Energy analysis of two stage packed-bed chemical looping combustion configurations for integrated gasification combined cycles

Hamers, H.P.; Romano, Matteo Carmelo; Spallina, Vincenzo; Chiesa, Paolo; Gallucci, Fausto; Annaland, Martin van Sint

doi:10.1016/j.energy.2015.03.063

Cited by 36 publications

(19 citation statements)

References 28 publications

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“…The most expensive component of reactor network is the high-temperature valve. This was expected, since, due to the presence of cheap sorbent (CaCO3), the impact of the solid material is not as significant as in similar reforming applications [23] in which only highly expensive Ni catalyst is used. Levelised cost of H2 (LCOH) 0.049 €kWh -1 Cost of CO2 avoided (ACs1) 29.85 €tCO2 -1 The cost of hydrogen for the SMR process without CO2 capture (LCOHref) reported in Table 5 was evaluated from [29].…”

Section: Resultsmentioning

confidence: 99%

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Hanak

Bareschino

Mancusi

et al. 2017

Journal of Power Sources

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Sorption-enhanced steam methane reforming (SE-SMR) is a promising alternative for H2 production with inherent CO2 capture. This study evaluates the techno-economic performance of SE-SMR in a network of fixed beds and its integration with a solid oxide fuel cell (SE-SMR-SOFC) for power generation. The analysis revealed that both proposed systems are characterised by better economic performance than the reference systems. In particular, for SE-SMR the levelised cost of hydrogen is 1.6 €⋅kg−1 and the cost of CO2 avoided is 29.9 €⋅tCO2−1 (2.4 €⋅kg−1 and 50 €⋅tCO2−1, respectively, for SMR with CO2 capture) while for SE-SMR-SOFC the levelised cost of electricity is 0.078 €⋅kWh−1 and the cost of CO2 avoided is 36.9 €⋅tCO2−1 (0.080 €⋅kWh−1 and 80 €⋅tCO2−1, respectively, for natural gas-fired power plant with carbon capture). The sensitivity analysis showed that the specific cost of fuel and the capital cost of fuel cell mainly affect the economic performance of SE-SMR and SE-SMR-SOFC, respectively. The daily revenue of the SE-SMR-SOFC system is higher than that of the natural gas-fired power plant if the difference between the carbon tax and the CO2 transport and storage cost is > 6 €⋅tCO2−1

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Section: Resultsmentioning

confidence: 99%

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Hanak

Bareschino

Mancusi

et al. 2017

Journal of Power Sources

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“…A.2. Specific cost of refractory, screfr 0.45 € kg -1 [72] Specific cost of sorbent, scCaO 0.02 € kg -1 [73] Specific cost of oxygen carrier, scCu 6 € kg -1 [73] Specific cost of catalyst, scNi 50 € kg -1 [72] Specific cost of inert, scAl2O3(NiO) 1 € kg -1 [73] Specific cost of heat exchanger/condenser, scHE/cond 241 € m -2 [70] Specific cost of hydrogen buffer, scbuffer 1,200 € m -3 [74] Specific cost of boiler, scB 150 € kW -1 [75] Specific cost of MCHP, scMCHP 2,500 € kW -1 [65] Specific cost of EHP, scEHP 500 € kW -1 [75] Unit price of natural gas, UPNG 0.013 € kWh -1 [76] Unit price of methane, UPCH4 0.019 € kWh -1 [76] Unit price of electric energy, UPee 0.1 € kWh -1 [77] Maintenance cost of boiler, MB 0.20 € h -1 [75] Maintenance cost of MCHP, MMCHP 0.20 € h -1 [75] Maintenance cost of EHP, MEHP 0.05 € h -1 [75] Maintenance cost of the proposed system, Mps 2% of TCRps per annum [76] CO2 transport and storage cost, CTS 82 € tCO2 -1 [78]…”

