Performance of UASB reactors in two stages followed by post-treatment with activated sludge in wastewater batch of wet-processed coffee

In this study it was evaluated the efficiency of the treatment of wet-processed coffee wastewater in upflow anaerobic sludge blanket (UASB) reactors in two stages, in bench scale, followed by post-treatment with activated sludge in batch. The first UASB reactor was submitted to an hydraulic retention time (HRT) of 6.2 d and organic loading rates (OLR) of 2.3 and 4.5g CODtotal (L d)-1, and the second UASB reactor to HRT of 3.1 d with OLR of 0.4 and 1.4g CODtotal (L d)-1. The average values of the affluent CODtotal increased from 13,891 to 27,926mg L-1 and the average efficiencies of removal of the CODtotal decreased from 95 to 91%, respectively, in the UASB reactors in two stages. The volumetric methane production increased from 0.274 to 0.323L CH4 (L reactor d)-1 with increment in the OLR. The average concentrations of total phenols in the affluent were of 48 and 163mg L-1, and the removal efficiencies in the UASB reactors in two stages of 92 and 90%, respectively, and increased to 97% with post-treatment. The average values of the removal efficiencies of total nitrogen and phosphorus were of 57 to 80% and 44 to 60%, respectively, in the UASB reactors in two stages and increased to 91 and 84% with the post-treatment.

Analysis of a microbial community associated with polychlorinated biphenyl degradation in anaerobic batch reactors

The degradation of polychlorinated biphenyls (PCBs) was investigated under fermentativemethanogenic conditions for up to 60 days in the presence of anaerobic biomass from a full-scale UASB reactor. The low methane yields in the PCBs-spiked batch reactors suggested that the biomass had an inhibitory effect on the methanogenic community. Reactors containing PCBs and co-substrates (ethanol/ sodium formate) exhibited substantial PCB reductions from 0.7 to 0.2 mg mL-1 . For the Bacteria domain, the PCBs-spiked reactors were grouped with the PCB-free reactors with a similarity of 55 %, which suggested the selection of a specific population in the presence of PCBs. Three genera of bacteria were found exclusively in the PCB-spiked reactors and were identified using pyrosequencing analysis, Sedimentibacter, Tissierela and Fusibacter. Interestingly, the Sedimentibacter, which was previously correlated with the reductive dechlorination of PCBs, had the highest relative abundance in the RCS-PCB (7.4 %) and RCS-PCB-PF (12.4 %) reactors. Thus, the anaerobic sludge from the UASB reactor contains bacteria from the Firmicutes phylum that are capable of degrading PCBs.

Performance evaluation and phylogenetic characterization of anaerobic fluidized bed reactors using ground tire and pet as support materials for biohydrogen production

Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq)

Performance and composition of bacterial communiies in anaerobic fluidized bed reactors for hydrogen production: Effects of organic loading rate and alkalinity

Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq)

Electrochemical oxidation of landfill leachate in a flow reactor: optimization using response surface methodology

Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq)

Synthesis of Structured Lipids by Enzymatic Interesterification of Milkfat and Soybean Oil in a Basket-Type Stirred Tank Reactor

Fundação de Amparo à Pesquisa do Estado de São Paulo (FAPESP)

Combustion of coal, bagasse and blends thereof Part I: Emissions from batch combustion of fixed beds of fuels

Batch combustion of fixed beds of coal, bagasse and blends thereof took place in a pre-heated two-stage electric laboratory furnace, under high-heating rates. The average input fuel/air equivalence ratios were similar for all fuels. The primary and secondary furnace temperatures were varied from 800 degrees C to 1000 degrees C. The effects of fuel blending, combustion staging, and operating furnace temperatures on the emissions from the two fuels were assessed. Furnace effluents were analyzed for carbon dioxide and for products of incomplete combustion (PIC) including CO, volatile and semi-volatile hydrocarbons, as well as particulate matter. Results showed that whereas CO2 was generated during both the observed sequential volatile matter and char combustion phases of the fuels, PICs were only generated during the volatile matter combustion phase. CO2 emissions were the highest from coal, whereas CO and other PIC emissions were the highest from bagasse. Under this particular combustion configuration, combustion of the volatile matter of the blends resulted in lower yields of PIC, than combustion of the volatiles of the neat fuels. Though CO and unburned hydrocarbons from coal as well as from the blends did not exhibit a clear trend with furnace temperature, such emissions from bagasse clearly increased with temperature. The presence of the secondary furnace (afterburner) typically reduced PIC, by promoting further oxidation of the primary furnace effluents. (C) 2012 Elsevier Ltd. All rights reserved.

