gas turbine. In periods of low electricity prices, the turbine operates at 10% of its rated power to satisfy the internal electricity demand, while a large portion of the syngas heating value is extracted as H 2 in the MAWGS reactor and sold to the market. This product flexibility allows the inflexible process units such as gasification, gas treating, air separation unit and CO 2 compression, transport, and storage to operate continuously, while the plant supplies variable power output. Two configurations of the GSC-MAWGS plant are presented. The base configuration achieves 47.2% electric efficiency and 56.6% equivalent hydrogen production efficiency with 94.8–95.6% CO 2 capture. An advanced scheme using the GSC reduction gases for coal-water slurry preheating and pre-gasification reached an electric efficiency of 50.3%, hydrogen efficiency of 62.4%, and CO 2 capture ratio of 98.1–99.5%. The efficiency is 8.4%-points higher than the pre-combustion CO 2 capture benchmark and only 1.9%-points below the unabated IGCC benchmark.

The effect of steam on air gasification of mechanically activated coal in a flow reactor

A combined steam-gas plant with in-cycle steam gasification of coal and hot gas purification is considered as a promising technology for increasing the efficiency of energy production with simultaneous reduction in environmental impact. To intensify steam-air gasification, mechanical activation of fuel is used; it consists in high-stress grinding in a mill-disintegrator. The supply of steam to the gasifier allows an increase in reactivity of fuel, suppression of sorbent decomposition in the unit of hot desulfurization, reduction in the steam load on the shift reactor, increase in useful external work of gas turbine expansion, reduction in nitrogen oxide formation, and general increase in the efficiency and ecological compatibility of energy generation. On the other hand, a significant amount of steam can deteriorate the heat balance and efficiency of the gasifier. In this work, the influence of the steam/fuel ratio on steam-air gasification of mechanically activated Kuznetsk coal in a flow reactor was studied experimentally. The excess air coefficient was maintained constant and equal to 0.51, which corresponded to a temperature at the reactor outlet of about 1100?C. When steam was supplied, the fuel and air-flow rates were adjusted to ensure a constant gas-dynamic regime. To evaluate the obtained regimes, the heat and material balances were compiled. A positive effect of steam on characteristics of the gasification process was revealed. For the studied coal, the maximum degree of coal conversion and the calorific value of synthesis gas are achieved with a steam/fuel ratio of about 0.4 kg/kg.

Opportunities and limitations for existing CHP plants to integrate polygeneration of drop-in biofuels with onsite hydrogen production

Over the past few years, there has been increasing research interest in retrofitting existing combined heat and power (CHP) plants with new technologies to co-produce other products. The focus has been on the design of fixed-sized processes for integration into CHP plants without affecting their performance. The primary objective of this study was to test the limits of a CHP plant with respect to retrofitting flexible thermochemical conversion of waste to drop-in biofuels with properties similar to petroleum fuels. Waste conversion to drop-in biofuels also requires significant amount of hydrogen for drop-in biofuels synthesis — Required hydrogen was also produced onsite in thermochemical processes integrated with CHP plant. The secondary objective was to determine the maximum number of days a flexible retrofitted waste-thermochemical process can run annually using only excess heat from a CHP plant, and whether such processes are profitable when operating flexibly. The results show that the selection of heat extraction points for the utilization of excess heat from the CHP plant for energy-intensive processes is critical for maintaining the flexibility of the integrated thermochemical processes. Thermochemical processes integrated with CHP plants were able to operate on approximately 180 days of the year by utilizing only excess heat from the CHP plant. Integration of pyrolysis showed more flexibility than integration of gasification. Onsite hydrogen production was the main limiting factor for the integration of thermochemical process with the existing CHP plant to produce drop-in biofuels. Hydrogen produced with a solid oxide electrolysis cell (SOEC) decreased the overall system efficiency and limited the capacity of the overall process. However, hydrogen production from a water gas shift (WGS) reactor was more expensive. The results also indicated that small changes in the financial parameters have a large impact on the economic performance of the integrated process.

Methanol Synthesis at a Wide Range of H2/CO2 Ratios over a Rh‐In Bimetallic Catalyst

AbstractThere is increasing interest in capturing H2 generated from renewables with CO2 to produce methanol. However, renewable hydrogen production is expensive and in limited quantity compared to CO2. Excess CO2 and limited H2 in the feedstock gas is not favorable for CO2 hydrogenation to methanol, causing low activity and poor methanol selectivity. Now, a class of Rh‐In catalysts with optimal adsorption properties to the intermediates of methanol production is presented. The Rh‐In catalyst can effectively catalyze methanol synthesis but inhibit the reverse water‐gas shift reaction under H2‐deficient gas flow and shows the best competitive methanol productivity under industrially applicable conditions in comparison with reported values. This work demonstrates a strong potential of Rh‐In bimetallic composition, from which a convenient methanol synthesis based on flexible feedstock compositions (such as H2/CO2 from biomass derivatives) with lower energy cost can be established.

Compact Heat Integrated Reactor System of Steam Reformer, Shift Reactor and Combustor for Hydrogen Production from Ethanol

A compact heat integrated reactor system (CHIRS) of a steam reformer, a water gas shift reactor, and a combustor were designed for stationary hydrogen production from ethanol. Different reactor integration concepts were firstly studied using Aspen Plus. The sequential steam reformer and shift reactor (SRSR) was considered as a conventional system. The efficiency of the SRSR could be improved by more than 12% by splitting water addition to the shift reactor (SRSR-WS). Two compact heat integrated reactor systems (CHIRS) were proposed and simulated by using COMSOL Multiphysics software. Although the overall efficiency of the CHIRS was quite a bit lower than the SRSR-WS, the compact systems were properly designed for portable use. CHIRS (I) design, combining the reactors in a radial direction, was large in reactor volume and provided poor temperature control. As a result, the ethanol steam reforming and water gas shift reactions were suppressed, leading to lower hydrogen selectivity. On the other hand, CHIRS (II) design, combining the process in a vertical direction, provided better temperature control. The reactions performed efficiently, resulting in higher hydrogen selectivity. Therefore, the high performance CHIRS (II) design is recommended as a suitable stationary system for hydrogen production from ethanol.

A high‐efficiency novel IGCC‐OTM carbon capture power plant design

AbstractCoal power plants play an important role in supplying affordable and reliable electricity. It is necessary to develop high‐efficiency and low‐cost carbon capture (CC) technologies to mitigate the associated global warming. Using H2S‐tolerant oxygen transport membranes (OTMs) for hydrogen production and CO2 separation can significantly reduce the energy penalty of CC in integrated gasification combined cycle (IGCC) power plants. We carried out system‐level analysis to investigate a novel IGCC‐CC power plant design using OTMs. We studied the impacts of various operating parameters on the overall efficiency and energy penalty. This novel IGCC‐OTM system has an overall efficiency 3.2%‐point lower than the same system without CC, much lower than the IGCC with water‐gas shift reactors and acid gas removal units (IGCC‐WGS) of 6.8%‐point drop. The specific primary energy consumption for CO2 avoided (SPECCA) of this novel technology is 1.08 MJ kgCO2−1, which is 59.4% lower than that of the IGCC‐WGS.