Fe salts as catalyst for the wet oxidation of o-chlorophenol

Fe salts as catalyst for the wet oxidation of o -chlorophenol first-author †E-mail:xhxu@hzcnc.com †E-mail:xhxu@hzcnc.com xhxu@hzcnc.com Department of Environmental Engineering, Zhejiang University, Hangzhou 310027, China Department of Environmental Engineering, Zhejiang University, Hangzhou 310027, China Catalytic wet air oxidation (CWAO) of o -chlorophenol in wastewater was studied in a stainless steel autoclave using four different Fe catalysts in the temperature range of 100–200 °C. Experimental results showed that high rate of o -chlorophenol and COD Cr (Chemical Oxygen Demand, mg/L) removal by CWAO was obtained at relatively low temperature and pressure. The catalysts Fe 2 (SO 4 ) 3 , FeSO 4 , Fe 2 O 3 and FeCl 3 all exhibited high catalytic activity. More than 93.7% of the initial COD Cr and nearly 100% of o -chlorophenol were removed at 150 °C after 150 min with FeSO 4 as catalyst. The CWAO of o -chlorophenol was found to be pseudo-first order reaction with respect to o -chlorophenol, with activation energy of 75.56 kJ/mol in the temperature range of 100–175 °C. Fe o -chlorophenol Catalytic wet air oxidation Kinetic INTRODUCTION 1 Chlorophenols (CPs) are chemicals widely used in industry to manufacture insecticides, herbicides, fungicides, biocides, and dye, are also found in the effluent of the pulp and paper mill industry, and are mainly man-made compounds, and have been recognized as organic pollutants of air, groundwater, soil and sediments. They are carcinogenic and stable in water. Most chlorophenols are listed as priority pollutants by the US Environmental Protection Agency ( 1988 1988 ) due to their toxicity and persistence. Their fate in the environment is of great importance. Of particular interest is their reactivity by oxidation treatment, including wet air oxidation, ozonation, UV-Fenton oxidation and other advanced oxidation technologies. Among all the wet oxidation technologies, WAO, which can mineralise pollutants at elevated temperature and pressure, has the ability to convert most organic and inorganic compounds into end products such as minerals, carbon dioxide and water (Shende and Mahajani, 1997 1997 ; Santos et al., 2001 2001 ). WAO has been demonstrated as a viable process for o -chlorophenol wastewater treatment (Lin et al., 1999 1999 ; Lin and Wang, 1999 1999 ; 2000 2000 ; Lei and Wang, 2000 2000 ). Practically, WAO can be implemented in a wide range of temperature and pressure. Temperature is recognized as the most important process parameter. Pressure is required to maintain the water in liquid state and provide an overpressure of oxygen. CWAO has been successfully applied for the treatment of wastewater discharged from various sources such as petroleum and petrochemical industries, and pulp and paper mills, and has become one of the attractive technologies for the treatment of wastewater containing a small amount of pollutants to be incinerated, while still containing high concentration of toxic materials for biological treatment carried out under extreme reaction conditions and involves high operation and installation costs. Therefore, the development of CWAO has been attempted in order to mitigate the severe reactions and enhance the treatment efficiency. CWAO reactions are of interest for reducing the high temperature and pressure requirements of conventional WAO processes. The partial or total replacement of oxygen with a stronger oxidant, such as hydrogen peroxide, also has been applied and is finding increasing use for enhancing the reaction rate (Lei and Wang, 2000 2000 ). Homogeneous copper salts are known as widely effective catalysts for many kinds of organic compounds and are used in the practical wastewater treatment (Robert and Robert, 1985 1985 ; Wu et al., 1987 1987 ; Li et al., 1991 1991 ; Lei and Wang, 2000 2000 ; Wu et al., 2003 2003 ), but the copper salts will cause heavy metal pollution after treatment, so it will be more interesting to choose iron salts or ferric oxide as catalysts in CWAO. EXPERIMENTS