Performance and composition of bacterial communities in anaerobic fluidized bed reactors for hydrogen production: Effects of organic loading rate and alkalinity

This study evaluated the effects of the organic loading rate (OLR) and pH buffer addition on hydrogen production in two anaerobic fluidized bed reactors (AFBRs) operated simultaneously. The AFBRs were fed with glucose, and expanded clay was used as support material. The reactors were operated at a temperature of 30 degrees C, without the addition of a buffer (AFBR1) and with the addition of a pH buffer (AFBR2, sodium bicarbonate) for OLRs ranging from 19.0 to 140.6 kg COD m(-3) d(-1) (COD: chemical oxygen demand). The maximum hydrogen yields for AFBR1 and AFBR2 were 2.45 and 1.90 mol H-2 mol(-1) glucose (OLR of 84.3 kg COD m(-3) d(-1)), respectively. The highest hydrogen production rates were 0.95 and 0.76 L h(-1) L-1 for AFBR1 and AFBR2 (OLR of 140.6 kg COD m(-3) d(-1)), respectively. The operating conditions in AFBR1 favored the presence of such bacteria as Clostridium, while the bacteria in AFBR2 included Clostridium, Enterobacter, Klebsiella, Veillonellaceae, Chryseobacterium, Sporolactobacillus, and Burkholderiaceae. Copyright (C) 2012, Hydrogen Energy Publications, LLC. Published by Elsevier Ltd. All rights reserved.

Effect of sulfide concentration on autotrophic denitrification from nitrate and nitrite in vertical fixed-bed reactors

Autotrophic denitrification coupled with sulfide oxidation represents an interesting alternative for the simultaneous removal of nitrate/nitrite and sulfide from wastewaters. The applicability of such bioprocess is especially advantageous for the post treatment of effluents from anaerobic reactors, since they usually produce sulfides, which can be used as endogenous electron donor for autotrophic denitrification. This study evaluated the effect of sulfide concentration on this bioprocess using nitrate and nitrite as electron acceptors in vertical fixed-bed reactors. The results showed that intermediary sulfur compounds were mainly produced when excess of electron donor was applied, which was more evident when nitrate was used. Visual evidences suggested that elemental sulfur was the intermediary compound produced. There was also evidence that the elemental sulfur previously formed was being used when sulfide was applied in stoichiometric concentration relative to nitrate/nitrite. Nitrite was more readily consumed than nitrate. For both electron acceptors and sulfide concentrations tested, autotrophic denitrification was not affected by residual heterotrophic denitrification via endogenic activity, occurring as a minor additional nitrogen removal process. (C) 2012 Elsevier Ltd. All rights reserved.

A Two-Stage Aerobic/Anaerobic Denitrifying Horizontal Bioreactor Designed for Treating Ammonium and H2S Simultaneously

A two-stage bioreactor was operated for a period of 140 days in order to develop a post-treatment process based on anaerobic bioxidation of sulfite. This process was designed for simultaneously treating the effluent and biogas of a full-scale UASB reactor, containing significant concentrations of NH4 and H2S, respectively. The system comprised of two horizontal-flow bed-packed reactors operated with different oxygen concentrations. Ammonium present in the effluent was transformed into nitrates in the first aerobic stage. The second anaerobic stage combined the treatment of nitrates in the liquor with the hydrogen sulfide present in the UASB-reactor biogas. Nitrates were consumed with a significant production of sulfate, resulting in a nitrate removal rate of 0.43 kg N m(3) day(-1) and a parts per thousand yen92 % efficiency. Such a removal rate is comparable to those achieved by heterotrophic denitrifying systems. Polymeric forms of sulfur were not detected (elementary sulfur); sulfate was the main product of the sulfide-based denitrifying process. S-sulfate was produced at a rate of about 0.35 kg m(3) day(-1). Sulfur inputs as S-H2S were estimated at about 0.75 kg m(3) day(-1) and Chemical Oxygen Demand (COD) removal rates did not vary significantly during the process. DGGE profiling and 16S rRNA identified Halothiobacillus-like species as the key microorganism supporting this process; such a strain has not yet been previously associated with such bioengineered systems.

