Biomass chemical looping gasification for syngas production using LD Slag as oxygen carrier in a 1.5 kWth unit

Condori, Óscar; Garcı́a-Labiano, F.; Diego, Luis F. de; Izquierdo, M.T.; Adánez, Juan

doi:10.1016/j.fuproc.2021.106963

Cited by 47 publications

(47 citation statements)

References 28 publications

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“…BCLG studies carried out with other oxygen carriers found the same decreasing tendency with the temperature, reaching values of around 1.5–3.7 g/Nm 3 for ilmenite and 2.3–3.5 g/Nm 3 for LD slag under similar conditions. 12 , 45 In contrast, it was observed that an increase in the S/B ratio led to an increase in the amount of tars generated using ilmenite.…”

Section: Resultsmentioning

confidence: 98%

Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

et al. 2021

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Biomass chemical looping gasification (BCLG) uses lattice oxygen from an oxygen carrier instead of gaseous oxygen for high-quality syngas production without CO 2 emissions. In this work, the effect of the main operating variables, such as oxygen/biomass ratio (λ), gasification temperature, and steam/biomass ratio (S/B), was investigated using two low-cost materials: a Fe ore and a Mn ore. Oxygen fed to the air reactor for oxidation was used as an effective method for controlling the amount of lattice oxygen used for syngas production. The main variable that affected the process performance and the syngas quality was λ, while the fuel reactor temperature and the S/B ratio had a minor effect. Small performance differences found between the ores can be attributed to different degrees of CH 4 and light hydrocarbons reforming in the process. The CO 2 content in the syngas was high (40 −43%) under autothermal conditions because the gasification reactions required the heat to be generated by combustion. CH 4 contents of around 10% were found in syngas, coming from the unburned or unreformed volatiles. Syngas yields around 0.60 Nm 3 /kg of dry biomass were found for both ores. Additionally, high biomass conversions ( X b > 94%) and carbon conversion efficiencies (η cc > 95%) were obtained in all cases, showing the capability of the process of avoiding CO 2 emissions to the atmosphere. No agglomeration was found in the bed during the BCLG process, although attrition rates were high, leading to lifetimes of 160 and 300 h for the manganese and iron ores, respectively. Migration of Fe or Mn to the external part of the particle, generating a metal concentrated shell, was observed. Its detachment was responsible for the decrease in the oxygen transport capacity ( R OC ) of the material with the operating time and the reduced lifetime. The results obtained here allowed the iron ore to be considered as an oxygen carrier suitable for the BCLG process.

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Section: Resultsmentioning

confidence: 98%

Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

et al. 2021

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“…Lifetimes between 160 and 630 h have been reported. 13 , 15 , 16 In addition, high amounts of CH 4 (5–15 vol %) and light hydrocarbons, such as C 2 H 6 and C 3 H 8 (0.1–3.7 vol %), appeared in the syngas. 13 , 15 − 18 Despite their higher costs, synthetic materials have also been proposed to improve some properties, such as lifetime.…”

Section: Introductionmentioning

confidence: 99%

Influence of an Oxygen Carrier on the CH₄ Reforming Reaction Linked to the Biomass Chemical Looping Gasification Process

et al. 2022

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A major challenge in biomass chemical looping gasification (BCLG) is the conversion of CH 4 and light hydrocarbons to syngas (CO + H 2 ) when the goal is the use for bioliquid fuel production. In this work, tests were performed in a batch fluidized bed reactor to determine the catalytic effect on the CH 4 reforming reaction of oxygen carriers used in the BCLG process. Three ores (ilmenite, MnGB, and Tierga), one waste (LD slag), and five synthetic materials (Fe10Al, Fe20Al, Fe25Al, Cu14Al, and Ni18Al) were analyzed. These results were compared to those obtained during ∼300 h of continuous biomass gasification operation in a 1.5 kW th BCLG unit. The low-cost materials (ores and waste) did not show any catalytic effect in the CH 4 reforming reaction, and as a consequence, the CH 4 concentration values measured in the syngas produced in the continuous prototype were high. The synthetic oxygen carriers showed a catalytic effect in the CH 4 reforming reaction, increasing this effect with increasing temperature. With the exception of the Ni-based oxygen carrier (used as a reference), the Cu-based oxygen carrier, working at 940 °C, showed the best catalytic properties, in good agreement with the low CH 4 concentration values measured in the syngas generated in the continuous unit. The tests performed in a batch fluidized bed reactor were demonstrated to be very useful in determining the catalytic capacity of oxygen carriers in the CH 4 reforming reaction. This fact is highly relevant when a syngas with a low CH 4 content is desired as a final product.

