Nitrifying microbial community analysis of nitrite accumulating biofilm reactor by fluorescence in situ hybridization

Biological nitrogen removal via nitrite pathway in wastewater treatment is very important especially in the cost of aeration and as an electron donor for denitrification. Wastewater nitrification and nitrite accumulations were carried out in a biofilm reactor. The biofilm reactor showed almost complete nitrification and most of the oxidized ammonium was present as nitrite at the ammonium load of 1.2 kg N/m3/d. Nitrite accumulation was achieved by the selective inhibition of nitrite oxidizers by free ammonia and oxygen limitation. Nitrite oxidation activity was recovered as soon as the inhibition factor was removed. Fluorescence in situ hybridization studies of the nitrite accumulating biofilm system have shown that genus Nitrosomonas which is specifically hybridized with probe NSM 156 was the dominant nitrifying bacteria while Nitrospira was less abundant than those of normal nitrification systems. Further FISH analysis showed that the combinations of Nitrosomonas and Nitrospira cells were identified as important populations of nitrifying bacteria in an autotrophic nitrifying biofilm system.

Nitrification of high strength ammonia wastewtaer treatment - process selection is the major factor.

Biological nitrogen removal via the nitrite pathway in wastewater treatment is very important in Saving the cost of aeration and as an electron donor for denitrification. Wastewater nitrification and nitrite accumulation were carried out in a biofilm airlift reactor with autotrophic nitrifying biofilm. The biofilm reactor showed almost complete nitrification and most of the oxidized ammonium was present as nitrite at the ammonium load of 1.5 to 3.5 kg N/m3.d. Nitrite accumulation was stably achieved by the selective inhibition of nitrite oxidizers with free ammonia and dissolved oxygen limitation. Stable 100% conversion to nitrite could also be achieved even under the absence of free ammonia inhibition on nitrite oxidizers. Batch ammonium oxidation and nitrite oxidation with nitrite accumulating nitrifying biofilm showed that nitrite Oxidation was completely inhibited when free ammonia is higher than 0.2 mg N/L. However, nitrite oxidation activity was recovered as soon as the free ammonia concentration was below the threshold level when dissolved oxygen concentration was not the limiting factor. Fluorescence in situ hybridization analysis of cryosectioned nitrite accumulating nitrifying biofilm showed that the β-subclass of Proteobacteria, where ammonia oxidizers belong, was distributed outside the biofilm whereas the α-subclass of Proteobacteria, where nitrite oxidizers belong, was found mainly in the inner part of the biofilm. It is likely that dissolved oxygen deficiency or limitation in the inner part of the nitrifying biofilm, where nitrite oxidizers exist, is responsible for the complete shut down of the nitrite oxidizers activity under the absence of free ammonia inhibition.

Dryout phenomena in a three-phase fixed-bed reactor

Understanding the mechanism of liquid-phase evaporation in a three-phase fixed-bed reactor is of practical importance, because the reaction heat is usually 7-10 times the vaporization heat of the liquid components. Evaporation, especially the liquid dryout, can largely influence the reactor performance and even safety. To predict the vanishing condition of the liquid phase, Raoult's law was applied as a preliminary approach, with the liquid vanishing temperature defined based on a liquid flow rate of zero. While providing correct trends, Raoult's law exhibits some limitation in explaining the temperature profile in the reactor. To comprehensively understand the whole process of liquid evaporation, a set of experiments on inlet temperature, catalyst activity, liquid flow rate, gas flow rate, and operation pressure were carried out. A liquid-region length-predicting equation is suggested based on these experiments and the principle of heat balance.

Estudo de digestão anaeróbia de resíduos sólidos agro-alimentares em instalação piloto

