Performance analysis of the cold flow model of a second generation chemical looping combustion reactor system

Bischi, Aldo; Langørgen, Øyvind; Morin, Jean-Xavier; Bakken, Jørn; Ghorbaniyan, Masoud; Bysveen, Marie; Bolland, Olav

doi:10.1016/j.egypro.2011.01.074

Cited by 18 publications

(4 citation statements)

References 13 publications

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“…It has been extensively applied for obtaining dynamic ation of powder flow in a very wide variety of processes. repared and is incorporated into the tracer by an anion-subn surface adsorption procedure [21,22]. The tracer is loby triangulation of a number of detected annihilation and this every 4 ms, thus providing trajectory and velocity ation.…”

Section: Rimental Set-up Procedures and Illustration Of Resultsmentioning

confidence: 99%

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Pressurised Chemical Looping Combustion (PCLC): Air Reactor design

Bartocci

Bidini

Abad

et al. 2022

J. Phys.: Conf. Ser.

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Bioenergy combustion with Carbon Capture and Storage (BECCS) is a key technology to achieve carbon negative emissions power generation. This can be achieved by coupling the biofuels combustion with CO2 capture and storage (CCS). The lowest cost for CCS corresponds at the moment to the Chemical Looping Combustion (CLC) process. This can use biofuels which can be gaseous (biomethane, biogas or syngas etc.), liquid (biodiesel, bioethanol, biobutanol and pyrolysis oils etc.) or solids (wood dust, charcoal dust, wood chips, wood pellets etc.) While plant design with gaseous and liquid biofuels would be simpler, plants using solid biofuels and based on two couple fluidisd beds would need the use of a third reactor named carbon stripper. In the specific case if we plan to couple a CLC plant with a turbo expander (to achieve the high efficiencies of a combined cycle power plant) we have to work with pressurized reactors. However, there are some technical barriers to the coupling of a chemical looping combustor with a turbo expander, such as: the operation of the combustor in pressurised conditions; the inventory balance among reactors; elutriated particles reaching the turbo expander. This explaind why there is no commercial plant at the moment capable to do this. The aim of this paper is to present a model for the dimensioning of an air reactor to be coupled to a turbo expander of the power of about 12 MWe. Based on this, the air mass flow can be obtained and the geometric parameters can be calculated, to have an air velocity which is needed to achieve the fast fluidization regime and to ensure a high conversion rate as well as particles and heat exchage among air and fuel reactor.

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Section: Rimental Set-up Procedures and Illustration Of Resultsmentioning

confidence: 99%

“…Many review papers have already dealt with several aspects of chemical looping, see for example [15,[17][18][19][20][21]. Reactor optimisaztion has been performed and studied in [22][23][24]. There is also a recent interest on pressurized chemical looping as reported in [25].…”

Section: Introductionmentioning

confidence: 99%

Pressurised Chemical Looping Combustion (PCLC): Air Reactor design

Bartocci

Bidini

Abad

et al. 2022

J. Phys.: Conf. Ser.

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“…With this fast mode of fluid bed operation, it is necessary to reduce the possible gas/particle wall friction effects, which may have been unavoidable had the model been decreased in scale. This approach of “like‐for‐like” scaling has been successfully employed previously by Bischi et al …”

Section: Methodsmentioning

confidence: 99%

“…Cold-flowm odel design Cold-flow model reactors are typically reduced in size compared to the larger reactors,w hich they aim to simulate based on Glicksmansd imensionless scaling laws.T he CFM described in this investigation is of 1:1s cale to the Cranfield CLC fast-bed design. With this fast mode of fluid bed operation, it is necessary to reduce the possible gas/particle wall friction effects,w hich may have been unavoidable had the model been decreased in scale.T his approach of "like-for-like" scaling has been successfully employed previously by Bischi et al [29,30] With the requirement for a1 :1 CFM plus the constraint of air being used as the fluidizing gas at this scale,i twasn ecessary to satisfy other dynamically similar properties in Glicksmanss implified scaling laws.T he conditions of the CLC unit with CFM are detailed in Table 2. Them ajor parameters that were used to simulate similar dynamic properties between the two systems were the particle density and particle diameter.…”

Section: Methodsmentioning

confidence: 99%

A Hydrodynamic Study of a Fast‐Bed Dual Circulating Fluidized Bed for Chemical Looping Combustion

et al. 2016

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This study explores the use of a dual interconnected circulating fluidized bed (CFB) for chemical looping combustion. This design can enhance gas–solid interactions, but it is difficult to control the solid transfer and circulation rates. With the use of a 1:1 scale cold‐flow model, an investigation determining the hydrodynamic behavior of the dual CFB system has been conducted. The cold‐flow system consists of two identical fast‐bed risers, each with an internal diameter of 100 mm and a height of 7 m. The simplified cold‐flow model is based on the chemical looping Pilot‐Scale Advanced CO2 Capture Technology (PACT) facility at Cranfield. Here, we have determined the minimum fluidization and transport velocities, and we have assessed the solid density profiles, transport capacity, and potential for the dilution by air/N2 leakage into the CO2 stream exiting the fuel reactor. The experimental procedure uses two different bed materials, molochite (ceramic clay) and FE100 (iron particles), and it satisfies the dynamic scaling laws to model the bed inventory within the system. The results indicate that the two fast‐bed risers share similar density and pressure profiles. Stable circulation can be achieved through pneumatic transport. The circulation rate of the system is flexible and can be adjusted by altering the fluidization velocity in the riser and by altering the bed inventory. The gas leakage from the loop seal to the cyclone was found to be sensitive to the bed height and fluidization velocity in the loop seal. However, by maintaining a loop‐seal bed height above 600 mm during operation, the outlet stream remains undiluted.

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