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“…CLG operation in the 10 kW Chalmers unit with high-volatile fuel, such as white wood pellets and black wood pellets with LD slag as the OC was investigated by Moldenhauer et al, 17 where the estimated raw gas composition mainly comprised of H 2 , CO 2 , CO, and CH 4 in that order. In a more recently published work by Condori et al, 18 CLG Energy & Fuels pubs.acs.org/EF Article experiments were performed on industrial wood pellets and other agricultural wastes in a 1.5 kW th unit with LD slag, where gas compositions were estimated for different operating conditions (varied temperatures, steam/biomass ratios, and oxygen/biomass ratios and different gasification agents). Here, with steam as the gasification agent, the reported gas compositions (vol %, dry and N 2 -free basis) were in a wide range of H 2 (25−40%), CO 2 (20−46%), CO (18−40%), and CH 4 (8−9%), indicating the influence of different operating conditions.…”

Section: Clgmentioning

confidence: 99%

“…In case CG, with the restriction on iron oxide reduction to the Fe 2 O 3 /Fe 3 O 4 oxide couple, the model predicts a maximum oxygen transport capacity of 0.963%, and this is comparable to the maximum oxygen transport capacity of 1.12% for LD slag reported in the literature. 40 Further, the model is validated with a more recent experimental study on CLG of industrial wood pellets (IWP) with LD slag as the OC in a 1.5 kW th unit performed by Condori et al 18 Here, the tests were performed for different gasification agents (steam and CO 2 ), wide-ranging S/B ratios, and oxygen/fuel ratios (λ) to investigate the effect on raw gas compositions. The gas compositions reported for the closest operational conditions (test 11 18 performed with a S/B ratio of 0.58 and λ of 0.27) with the modeled CLG model are considered for model validation.…”

Section: Energy and Fuels Pubsacsorg/ef Articlementioning

confidence: 99%

“…In addition to this, LD slag has a high calcium content that could favor WGS activity in the FR . It is estimated to have a maximum oxygen transport capacity (OTC) of 1.12% by weight. , Condori et al also reported an OTC of 1.2% for used LD slag after 60 h of operation, and 1.8% for unused or fresh LD slag. In cases CG and HG, the active species assumed in LD slag is hematite that is restricted to Fe 2 O 3 /Fe 3 O 4 oxide couple, owing to the thermodynamic limitation on its reduction. − Both cases are described in more detail in the following section.…”

Section: Case Descriptionmentioning

confidence: 99%

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Process Analysis of Chemical Looping Gasification of Biomass for Fischer–Tropsch Crude Production with Net-Negative CO₂ Emissions: Part 1

et al. 2022

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Large-scale biofuel production plants require an efficient gasification process that generates syngas of high quality (with minimal gas contaminants and inert gases) to minimize the extent of the syngas cleaning processes required for liquid biofuel production. This work presents process modeling of the chemical looping gasification (CLG) process for syngas production. The CLG process is integrated with a Fischer−Tropsch synthesis (FTS) process to produce Fischer−Tropsch (FT) crude with net-negative CO 2 emissions, enabling process and system-level analyses of this novel biomass-to-liquid process. CLG resembles indirect gasification in an interconnected circulating fluidized bed reactor, where instead of inert bed material, a solid-oxygen carrier, such as mineral ores rich in iron or manganese oxides, is used. The oxygen carrier particles undergo oxidation and reduction in the air reactor and fuel reactor, respectively, thereby providing heat and oxygen for gasification. This work uses data from CLG experiments performed with steel converter slag as the oxygen carrier and investigates its potential when integrated with different downstream gas cleaning trains and the subsequent fuel synthesis process with the primary objective of quantifying and evaluating the performance of the integrated CLG−FT process plant. Syngas with a high energy content of 12 MJ/Nm 3 (lower heating value basis) is predicted with a cold gas efficiency of 73%. CO 2 /CO ratios, higher than indirect biomass gasification, are also predicted in the raw syngas produced; thus, there exists an opportunity to capture biogenic CO 2 with a relatively lower energy penalty in the subsequent gas cleaning stages. This work quantifies other key performance indicators, such as heat recovery potential, negative CO 2 emission capacity, and FT crude production efficiency of the CLG−FT plant. A 100 MW th CLG plant produces roughly 677−696 barrels per day of FT crude, with net-negative emissions of roughly 180 kilotonnes of CO 2 annually.

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Biomass chemical looping gasification for syngas production using LD Slag as oxygen carrier in a 1.5 kWth unit

Cited by 47 publications

References 28 publications

Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Influence of an Oxygen Carrier on the CH₄ Reforming Reaction Linked to the Biomass Chemical Looping Gasification Process

Process Analysis of Chemical Looping Gasification of Biomass for Fischer–Tropsch Crude Production with Net-Negative CO₂ Emissions: Part 1

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Biomass chemical looping gasification for syngas production using LD Slag as oxygen carrier in a 1.5 kWth unit

Cited by 47 publications

References 28 publications

Syngas Production in a 1.5 kWth Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Syngas Production in a 1.5 kWth Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Influence of an Oxygen Carrier on the CH4 Reforming Reaction Linked to the Biomass Chemical Looping Gasification Process

Process Analysis of Chemical Looping Gasification of Biomass for Fischer–Tropsch Crude Production with Net-Negative CO2 Emissions: Part 1

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Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Syngas Production in a 1.5 kW_th Biomass Chemical Looping Gasification Unit Using Fe and Mn Ores as the Oxygen Carrier

Influence of an Oxygen Carrier on the CH₄ Reforming Reaction Linked to the Biomass Chemical Looping Gasification Process

Process Analysis of Chemical Looping Gasification of Biomass for Fischer–Tropsch Crude Production with Net-Negative CO₂ Emissions: Part 1