Hoje em dia são várias as energias “verdes” que beneficiam de forma inequívoca o meio ambiente, de modo a aproveitar recursos naturais disponíveis na natureza. Entre todos os tipos de energias limpas, surge a produção de biogás. É de notar que apesar de ser uma forma de energia já utilizada há muitos anos, esta pode ser melhorada através de uma gestão adequada de todos os recursos envolvidos na sua produção. Consegue-se desta forma, optimizar a produção de biogás, contribuindo para uma rentabilização do funcionamento de uma instalação. Para esta optimização é necessária uma análise e caracterização detalhada dos resíduos utilizados na geração desta energia. O presente trabalho foca-se no estudo da produção de biogás através de digestão anaeróbica. Este trabalho baseia-se num estudo real de produção de biogás, num reactor à escala semi-industrial, e com uma temperatura de trabalho em regime mesofílico (37°C). O substrato utilizado para a alimentação deste reactor foi cedido por uma conhecida indústria do ramo alimentar e consistia numa mistura de “casca” de batatas e lamas, numa proporção de 30% e 30% respectivamente. Em termos de resultados Óbidos neste projecto, verificou-se uma redução de cerca de 40% dos sólidos totais, o que indicia, aparentemente, a existência de dificuldades na hidrólise dos compostos em suspensão. A remoção orgânica na sua globalidade oscilou numa ampla gama de valores, com um valor médio de cerca 50%. A larga variedade de resultados pode estar relacionada com a heterogeneidade da amostra da alimentação. Apesar da existência de algumas dificuldades inerentes à realização do trabalho prático, concluiu-se que o substrato utilizado neste estudo revela grande potencial de produção de biogás.

Viabilidade económica da implementação de um reactor nuclear para a produção de energia eléctrica em Portugal

O presente trabalho tem como objectivo avaliar economicamente e determinar a viabilidade da implementação de um reactor nuclear para produção de energia eléctrica. Faz-se uma abordagem a aspectos da energia nuclear no mundo e em particular a energia nuclear na união europeia, faz-se uma análise sobre a estrutura do sector nuclear em Espanha e o futuro da energia no mundo. É realizada uma análise sobre a energia nuclear em Portugal, são abordados aspectos como o planeamento energético, a localização da central nuclear, os recursos nacionais e internacionais, a inspecção e regulação nuclear e o impacto industrial. Por fim, faz-se uma análise sobre o mix energético português. Faz-se uma descrição do ciclo de combustível, isto é, um estudo a todas as fases pela qual o combustível nuclear passa desde a sua extracção, passando pela produção de energia e processamento dos resíduos. São descritos os principais componentes de uma central nuclear e o seu princípio de funcionamento. São analisados em detalhe os principais componentes de um reactor PWR (Objecto de estudo deste trabalho) e faz-se uma breve descrição de alguns modelos de reactores nucleares. É feita uma breve abordagem aos principais acidentes nucleares que ocorreram, e descrita a escala de ocorrências nucleares e as várias fases de desmantelamento de uma central. São apresentados os principais custos da central nuclear. Também é apresentado um estudo de viabilidade económica analisando três cenários diferentes e é apresentada uma análise de sensibilidade do VAL em função de algumas variáveis que têm grande influência na avaliação económica. São apresentadas as principais conclusões.

Recuperação do calor de um efluente primário para aquecimento de lamas de um reactor anaeróbio

O presente trabalho tem como principal objectivo o estudo da possibilidade de recuperação de calor de um efluente proveniente do tratamento primário da fábrica do grupo Portucel Soporcel (fábrica produtora de pasta de papel), para o aquecimento da corrente de lamas do digestor anaeróbio da SimRia S.A. – ETAR Norte, (ambas localizadas em Cacia, distrito de Aveiro). A solução consiste na implementação de um sistema de permuta térmica entre estas duas correntes, constituído fundamentalmente por dois permutadores de placas em espiral, montados em paralelo que operam em contra-corrente. Segundo este novo sistema de aquecimento, as lamas abandonam o digestor anaeróbio da mesma ETAR a um caudal de 110 m3/h, que se dividirá em duas linhas, sendo admitidas em cada permutador a 55 m3/h e a uma temperatura de 32 ºC regressando ao digestor a uma temperatura de 37 ºC (temperatura óptima a que ocorre a digestão anaeróbia das lamas). O efluente disponível, abandona o tratamento primário da Portucel, a 45 ºC e é encaminhado até aos permutadores da SimRia S.A., onde vai trocar calor com as lamas e regressa à Portucel a 40ºC, sendo admitido nas torres de arrefecimento da fábrica de papel. A nova instalação proposta pretende substituir a actual existente na ETAR em causa, em que a corrente de água que aquece as lamas, circula num circuito fechado entre um único permutador e uma caldeira, alimentada com o biogás que se produz no digestor anaeróbio, e que é responsável pelo controlo da temperatura da corrente de água. Pretende-se que a implementação deste novo método de aquecimento de lamas seja uma alternativa económica relativamente ao actual sistema, uma vez que vai substituir a corrente de biogás alimentada à caldeira podendo este recurso ser transformado em energia eléctrica e posteriormente comercializada. A análise financeira realizada ao projecto demonstrou que o projecto é rentável, uma vez que, a diferença entre todos ganhos e custos ao fim dos 10 anos de vida útil estimados é de cerca de 150 000,0 €. O período de retorno do investimento é alcançado no final dos primeiros 6 anos e a taxa interna de rentabilidade obtida foi de 36 %. Posteriormente incluiu-se neste estudo a possibilidade de tratamento das lamas geradas na fábrica da Portucel na ETAR da SimRia recorrendo a um terceiro digestor. Conclui-se que se trata duma opção vantajosa, uma vez que permite obter um caudal de biogás 44 m3/h, que convertido em potência permite obter 150 kW que poderá ser aproveitado para produção de energia ou comercializado gerando uma receita adicional de 130 000,0 €/ano para as entidades envolvidas.

