To get an optimized pulsed electrical plasma discharge reactor and to increase the energy utilization efficiency in the removal of pollutants,two hybrid plasma discharge reactors were designed and optimized.The reactors were compared via the discharge characteristics,energy transfer efficiency,the yields of the active species and the energy utilization in dye wastewater degradation.The results showed that under the same AC input power,the characteristics of the discharge waveform of the point-to-plate reactor were better.Under the same AC input power,the two reactors both had almost the same peak voltage of 22 kV.The peak current of the point-to-plate reactor was 146 A,while that of the wire-to-cylinder reactor was only 48.8 A.The peak powers of the point-to-plate reactor and the wire-to-cylinder reactor were 1.38 MW and 1.01 MW,respectively.The energy per pulse of the point-to-plate reactor was 0.2221 J,which was about 29.4% higher than that of the wire-to-cylinder reactor(0.1716 J).To remove 50% Acid Orange 7(A07),the energy utilizations of the point-to-plate reactor and the wireto-cylinder reactor were 1.02×10^(-9) mol/L and 0.61×10^(-9) mol/L,respectively.In the point-toplate reactor,the concentration of hydrogen peroxide in pure water was 3.6 mmol/L after 40 min of discharge,which was higher than that of the wire-to-cylinder reactor(2.5 mmol/L).The concentration of liquid phase ozone in the point-to-plate reactor(5.7×10^(-2) mmol/L) was about 26.7% higher than that in the wire-to-cylinder reactor(4.5×10^(-2) mmol/L).The analysis results of the variance showed that the type of reactor and reaction time had significant impacts on the yields of the hydrogen peroxide and ozone.The main degradation intermediates of A07 identified by gas chromatography and mass spectrometry(GCMS) were acetic acid,maleic anhydride,pbenzoquinone,phenol,benzoic acid,phthalic anhydride,coumarin and 2-naphthol.Proposed degradation pathways were elucidated in light of the analyzed degradation products.
In order to realize hydrogen generation under visible light, novel CdS/TiO_2 nanotubes arrays are de- veloped by electrochemical anodization of Ti in 0.15 mol/L NH_4F + 0.08mol/L H_2C_2O_4 electrolyte. The diameter of the nanotube is 80―100nm and the length is approximately 550 nm. The CdS nano-particles are deposited on the TiO_2 nanotubes arrays by chemical bath deposition (CBD) in the ammonia-thiourea system. A 300W Xe lamp is used as the light source, CdS/TiO_2 nanotube arrays are used as the photoanode with the application of 1.0V bath voltage, and 0.1 mol/L Na_2S + 0.04 mol/L Na_2SO_3 solution is used as the electrolyte, then the rate of photoelectrocatalytic hydrogen generation is 245.4 μL/(h·cm^2). This opens new perspectives for photoelectrocatalytic hydrogen generation by using CdS/TiO_2 nanotubes arrays.
Fabrication and S-F-codoping of TiO2 nanotubes were carried out by a one-step electrochemical ano-dization process to extend the photoresponse of TiO2 to the visible-light region. The prepared samples were annealed in air and detected by SEM,XRD,XPS and UV-vis DRS spectrophotometer. The results showed that the average tube diameter of the nanotubes was 150 nm and the average tube length was 400 nm. The doped TiO2 nanotubes exhibited strong absorption in visible-light region. Photoelectro-catalytic degradation efficiency of 4-CP over S-F-codoped TiO2 nanotubes was 39.7% higher than that of only-F-doped sample. Moreover,sulfur and fluorine codoped into substitutional sites of TiO2 had been proven to be indispensable for strong response and high photocatalytic activity under visible light,as assessed by XPS.
A small scale isotropic mass transfer model was developed for the local liquid side mass transfer coefficients in gas-liquid-solid three-phase flow airlift loop reactor for Newtonian and non-Newtonian fluids. It is based on Higbie's penetration theory and Kolmogoroff's theory of isotropic turbulence with kl=3√2D∈11/3/π(η1^-1/3-λf^-1/3)where e1 is local rate of energy dissipation, Af is the local microscale, r/l is the local Kolmogoroff scale and D is the diffusion coefficient. The capability of the proposed model is discussed in the light of experimental data obtained from 12 L gas-liquid-solid three-phase flow airlift loop reactor using Newtonian and non-Newtonian fluids. Good agreement with the experimental data was obtained over a wide range of conditions suggesting a general applicability of the proposed model.
