Enhanced hydrogen production from biomass with in situ carbon dioxide capture using calcium oxide sorbents

Florin, Nick; Harris, Andrew T.

doi:10.1016/j.ces.2007.09.011

Cited by 425 publications

(274 citation statements)

References 112 publications

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“…(8) strongly depends on the process temperature at atmospheric conditions. The CO 2 capture takes place between 450 °C to 750 °C (Florin and Harris, 2008). Above 750 °C, CO 2 can not be captured whereas at a temperature above 800 °C CaCO 3 is regenerated to CaO, while CO 2 is released.…”

Section: Absorption Enhanced Reforming (Aer)mentioning

confidence: 99%

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Experimental investigation of the absorption enhanced reforming of biomass in a 20 kWth dual fluidized bed system

Poboss¹

2012

Int. J. Thermo

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A gasification product gas with a hydrogen content over 75 vol-% db and a heating value of 15 MJ/m³ STP,db has been obtained through the absorption enhanced reforming of biomass. The Absorption Enhanced Reforming (AER) process involves a Dual Fluidized Bed (DFB) system consisting of a gasifier and a regenerator (calciner). In the DFB system, the Ca -looping ratio is an important parameter defined as the ratio of the molar flow rate of regenerated sorbent (F Ca ) and carbon (F c ) which enters the gasifier as fuel. A special feature of the 20 kW th DFB test facility at IFK is the Ca -looping rate control through a cone valve. Therefore, the Ca -looping ratio (F Ca /F C ) was varied between a value of 2 and 12 mol CaO /mol C to investigate its influence on the cold gas efficiency, product gas yield, yield of gas components and gravimetric tar concentration during the AER of biomass. The experiments were carried out with wood pellets and a Greek limestone as CO 2 sorbent. The experimental work shows a clear influence of the Ca -looping ratio on the AER process. It shows also that beyond a certain value of this parameter, the tar and gas composition is stabilized.

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Section: Absorption Enhanced Reforming (Aer)mentioning

confidence: 99%

“…Based on this principle a 9 MW th CHP DFB gasifier was constructed in 2009 in Oberwart (Neues Biomassekraftwerk Oberwart, 2009 (Florin, Harris, 2008;Higman, van der Burgt, 2003).…”

Section: Introduction 1dual Fluidized Bed Biomass Steam Gasificationmentioning

confidence: 99%

Experimental investigation of the absorption enhanced reforming of biomass in a 20 kWth dual fluidized bed system

Poboss¹

2012

Int. J. Thermo

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“…Reduction of tar formation can be achieved by different ways such as varying the operating conditions, adding catalysts to the feedstock, mechanical cleaning of cold gas and using secondary catalytic bed to decompose tar into gas products (Anisa et al, 2011). In the case of using secondary catalytic bed, many type of catalysts were studied (Hu et al, 2006;Florin and Harris, 2008;Kimure et al, 2006). Iron based catalysts are widely used to decompose of tar (Min et al, 2011;Uddin et al 2008;Khelfa et al, 2009;Hurley et al, 2012;Xie et al, 2009;Tang et al, 2010;Xiwei et al, 2012).…”

Section: Introductionmentioning

confidence: 99%

Hydrogen production from algal biomass via steam gasification

Duman

Uddin

Yanık

2014

Bioresource Technology

168

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Algal biomasses were tested as feedstock for steam gasification in a dual-bed microreactor in a two-stage process. Gasification experiments were carried out in absence and presence of catalyst. The catalysts used were 10% Fe2O3-90% CeO2 and red mud (activated and natural forms). Effects of catalysts on tar formation and gasification efficiencies were comparatively investigated. It was observed that the characteristic of algae gasification was dependent on its components and the catalysts used. The main role of the catalyst was reforming of the tar derived from algae pyrolysis, besides enhancing water gas shift reaction. The tar reduction levels were in the range of 80-100% for seaweeds and of 53-70% for microalgae. Fe2O3-CeO2 was found to be the most effective catalyst. The maximum hydrogen yields obtained were 1036cc/g algae for Fucus serratus, 937cc/g algae for Laminaria digitata and 413cc/g algae for Nannochloropsis oculata.FP7 Marie-Curie IAPP-Project (230598

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“…As principais diferenças são sumarizadas a seguir. 7,8,12 O leito fluidizado, dependendo do regime de fluidização, pode ser do tipo borbulhante ou circulante. Esse tipo de gaseificador opera com as seguintes condições típicas: tempo de residência de 1 min, temperatura igual a 800-1000 °C, o material deve ter granulometria uniforme (10-100 mm), com teor de umidade menor que 40% e de cinzas menor que 20%, no entanto o ponto de fusão das cinzas da biomassa deve ser superior a 1000 °C.…”

Section: Tipos De Gaseificadoresunclassified

Tar Removal From Biomass Gasification Streams: Processes and Catalysts

Quitete¹,

Souza²

2014

Química Nova

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Enhanced hydrogen production from biomass with in situ carbon dioxide capture using calcium oxide sorbents

Cited by 425 publications

References 112 publications

Experimental investigation of the absorption enhanced reforming of biomass in a 20 kWth dual fluidized bed system

Experimental investigation of the absorption enhanced reforming of biomass in a 20 kWth dual fluidized bed system

Hydrogen production from algal biomass via steam gasification

Tar Removal From Biomass Gasification Streams: Processes and Catalysts

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