Section: A1 Energy and Environmental Analysismentioning

confidence: 99%

Feasibility of CaO/CuO/NiO sorption-enhanced steam methane reforming integrated with solid-oxide fuel cell for near-zero-CO2 emissions cogeneration system

et al. 2018

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In this article, a process for sorption-enhanced steam methane reforming in an adiabatic fixedbed reactor coupled with a solid oxide fuel cell (SOFC) is evaluated using a 1D numerical reactor model combined with a simplified fuel cell simulation. A novel material comprising CaO/CuO/Al2O3(NiO) pellets is considered. Three operating stages are considered in the proposed system, namely (i) CaO carbonation/reforming, (ii) Cu and Ni oxidation, and (iii) CaCO3 calcination/CuO and NiO reduction. The operating conditions that enable cyclic operation of these stages and the strategy needed to switch between each stage are evaluated. Under the adopted control strategy, methane conversion was about 95%, whilst H2 yield and purity were around 3.2 molH2 molCH4-1 and 90%, respectively. Moreover, a concentrated CO2 stream ready for storage was obtained. By using a portion of the produced H2 to make the process self-sufficient from an energy standpoint, an equivalent H2 yield and a reforming efficiency of about 2.8 molH2 molCH4-1 and 84% were achieved, respectively. With respect to SOFC integration, net power and thermal energy generation of around 11 kW and 6 kW, respectively, can be achieved. With respect to the chemical energy of the inlet methane, the net electrical and thermal efficiencies of the considered process are 56% and 30%, respectively, i.e., the overall efficiency of the entire system is 86%. The proposed cogeneration system showed better thermodynamic, environmental and economic performances than those of conventional systems, with an investment pay-back period of 2.2 years in the worst-case scenario. The levelised cost of electricity, of heat and total power were about 0.096 € kWh-1 , 0.19 € kWh-1 , and 0.065 € kWh-1 , respectively, while the CO2 emissions were avoided at no cost.

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“…The technologies for converting CO 2 emission and CH 4 to value‐added products such as chemical fuels (H 2 , syngas, liquid fuels) have a great potential for addressing the major challenges for sustainable development. Unlike conventional methods for CO 2 emission control, the chemical looping combustion (CLC) technology has been considered a low‐cost carbon capture and storage option . However, CLC does not provide enough understanding regarding the sustainable utilization of CO 2 in chemical fuels.…”

Section: Introductionmentioning

confidence: 99%

Analysis of Two‐Step Solar Thermochemical Looping Reforming of Fe₃O₄ Redox Cycles for Synthesis Gas Production

et al. 2019

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A two‐step solar thermochemical looping reforming (STCLR) of CH4—Fe3O4 redox cycles via H2O and CO2 splitting is investigated for H2 and CO production. The P1 approximation is adopted for the radiation heat transfer and high‐temperature thermal characteristics of active materials in the reaction medium. A benchmark experimental setup for the conversion of solar energy to syngas based on the solar thermochemical technology is presented. The effects of operating conditions on the yield of H2 and CO as well as syngas production are investigated at both thermal reduction and oxidation steps. It is found that the key performance of two‐step CH4—Fe3O4 redox cycles for a higher H2 and CO production depends on the efficiency of methane and oxidizer (H2O and CO2) conversion. Furthermore, a substantial amount of H2 and CO production with carbon deposition is obtained when the thermal reduction is extended to the mixed oxide solid solution (FeO—Fe). Among the oxygen carriers, FeO exhibits a higher oxygen exchange for H2 production. However, the synergetic effect of FeO—Fe reactivity strongly contributes to syngas yield. The present solar reactor model can significantly contribute to the reduction of greenhouse gas emission by utilizing 40% of CO2 emissions into solar fuels such as H2 and syngas. The results indicate that highly selective syngas with an H2/CO ratio close to 2 can be obtained with a strong control of γ = H2O/CO2.

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Energy analysis of two stage packed-bed chemical looping combustion configurations for integrated gasification combined cycles

Cited by 36 publications

References 28 publications

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Feasibility of CaO/CuO/NiO sorption-enhanced steam methane reforming integrated with solid-oxide fuel cell for near-zero-CO2 emissions cogeneration system

Analysis of Two‐Step Solar Thermochemical Looping Reforming of Fe₃O₄ Redox Cycles for Synthesis Gas Production

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Energy analysis of two stage packed-bed chemical looping combustion configurations for integrated gasification combined cycles

Cited by 36 publications

References 28 publications

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Techno-economic analysis of sorption-enhanced steam methane reforming in a fixed bed reactor network integrated with fuel cell

Feasibility of CaO/CuO/NiO sorption-enhanced steam methane reforming integrated with solid-oxide fuel cell for near-zero-CO2 emissions cogeneration system

Analysis of Two‐Step Solar Thermochemical Looping Reforming of Fe3O4 Redox Cycles for Synthesis Gas Production

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Analysis of Two‐Step Solar Thermochemical Looping Reforming of Fe₃O₄ Redox Cycles for Synthesis Gas Production