Dimensionamento de um reactor de leito fluidizado para gasificação de biomassa

Na actualidade, quando se procura a diversificação energética, em especial de fontes renováveis, a gasificação surge como uma forma promissora de aproveitamento da biomassa, nomeadamente dos resíduos florestais, para a geração de energia eléctrica. Neste contexto, passou-se em revista as diversas formas de gasificação, a sua evolução histórica e os diversos tipos de reactores com as suas vantagens e desvantagens. De igual forma, foram analisadas as disponibilidades e características da biomassa no mundo e em Portugal, destacando-se as suas potencialidades e as dificuldades no seu aproveitamento. Fez-se o dimensionamento de um reactor-gasificador de leito fluidizado borbulhante à escala piloto, bem como dos equipamentos complementares, sistema de alimentação, ventilador, ciclone, filtro para o gás produzido e gerador eléctrico. As dimensões dum reactor para trabalhos laboratoriais foram determinadas por cálculo das condições hidrodinâmicas, que, também, permitiram calcular o caudal de ar a utilizar. Por balanços materiais, considerando-se uma composição experimental do gás de síntese citada na literatura, determinou-se uma possível composição da alimentação e um caudal de alimentação.

Biofiltration of Air/Styrene and Air/Styrene/Acetone mixtures in a bubble column reactor

The goal of this work was the treatment of polluted waste gases in a bubble column reactor (BCR), in order to determinate the maximum value of reactor’s efficiency (RE), varying the inlet concentration (C in) of the pollutants. The gaseous mixtures studied were: (i) air with styrene and (ii) air with styrene and acetone. The liquid phase used to contain the biomass in the reactor was a basal salt medium (BSM), fundamental for the microorganisms’ development. The reactor used in this project consists of a glass column of 620mm height and inside diameter 75mm. In all essays there were continually measured: pH, dissolved oxygen and liquid’s temperature. Temperature and pH were controlled (T=24ºC, 7.0 ≤ pH ≤ 7.7). In all experiments the liquid volume (including the biomass) used in the reactor was kept constant (1.5L) as well as the total gas flowrate (1 L/min). Concerning the goal of the work, some parameters were calculated: the organic load (OL), removal efficiency (RE), elimination capacity (EC), biomass concentration (xf) and dry biomass concentration (Xdw). In a first series of experiments, the gas mixture used was air with styrene, varying its concentration from 191 mg.m-3 to 6500 mg.m-3.It was concluded that the RE maximum value (97%) was obtained for C in Sty = 4200 mg.m-3. For the maximum tested value of C in Sty, RE obtained was 20%. In a second step, the gaseous mixture included acetone, varying C in Sty between 225 mg.m-3 and 2659 mg.m-3 and C in Ac between 153mg.m-3 and 1389 mg.m-3. The aim of these tests was the determination of C in Ac for which RE was maximum, obtaining C in Ac = 750 mg.m-3. A third series of experiments was performed, in which C in Ac was maintained equal to that value and C in Sty was varied until higher values (5422 mg.m-3). RE maximum values obtained in this last series were 100% for styrene and 40% for acetone. One important conclusion is the fact that the microorganisms available degrade better styrene than acetone. On the ambit of this study, it was possible to identify the species available in biomass: Xanthobacter antotrophicus py2, Enterobacter aerogenes, Nocardia, Corynebacterium Spp., Rhodococcus rhodochrous e Pseudomonas Sp.

