Abstract
For the last four decades, viability of photocatalytic degradation of organic compounds in water streams has been demonstrated. Different configurations for solar TiO2 photocatalytic reactors have been used, however pilot and demonstration plants are still countable. Degradation efficiency reported as a function of treatment time does not answer the question: which of these reactor configurations is the most suitable for photocatalytic process and optimum for scale-up and commercialization? Degradation efficiency expressed as a function of the reactor throughput and ease of catalyst removal from treated effluent are used for comparing performance of different reactor configurations to select the optimum for scale-up. Comparison included parabolic trough, flat plate, double skin sheet, shallow ponds, shallow tanks, thin-film fixed-bed, thin film cascade, step, compound parabolic concentrators, fountain, slurry bubble column, pebble bed and packed bed reactors. Degradation efficiency as a function of system throughput is a powerful indicator for comparing the performance of photocatalytic reactors of different types and geometries, at different development scales. Shallow ponds, shallow tanks and fountain reactors have the potential of meeting all the process requirements and a relatively high throughput are suitable for developing into continuous industrial-scale treatment units given that an efficient immobilized or supported photocatalyst is used.
Highlights
In the mid-1970s, the viability of photocatalytic degradation of organic compounds in water using titanium dioxide (TiO2 ) was demonstrated by several research groups [1]
Parabolic Trough reactor (PTR) was used in Sandia National Laboratory, New Mexico for treating water contaminated with salicylic acid
NA: not available; a concentration; b Dichloroacetic acid; c degradation efficiency was reported as a function of accumulated energy, assuming UV-A intensity of 30 W/m2, a normalized treatment duration is calculated; d pH adjusted to 2.8; e conducted at pH 3.8; f conducted at pH 3.3; g in addition to 100 mg/L H2 O2 ; h Calculating throughput for this reactor based on its aperture area is not valid since the parabolic trough is vertical
Summary
In the mid-1970s, the viability of photocatalytic degradation of organic compounds in water using titanium dioxide (TiO2 ) was demonstrated by several research groups [1]. Compound parabolic concentrator; Different reactor configurations have been used to degrade various types of pollutants using solar light or artificial light simulating sunlight. Which of these reactor configurations is the most suitable for the photocatalytic process and is optimum for scale-up and commercialization? F where ACM and ACO are in m2 /kg and m2 /m3 -order, respectively, Ar is the actual reactor area (m2 ), t and to are irradiance and reference time (h), Es and Eso are average solar irradiance and reference solar irradiance (W/m2 ), Vt treated volume (L), M molar mass g/mol, and ci and cf are initial and final pollutant molar concentrations, respectively. Collector area per mass has been used by researchers to compare performances of reactors of different configurations based on estimate of area required for scale-up [80,81]. This review focuses on pilot scale demonstrations using solar or artificial lighting simulating solar radiation
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