Feasibility Study of a Solar Reactor for Phenol Treatment by the Photo-Fenton process in Aqueous Solution

Solar reactors can be attractive in photodegradation processes due to lower electrical energy demand. The performance of a solar reactor for two flow configurations, i.e., plug flow and mixed flow, is compared based on experimental results with a pilot-scale solar reactor. Aqueous solutions of phenol were used as a model for industrial wastewater containing organic contaminants. Batch experiments were carried out under clear sky, resulting in removal rates in the range of 96100?%. The dissolved organic carbon removal rate was simulated by an empirical model based on neural networks, which was adjusted to the experimental data, resulting in a correlation coefficient of 0.9856. This approach enabled to estimate effects of process variables which could not be evaluated from the experiments. Simulations with different reactor configurations indicated relevant aspects for the design of solar reactors.

Catalytic liquid- and gas-phase oxidations for the synthesis of intermediates and specialty chemicals: some examples of industrial relevance

Nowadays, it is clear that the target of creating a sustainable future for the next generations requires to re-think the industrial application of chemistry. It is also evident that more sustainable chemical processes may be economically convenient, in comparison with the conventional ones, because fewer by-products means lower costs for raw materials, for separation and for disposal treatments; but also it implies an increase of productivity and, as a consequence, smaller reactors can be used. In addition, an indirect gain could derive from the better public image of the company, marketing sustainable products or processes. In this context, oxidation reactions play a major role, being the tool for the production of huge quantities of chemical intermediates and specialties. Potentially, the impact of these productions on the environment could have been much worse than it is, if a continuous efforts hadn’t been spent to improve the technologies employed. Substantial technological innovations have driven the development of new catalytic systems, the improvement of reactions and process technologies, contributing to move the chemical industry in the direction of a more sustainable and ecological approach. The roadmap for the application of these concepts includes new synthetic strategies, alternative reactants, catalysts heterogenisation and innovative reactor configurations and process design. Actually, in order to implement all these ideas into real projects, the development of more efficient reactions is one primary target. Yield, selectivity and space-time yield are the right metrics for evaluating the reaction efficiency. In the case of catalytic selective oxidation, the control of selectivity has always been the principal issue, because the formation of total oxidation products (carbon oxides) is thermodynamically more favoured than the formation of the desired, partially oxidized compound. As a matter of fact, only in few oxidation reactions a total, or close to total, conversion is achieved, and usually the selectivity is limited by the formation of by-products or co-products, that often implies unfavourable process economics; moreover, sometimes the cost of the oxidant further penalizes the process. During my PhD work, I have investigated four reactions that are emblematic of the new approaches used in the chemical industry. In the Part A of my thesis, a new process aimed at a more sustainable production of menadione (vitamin K3) is described. The “greener” approach includes the use of hydrogen peroxide in place of chromate (from a stoichiometric oxidation to a catalytic oxidation), also avoiding the production of dangerous waste. Moreover, I have studied the possibility of using an heterogeneous catalytic system, able to efficiently activate hydrogen peroxide. Indeed, the overall process would be carried out in two different steps: the first is the methylation of 1-naphthol with methanol to yield 2-methyl-1-naphthol, the second one is the oxidation of the latter compound to menadione. The catalyst for this latter step, the reaction object of my investigation, consists of Nb2O5-SiO2 prepared with the sol-gel technique. The catalytic tests were first carried out under conditions that simulate the in-situ generation of hydrogen peroxide, that means using a low concentration of the oxidant. Then, experiments were carried out using higher hydrogen peroxide concentration. The study of the reaction mechanism was fundamental to get indications about the best operative conditions, and improve the selectivity to menadione. In the Part B, I explored the direct oxidation of benzene to phenol with hydrogen peroxide. The industrial process for phenol is the oxidation of cumene with oxygen, that also co-produces acetone. This can be considered a case of how economics could drive the sustainability issue; in fact, the new process allowing to obtain directly phenol, besides avoiding the co-production of acetone (a burden for phenol, because the market requirements for the two products are quite different), might be economically convenient with respect to the conventional process, if a high selectivity to phenol were obtained. Titanium silicalite-1 (TS-1) is the catalyst chosen for this reaction. Comparing the reactivity results obtained with some TS-1 samples having different chemical-physical properties, and analyzing in detail the effect of the more important reaction parameters, we could formulate some hypothesis concerning the reaction network and mechanism. Part C of my thesis deals with the hydroxylation of phenol to hydroquinone and catechol. This reaction is already industrially applied but, for economical reason, an improvement of the selectivity to the para di-hydroxilated compound and a decrease of the selectivity to the ortho isomer would be desirable. Also in this case, the catalyst used was the TS-1. The aim of my research was to find out a method to control the selectivity ratio between the two isomers, and finally to make the industrial process more flexible, in order to adapt the process performance in function of fluctuations of the market requirements. The reaction was carried out in both a batch stirred reactor and in a re-circulating fixed-bed reactor. In the first system, the effect of various reaction parameters on catalytic behaviour was investigated: type of solvent or co-solvent, and particle size. With the second reactor type, I investigated the possibility to use a continuous system, and the catalyst shaped in extrudates (instead of powder), in order to avoid the catalyst filtration step. Finally, part D deals with the study of a new process for the valorisation of glycerol, by means of transformation into valuable chemicals. This molecule is nowadays produced in big amount, being a co-product in biodiesel synthesis; therefore, it is considered a raw material from renewable resources (a bio-platform molecule). Initially, we tested the oxidation of glycerol in the liquid-phase, with hydrogen peroxide and TS-1. However, results achieved were not satisfactory. Then we investigated the gas-phase transformation of glycerol into acrylic acid, with the intermediate formation of acrolein; the latter can be obtained by dehydration of glycerol, and then can be oxidized into acrylic acid. Actually, the oxidation step from acrolein to acrylic acid is already optimized at an industrial level; therefore, we decided to investigate in depth the first step of the process. I studied the reactivity of heterogeneous acid catalysts based on sulphated zirconia. Tests were carried out both in aerobic and anaerobic conditions, in order to investigate the effect of oxygen on the catalyst deactivation rate (one main problem usually met in glycerol dehydration). Finally, I studied the reactivity of bifunctional systems, made of Keggin-type polyoxometalates, either alone or supported over sulphated zirconia, in this way combining the acid functionality (necessary for the dehydrative step) with the redox one (necessary for the oxidative step). In conclusion, during my PhD work I investigated reactions that apply the “green chemistry” rules and strategies; in particular, I studied new greener approaches for the synthesis of chemicals (Part A and Part B), the optimisation of reaction parameters to make the oxidation process more flexible (Part C), and the use of a bioplatform molecule for the synthesis of a chemical intermediate (Part D).