AND METHODS 1 Chemicals 2 Fe 2 (SO 4 ) 3 , FeSO 4 , Fe 2 O 3 and FeCl 3 ( > 99%, AR), o -chlorophenol ( > 98.5%, CR), methanol (reagent for HPLC, > 99.9%). These reagents were purchased from Shanghai Chemical Reagents Company. Batch experimental procedures 2 Reactions were carried out in a 1 L stainless steel autoclave equipped with automatic temperature control, an adjustable speed stirrer, a tachometer, a valve for sampling and a pressure gauge (Fig. 1 1 ). Five-hundred ml wastewater and catalysts (when needed) were introduced into the autoclave, which was heated with an electrical heating jacket under the pressure of nitrogen, while a magnetic agitator continuously stirred the solution. After reaching the desired reaction temperature, oxygen was forced into the autoclave and the time was recorded as the starting point of the reaction. At appropriate time intervals, an aliquot of the solution was withdrawn, and samples after filtered and taken for analysis. Analytical method 2 o -chlorophenol was measured by HPLC. Analysis parameters were as follows: Instrument: Waters High Performance Liquid Chromatography. Column: Nova-Pak C18, 4 μm, 3.9 mm×150 mm. Mobile phase: MeOH/H 2 O (80/20). Flow rate: 1.0 ml/min. Detector: UV at 254 nm. Column temperature: 35 °C. Sample size: 20 μl. RESULTS AND DISCUSSION 1 Effect of addition of catalyst 2 Catalysts in the form of metal salt solution were added to the reactor to enhance the oxidation. Different Fe catalysts including Fe 2 (SO 4 ) 3 , FeSO 4 , Fe 2 O 3 and FeCl 3 were tested. The amount of catalysts in terms of metal ion (Fe) concentration added to the reactor was 100 mg/L. Reaction conditions were kept constant at a temperature of 150 °C, and an oxygen partial pressure of 0.3 MPa throughout the test. The wastewater treatment results are shown in Fig. 2 2 as COD Cr and o -chlorophenol removal versus reaction time. Addition of a catalyst significantly enhanced, the efficiency of wastewater treatment. The highest COD Cr removal achieved was about 93.7% after 150 min of reaction. Generally, the COD Cr removals were approximately three times that obtained without adding catalyst under the same reaction conditions. The o -chlorophenol removals were determined as 86.7%, 75.0%, 63.7%, 55.2% and 30.8% at 5 min with FeSO 4 , FeCl 3 , Fe 2 O 3 , Fe 2 (SO 4 ) 3 and no other catalyst, respectively, and more than 99.9% o -chlorophenol was removed by CWAO after 30 min reaction. Among these four Fe catalysts, the activity order was FeSO 4 > FeCl 3 > Fe 2 O 3 > Fe 2 (SO 4 ) 3 . However, in the absence of the above catalysts, COD Cr removal was only 30.4% at the end of the treatment. Initial conditions: COD Cr,in , 2000 mg/L; P O 2 , 0.30 MPa at 25 °C; pH, 6.0; T =150 °C; Catalys: 100 mg/L (total metal content): ○: No other catalyst; □: Fe 2 (SO 4 ) 3 ; ◊: Fe 2 O 3 ; ×: FeCl 3 ; Δ: FeSO 4 The effect of the amount of catalyst used 2 To obtain the optimal catalyst for CWAO, experiments were done with various amounts of Fe(II). Fig. 3 3 shows the percentage degradation of COD Cr and o -chlorophenol as a function of the amount of Fe(II) (FeSO 4 was added) added. As expected, the COD Cr and o -chlorophenol removal process was greatly expedited with increasing amount of iron salt. A COD Cr removal of 93.7% was achieved after two and a half hour reaction time with Fe(II) level of 100 mg/L while only 53.3% of COD Cr was removed when the dosage of Fe(II) dropped to 25 mg/L. The o -chlorophenol removal also could increase from 59.14% to over 99.98% after 30 min for different catalyst added. Initial conditions: COD Cr,in , 2000 mg/L; P O 2 , 0.30 MPa at 25 °C; pH, 6.0; T , 150 °C; FeSO 4 , total metal content: ○: No other catalyst; Δ: 25 mg/L; □: 50 mg/L; ◊: 100 mg/L The influence of temperature 2 The treatment of o -chlorophenol wastewater by CWAO in the absence of FeSO 4 was studied. This was conducted at temperature of 100 °C to 175 °C, and the oxygen partial pressure was kept at 0.30 MPa at a reference temperature of 25 °C. The progression of the oxidation process at various temperatures with CWAO