The effects of biofilm characteristics on the external mass transfer coefficient in a differential fluidized bed biofilm reactor
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Modelling of biofilm growth for photosynthetic biomass production in a pipe-overflow recirculation bioreactor
2019, Biochemical Engineering JournalCitation Excerpt :For biological wastewater treatment, a mathematical model is used to predict the performance of a biological treatment process and to determine important variables and critical parameters or help with troubleshooting [9]. A model that describes the biofilm process must include the biological process in the biofilm, such as diffusion-reaction [10,11], biofilm growth, biofilm biodegradation [12], and/or absorption on activated carbon [13,14], which depends on the type of process under consideration. Although many studies have described biofilm formation using mathematical models, they were generally limited to certain factors, such as biofilm thickness, biofilm density, and biofilm decay [11].
Three-phase fluidized bed bioreactor modelling and simulation
2017, Biochemical Engineering JournalCitation Excerpt :Symbols used in the mathematical model of the installation have been marked in this figure. Beyenal and Tanyolac [16] proved experimentally that the standard deviation of the mean biofilm thickness is sufficiently small to use a mean value in calculations. This assumption is applied in this work.
Determination of the external mass transfer coefficient and influence of mixing intensity in moving bed biofilm reactors for wastewater treatment
2015, Water ResearchCitation Excerpt :Within the biofilm, the substrates are transported by diffusion due the concentration gradient generated by the consumption of the pollutants. The external mass transfer resistance is usually described as a stagnant film between the bulk phase and the biofilm surface where all external mass transfer processes are included (Beyenal and Tanyolaç, 1998). One important factor which affects the external mass transfer to the biofilm is the mixing intensity within the reactor (Kugaprasatham et al., 1992; Chen et al., 2006).
Effects of mass transfer and light intensity on substrate biological degradation by immobilized photosynthetic bacteria within an annular fiber-illuminating biofilm reactor
2014, Journal of Photochemistry and Photobiology B: BiologyCitation Excerpt :Mathematical models for various configurations of the immobilized bioreactor, such as horizontal and vertical packed beds, fluidized beds, have been reported in the literatures [9,10]. Huang studied the mass transfer characteristics of the liquid film by taking into account the flow pattern and variation of liquid film thickness, but neglected substrate diffusion in fluid bulk zone [11,12]. Mowla established a diffusion–reaction model of biofilm, but they assumed substrate diffused only in the direction of the biofilm depth [13,14].
Effect of gas-liquid mass transfer coefficient and liquid-solid mass transfer resistance on phenol biodegradation in three phase inverse fluidized bed biofilm reactor
2014, Journal of Environmental Chemical EngineeringCitation Excerpt :In phenol biodegradation processes, transfer rates of phenol, oxygen and other nutrients from bulk phase to bioparticle are the rate limiting steps which controls the performance of the reactor. Unfortunately studies on gas–liquid–solid mass transfer effects are very limited in IFBBRs [3–5]. The performance evaluation of IFBBR often requires the calculation of external mass transfer resistance to the biofilm.
Approximate analytical solution of the concentration of phenol and oxygen and rate of phenol degradation in fluidized bed bioreactor
2012, Biochemical Engineering JournalCitation Excerpt :A fluidized-bed bioreactor consists of microorganism coated particles suspended in wastewater which is sufficiently aerated to keep the gas, liquid and the solid particles thoroughly mixed. Biodegradation of phenol in fluidized bed bioreactors (FBRs) have been reported because of their superior performance and some inherent advantages [1–6]. The superior performance of FBR is due to very high concentration of immobilized cells on the solid particles, prevention of washout of the microbes, lack of clogging of the biomass, ease of separation of cells from product stream and elimination of limit on liquid flow rates due to decoupling of residence time of liquid phase and of microbial cells.