Aplicación de un tratamiento biológico a las aguas residuales provenientes de una destilería de alcohol de caña, utilizando un reactor UASB

En este trabajo se llevó a cabo el tratamiento de vinazas mediante dos tecnologías anaerobias. Se dividió en cuatro estudios técnicos. El primero fue el arranque y estabilización del reactor UASB (Upflow Anaerobic Sludge Blanket), en dónde se evaluó la estabilización mediante la eficiencia de remoción de DQO y la granulación del lodo. El segundo estudio evaluó el rendimiento del reactor UASB frente a diferentes Cva. El tercer estudio evaluó el efecto del TRH sobre la eficiencia del reactor UASB, y el cuarto de ellos fue evaluar el rendimiento del RABF (Reactor Anaerobio de Biomasa Fija). El reactor UASB de 2,6 L de capacidad, fue arrancado por lotes, con seis ensayos utilizando vinaza como sustrato. Se obtuvieron eficiencias de remoción en DQO en un rango de 79-91%, en los seis lotes. Se obtuvo formación de gránulos con diámetro (Ø) de 0,85-1,15 mm y un coeficiente de esfericidad (Є) de 0,7-0,77. Se logró la granulación de lodos tras 2 meses de operación. Alcanzada la estabilización del reactor UASB, se siguió una operación en flujo continuo. Las Cva probadas de 1, 2, 4 y 6 gDQO/L.d para el reactor UASB dan una respuesta bastante favorable con respecto al rendimiento del reactor, ya que presento eficiencias de remoción de DQOs del 51 hasta el 76%, eficiencias similares a los reportados por la literatura. En el estudio de TRH se operó con Cva de 6 gDQO/L.d y los TRH fueron de 24, 12 ,5 ,3 y 1 día. El % de eliminación de DQO fue de 51, 60, 57, 60 y 63 % remoción en DQOsoluble, respectivamente. Se alcanzó una producción de biogás máximo de 5.283 ml/d, pero al reducir el TRH se observó una reducción proporcional del volumen total de biogás. El %CH4 contenido en el biogás aumento al disminuir el TRH, reflejando valores de 80 al 92 % de CH4. El RABF con un volumen de 8,2 L, utilizo tubos de plástico corrugado como medio de soporte para las bacterias. Se aplicaron las siguientes Cva; 0,5, 1, 3 y 6 gDQO/L.d. El reactor RABF presento una excelente remoción de la materia orgánica (80% DQOs), una producción de biogás estable, y un contenido en CH4 del biogás muy interesante. Sin embargo, para una Cva superior a 3 gDQO/L.d empezó un comportamiento inesperado de reducción de capacidad. Las condiciones hidrodinámicas del reactor UASB son decisivas para la formación de los gránulos, condición previa para iniciar el flujo continuo. Al operar el reactor UASB en modo continuo, se pudo evaluar las mejores condiciones de operación para este tipo de residuo (vinaza). La Cva de 6 gDQO/L.d para el reactor UASB alimentado con vinaza bruta representa el límite de su capacidad. Sin embargo, al aumentar la Cva se genera una mayor producción de biogás y metano. La eficiencia de remoción de la DQO soluble es independiente del TRH, para una Cva de 6 g DQO/L•d y las condiciones de TRH probadas (24, 12, 5, 3 y 1 días). Los valores de remoción de DQO alcanzados son un poco superior a los valores de biodegradabilidad anaerobia de la vinaza observados de 50 %. De manera general, la reducción del TRH o bien la dilución de la vinaza no presenta un efecto significativo sobre la remoción de la materia orgánica soluble, pero si lo presenta en la remoción de sulfatos reduciendo indirectamente su toxicidad. El soporte termoplástico inoculado en el RABF y alimentado