is shown in Fig. 4 4 showing that the catalytic reaction rate can be considerably increased with increasing temperature increasing. The o -chlorophenol removal rate can be increased from less than 10% to over 99% after 30 min, and the final COD Cr removal level can be increased from around 10.5% to 73.6% with the reaction temperature of 100 °C to 175 °C. Initial conditions: COD Cr,in , 2000 mg/L; P O 2 , 0.30 MPa at 25 °C; pH, 6.0; FeSO 4 , total metal content 50 mg/L; T (°C): □: 100; ◊: 125; ○: 150; ∆: 175 Reaction kinetics 2 If the initial oxygen concentration is much greater than initial o -chlorophenol concentration, the oxygen concentration can be considered practically invariable during the reaction, so it is possible to approximate the expression to pseudo-first order given the equation: $$- \ln \frac{{C_{{\text{CP}}} }}{{C_{{\text{CP}}} _0 }} = kt$$ As shown in Table 1 1 , in all the experiments, initial oxygen concentration was fixed at great excess over the stoichiometric concentration needed to oxidize o -chlorophenol completely. Thus, the rate constant ( k ) can be calculated from the slope of the straight line obtained when ln( C CP /C CP0 ) is represented versus time in the period in which rapid oxidation occurs. Run Catalyst Fe (mg/L) T (°C) k (min −1 ) 1 No catalyst 0 150 0.0278 2 FeSO 4 100 150 0.2926 3 FeCl 3 100 150 0.2468 4 Fe 2 O 3 100 150 0.2505 5 Fe 2 (SO 4 ) 3 10 150 0.2367 6 FeSO 4 25 150 0.0643 7 FeSO 4 50 150 0.0936 8 FeSO 4 50 100 0.0030 9 FeSO 4 50 125 0.0219 10 FeSO 4 50 175 0.1441 Following this procedure, k values were calculated for all temperature studied. These values are presented in Table 1 1 , showing that k increases with the increasing temperature. Assuming that k has an Arrhenius behaviour, the activation energy, E a , can be calculated by linear fitting of ln k versus 1/ T : $$\ln k = A - \frac{{E_{\text{a}} }}{{{\text{R}}T}}$$ where E a is the activation energy (kJ/mol), A the pre-exponential factor, k the observed pseudo-first-order reaction rate constant (min −1 ), R the universal gas constant (8.314 J/(mol·K)), and T is the reaction temperature (K). The effect of reaction temperature on the effectiveness of the removal efficiency was studied by varying the reaction temperature from 373 to 448 K. By rearranging the experiment data shown in Fig. 4 4 , a linear decrease of ln( C CP / C CP0 ) with time is obtained. This linear relationship reveals a pseudo-first-order reduction reaction regarding the removal efficiency. As a result, the reaction rate constants ( k ) were determined to be 0.003, 0.0219, 0.0936, and 0.1441 min −1 , respectively, with a reaction temperature of 100, 125, 150 and 175 °C (Table 1 1 ). As seen in Table 1 1 , an increase in the reaction temperature can enhance the reaction rates significantly. The k values calculated at various temperatures were correlated by Eq.( 1 1 ) and Eq.( 2 2 ) and shown in Fig. 5 5 indicating an estimated activation energy of 75.56 kJ/mol at the temperature range of 373–448 K. ln k =18.16−8847.9/ T CONCLUSION 1 The experimental results of CWAO of o -chlorophenol showed that at low iron concentration exhibited high catalytic activity at relatively low temperature and pressure; and that FeSO 4 has higher catalytic efficiency than other Fe catalysts, Fe 2 (SO 4 ) 3 , Fe 2 O 3 and FeCl 3 . More than 93.7% of the initial COD Cr and nearly 100% of o -chlorophenol were removed at 150 °C in 150 min with FeSO 4 as catalyst. The CWAO of o -chlorophenol was found to be pseudo-first order reaction with respect to o -chlorophenol. The activation energy was found to be 75.56 kJ/mol at the temperature range of 100–175 °C. References L Lei , D Wang . 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Kinetics study on catalytic wet air oxidation of phenol 10.1631/jzus.2005.B0569 Project (No. 20407015) supported by the National Natural Science Foundation of China 2004-12-12 2005-03-21 2005-05-22 2022-01-05 Copyright © 2005, Journal of Zhejiang University Science 2005 Journal of Zhejiang University-SCIENCE B (Biomedicine and Biotechnology) 06 6B