Sulfadiazine-potentiometric sensors for flow and batch determinations of sulfadiazine in drugs and biological fluids

New PVC membrane electrodes for the determination of sulfadiazine (SDZ) are presented. The electrodes are fabricated with conventional and tubular configurations with a graphite-based electrical contact, and no internal reference solution. The selective membranes consist of bis(triphenylphosphoranilidene)ammonium·SDZ (electrode A), tetraoctylammonium bromide (electrode B), or iron(II)-phthalocyanine (FePC) (electrode C) electroactive materials dispersed in a PVC matrix of o-nitrophenyl octyl ether (o-NPOE) plasticizer. The sensors A, B, and C displayed linear responses over the concentration ranges 1.0*10-2 – 1.0*10–5, 1.0*10–2 – 7.5*10–6, and 3.2*10–2 – 7.0* 10–6 mol l–1 (detection limits of 1.09, 2.04 and 0.87 mg ml–1) with anionic slopes of –57.3 ± 0.1, –46.7 ± 0.5, and –65.1 ± 0.2 mV decade–1, respectively. No effect from pH was observed within 4.0 – 5.5, 4.8 – 10, and 4.5 – 8, respectively, and good selectivity was found. The sensors were applied to the analysis of pharmaceuticals and biological fluids in steady state and in flow conditions.

Copper, nickel and zinc removal by peanut hulls: batch and column studies in mono, tri-component systems and with real effluent

The main goal of this research study was the removal of Cu(II), Ni(II) and Zn(II) from aqueous solutions using peanut hulls. This work was mainly focused on the following aspects: chemical characterization of the biosorbent, kinetic studies, study of the pH influence in mono-component systems, equilibrium isotherms and column studies, both in mono and tri-component systems, and with a real industrial effluent from the electroplating industry. The chemical characterization of peanut hulls showed a high cellulose (44.8%) and lignin (36.1%) content, which favours biosorption of metal cations. The kinetic studies performed indicate that most of the sorption occurs in the first 30 min for all systems. In general, a pseudo-second order kinetics was followed, both in mono and tri-component systems. The equilibrium isotherms were better described by Freundlich model in all systems. Peanut hulls showed higher affinity for copper than for nickel and zinc when they are both present. The pH value between 5 and 6 was the most favourable for all systems. The sorbent capacity in column was 0.028 and 0.025 mmol g-1 for copper, respectively in mono and tri-component systems. A decrease of capacity for copper (50%) was observed when dealing with the real effluent. The Yoon-Nelson, Thomas and Yan’s models were fitted to the experimental data, being the latter the best fit.

New biomimetic sensors for the determination of tetracycline in biological samples: batch and flow mode operations

New potentiometric membrane sensors with cylindrical configuration for tetracycline (TC) are described based on the use of a newly designed molecularly imprinted polymer (MIP) material consisting of 2-vinylpyridine as a functional monomer in a plasticized PVC membrane. The sensor exhibited significantly enhanced response towards TC over the concentration range 1.59 10 5–1.0 10 3 mol L 1 at pH 3–5 with a lower detection limit of 1.29 10 5 mol L 1. The response was near-Nernstian, with average slopes of 63.9 mV decade 1. The effect of lipophilic salts and various foreign common ions were tested and were found to be negligible. The possibility of applying the proposed sensor to TC determination in spiked biological fluid samples was demonstrated.

Direct electroanalytical determination of fluvastatin in a pharmaceutical dosage form: batch and flow analysis

The reduction of luvastatin (FLV) at a hanging mercury-drop electrode (HMDE) was studied by square-wave adsorptive-stripping voltammetry (SWAdSV). FLV can be accumulated and reduced at the electrode, with a maximum peak current intensity at a potential of approximately 1.26V vs. AgCl=Ag, in an aqueous electrolyte solution of pH 5.25. The method shows linearity between peak current intensity and FLV concentration between 1.0 10 8 and 2.7 10 6 mol L 1. Limits of detection (LOD) and quantification (LOQ) were found to be 9.9 10 9 mol L 1 and 3.3 10 8 mol L 1, respectively. Furthermore, FLV oxidation at a glassy carbon electrode surface was used for its hydrodynamic monitoring by amperometric detection in a flow-injection system. The amperometric signal was linear with FLV concentration over the range 1.0 10 6 to 1.0 10 5 mol L 1, with an LOD of 2.4 10 7 mol L 1 and an LOQ of 8.0 10 7 mol L 1. A sample rate of 50 injections per hour was achieved. Both methods were validated and showed to be precise and accurate, being satisfactorily applied to the determination of FLV in a commercial pharmaceutical.