con vinaza bruta, actuó como un filtro, además de obtener buenos resultados en eliminación de DQO, pero dada las dimensiones y la altura del relleno se frena la evacuación del metano. This work was carried out by treatment vinasses with two anaerobic technologies. It was divided into four technical studies. The first was the start up and stabilization Upflow Anaerobic Sludge Blanket (UASB) reactor, where the stability was evaluated by the removal efficiency of COD and sludge granulation. The second study evaluated the performance of the UASB reactor against different OLR. The third study evaluated the effect of HRT on the efficiency of the UASB reactor, and the fourth of which was evaluate the performance Fixed Biomass Anaerobic (FBA) reactor. The UASB reactor of 2,6 L capacity, was started in batch, with six assays using vinasse as substrate. Were obtained removal efficiencies of COD in the range of 79- 91% in the six batches. Forming granules were obtained with a diameter (Ø) of 0,85- 1,15 mm and sphericity coefficient (Є) of 0,7 to 0,77. Sludge granulation was achieved after 2 months of operation. Once stabilization is achieved of the UASB reactor, it was followed by a continuous flow operation. The OLR tested 1, 2, 4 and 6 gCOD/L.d for UASB reactor gives a very favorable response regarding the performance of the reactor, as presented COD5 removal efficiencies of 51 to 76%, similar efficiencies those reported in the literature The HRT study was operated with an OLR of 6 gCOD/L.d and HRT were 24, 12, 5, 3 and 1 day. The removal efficiency was 51, 60, 57, 60 and 63% in soluble COD, respectively. It reached a maximum biogas production of 5.283 ml / d, but by reducing the HRT showed a proportional reduction in the total volume of biogas. The %CH4 content in the biogas increased with decreasing TRH, reflecting values of 80 to 92% of CH4. The FBA reactor with a volume of 8,2 L, used corrugated plastic tubes as carrier for bacteria transportation. The following OLR was applied, 0,5, 1, 3 and 6 gCOD/L.d. The FBA reactor showed an excellent removal of organic matter (80% CODS), a stable biogas production, and CH4 content very interesting. However, for more than 3 gCOD/L.d OLR began with unexpected behavior of capacity reduction. The UASB reactor hydrodynamic conditions are decisive for the formation of the granules, precondition to start the continuous flow. By operating the UASB reactor in continuous mode, it was possible to evaluate the best operating conditions for this type of waste (vinasse). The OLR of 6 gCOD/L.d for the UASB reactor fed with raw vinasse represents the limit of its capacity. However, with increasing OLR creates increased biogas production and methane. The removal efficiency of soluble COD is independent of HRT for OLR of 6 gCOD/L.d and HRT conditions tested (24, 12, 5, 3 and 1 day). COD Removal values achieved are slightly higher than the values of the vinasse anaerobic biodegradability of observed at 50%. Generally, reduction of HRT or vinasse dilution does not present a significant effect on the removal of the soluble organic matter; however if it occurs in the removal of sulfate reducing indirectly its toxicity. The thermoplastic support inoculated in FBA reactor and fed with raw vinasse, acted as a filter, in addition to obtaining good results in COD removal, but given the size and height of the filling slows evacuation of methane.

Remoção de metil paration e atrazina em reatores de bancada com fungos

Neste estudo foi avaliada a remoção de metil paration - inseticida e atrazina - herbicida presentes em água, em reatores de bancada, com fungos. A pesquisa foi dividida em quatro etapas: operação em batelada com metil paration e micélio fúngico, com e sem glicose; teste de toxicidade em placas com Aspergillus niger AN400; operação em batelada com os pesticidas atrazina e metil paration e esporos de Aspergillus niger AN400, com e sem glicose; e operação em reatores de leito fixo e fluxo ascendente. Na primeira etapa, a remoção de metil paration foi de 97% nos reatores sem glicose e 94% nos reatores com glicose com 32 dias de reação. Na operação em batelada, com esporos, um modelo cinético de primeira ordem representou bem a velocidade de decaimento de metil paration nesta fase, principalmente, nos reatores que continham glicose. Para os experimentos sem adição de glicose, a constante cinética foi de 0,063 ± 0,005/h, enquanto que para os experimentos com glicose a constante foi de 0,162 ± 0,014/h. Dessa forma, a adição de glicose resultou efetivamente em aumento na velocidade de conversão do inseticida. Na fase experimental, com atrazina e esporos de Aspergillus niger AN400, a presença do substrato primário (glicose) não teve influência na remoção de atrazina, sendo que os percentuais de remoção foram muito próximos aos percentuais encontrados nos reatores sem glicose. O estudo cinético, nessa fase com atrazina e esporos, revelou que para os experimentos sem a adição de glicose, o valor da velocidade de conversão de atrazina (RATZo) foi de 0,023/d, enquanto que para os experimentos com glicose (RATZo) foi 0,022/d. Portanto, a adição de glicose parece não ter influenciado significativamente a velocidade de remoção do herbicida por Aspergillus niger AN400. O teste de toxicidade demonstrou que metil paration e atrazina não inibiram o crescimento do fungo nas várias concentrações testadas, inclusive nas mais elevadas, que foram 60 mg/L e 25 mg/L para metil paration e atrazina, respectivamente. No reator de leito fixo a remoção de metil paration foi de 40% com 12 h de tempo de detenção hidráulica, e 0,5 g glicose/L. Porém, quando a concentração de glicose foi duplicada a remoção de metil paration diminuiu para 35%. Neste reator o pH se manteve na faixa ácida 3,4 a 5,2, considerada ideal para os fungos. Os resultados encontrados mostram a viabilidade dos fungos para remoção desses pesticidas, considerados persistentes no ambiente.

Assessment of CO2 adsorption capacity on activated carbons by a combination of batch and dynamic tests

In this work, batch and dynamic adsorption tests are coupled for an accurate evaluation of CO2 adsorption performance for three different activated carbons obtained from olives stones by chemical activation followed by physical activation with CO2 at varying times, i.e. 20, 40 and 60 h. Kinetic and thermodynamic CO2 adsorption tests from simulated flue-gas at different temperature and CO2 pressure are carried out both in batch (a manometric equipment operating with pure CO2) and dynamic (a lab-scale fixed-bed column operating with CO2/N2 mixture) conditions. The textural characterization of the activated carbon samples shows a direct dependence of both micropore and ultramicropore volume on the activation time, hence AC60 has the higher contribution. The adsorption tests conducted at 273 and 293 K showed that, when CO2 pressure is lower than 0.3 bar, the lower the activation time the higher CO2 adsorption capacity and a ranking ωeq(AC20)>ωeq(AC40)>ωeq(AC60) can be exactly defined when T= 293 K. This result can be likely ascribed to a narrower pore size distribution of the AC20 sample, whose smaller pores are more effective for CO2 capture at higher temperature and lower CO2 pressure, the latter representing operating conditions of major interest for decarbonation of a flue-gas effluent. Moreover, the experimental results obtained from dynamic tests confirm the results derived from the batch tests in terms of CO2 adsorption capacity. It is important to highlight that the adsorption of N2 on the synthesized AC samples can be considered negligible. Finally, the importance of a proper analysis of characterization data and adsorption experimental results is highlighted for a correct assessment of CO2 removal performances of activated carbons at different CO2 pressure and operating temperature.