Rapid determination of tartaric acid in wines

A flow-spectrophotometric method is proposed for the routine determination of tartaric acid in wines. The reaction between tartaric acid and vanadate in acetic media is carried out in flowing conditions and the subsequent colored complex is monitored at 475 nm. The stability of the complex and the corresponding formation constant are presented. The effect of wavelength and pH was evaluated by batch experiments. The selected conditions were transposed to a flowinjection analytical system. Optimization of several flow parameters such as reactor lengths, flow-rate and injection volume was carried out. Using optimized conditions, a linear behavior was observed up to 1000 µg mL-1 tartaric acid, with a molar extinction coefficient of 450 L mg-1 cm-1 and ± 1 % repeatability. Sample throughput was 25 samples per hour. The flow-spectrophotometric method was satisfactorily applied to the quantification of tartaric acid (TA) in wines from different sources. Its accuracy was confirmed by statistical comparison to the conventional Rebelein procedure and to a certified analytical method carried out in a routine laboratory.

Natural waste materials containing chitin as adsorbents for textile dyestuffs: batch and continuous studies

In this work three natural waste materials containing chitin were used as adsorbents for textile dyestuffs, namely the Anodonta (Anodonta cygnea) shell, the Sepia (Sepia officinalis) and the Squid (Loligo vulgaris) pens. The selected dyestuffs were the Cibacron green T3G-E (CI reactive green 12), and the Solophenyl green BLE 155% (CI direct green 26), both from CIBA, commonly used in cellulosic fibres dyeing, the most used fibres in the textile industry. Batch equilibrium studies showed that the materials’ adsorption capacities increase after a simple and inexpensive chemical treatment, which increases their porosity and chitin relative content. Kinetic studies suggested the existence of a high internal resistance in both systems. Fixed bed column experiments performed showed an improvement in adsorbents’ behaviour after chemical treatment. However, in the column experiments, the biodegradation was the main mechanism of dyestuff removal, allowing the materials’ bioregeneration. The adsorption was strongly reduced by the pore clogging effect of the biomass. The deproteinised Squid pen (grain size 0.500–1.41 mm) is the adsorbent with highest adsorption capacity (0.27 and 0.037 g/g, respectively, for the reactive and direct dyestuffs, at 20ºC), followed by the demineralised Sepia pen and Anodonta shell, behaving like pure chitin in all experiments, but showing inferior performances than the granular activated carbon tested in the column experiments.

Experimental design methodologies for the identification of Michaelis-Menten type kinetics

The main objective of this work was to investigate the application of experimental design techniques for the identification of Michaelis-Menten kinetic parameters. More specifically, this study attempts to elucidate the relative advantages/disadvantages of employing complex experimental design techniques in relation to equidistant sampling when applied to different reactor operation modes. All studies were supported by simulation data of a generic enzymatic process that obeys to the Michaelis-Menten kinetic equation. Different aspects were investigated, such as the influence of the reactor operation mode (batch, fed-batch with pulse wise feeding and fed-batch with continuous feeding) and the experimental design optimality criteria on the effectiveness of kinetic parameters identification. The following experimental design optimality criteria were investigated: 1) minimization of the sum of the diagonal of the Fisher information matrix (FIM) inverse (A-criterion), 2) maximization of the determinant of the FIM (D-criterion), 3) maximization of the smallest eigenvalue of the FIM (E-criterion) and 4) minimization of the quotient between the largest and the smallest eigenvalue (modified E-criterion). The comparison and assessment of the different methodologies was made on the basis of the Cramér-Rao lower bounds (CRLB) error in respect to the parameters vmax and Km of the Michaelis-Menten kinetic equation. In what concerns the reactor operation mode, it was concluded that fed-batch (pulses) is better than batch operation for parameter identification. When the former operation mode is adopted, the vmax CRLB error is lowered by 18.6 % while the Km CRLB error is lowered by 26.4 % when compared to the batch operation mode. Regarding the optimality criteria, the best method was the A-criterion, with an average vmax CRLB of 6.34 % and 5.27 %, for batch and fed-batch (pulses), respectively, while presenting a Km’s CRLB of 25.1 % and 18.1 %, for batch and fed-batch (pulses), respectively. As a general conclusion of the present study, it can be stated that experimental design is justified if the starting parameters CRLB errors are inferior to 19.5 % (vmax) and 45% (Km), for batch processes, and inferior to 42 % and to 50% for fed-batch (pulses) process. Otherwise equidistant sampling is a more rational decision. This conclusion clearly supports that, for fed-batch operation, the use of experimental design is likely to largely improve the identification of Michaelis-Menten kinetic parameters.