Combination of Coagulation and Ozone Catalytic Oxidation for Pretreating Coking Wastewater

In this study, coagulation, ozone (O3) catalytic oxidation, and their combined process were used to pretreat actual coking wastewater. The effects on the removal of chemical oxygen demand (COD) and phenol in coking wastewater were investigated. Results showed that the optimum reaction conditions were an O3 mass flow rate of 4.1 mg min−1, a reaction temperature of 35 °C, a catalyst dosage ratio of 5:1, and a O3 dosage of 500 mg·L−1. The phenol removal ratio was 36.8% for the coagulation and sedimentation of coking wastewater under optimal conditions of 25 °C of reaction temperature, 7.5 reaction pH, 150 reaction gradient (G) value, and 500 mg·L−1 coagulant dosage. The removal ratios of COD and phenol reached 24.06% and 2.18%, respectively. After the O3-catalyzed oxidation treatment, the phenols, polycyclic aromatic hydrocarbons, and heterocyclic compounds were degraded to varying degrees. Coagulation and O3 catalytic oxidation contributed to the removal of phenol and COD. The optimum reaction conditions for the combined process were as follows: O3 dosage of 500 mg·L−1, O3 mass flow of 4.1 mg·min−1, catalyst dosage ratio of 5:1, and reaction temperature of 35 °C. The removal ratios of phenol and COD reached 47.3% and 30.7%, respectively.


Introduction
Coking wastewater is generated by coal coking and mainly includes residual ammonia water, gas cold sewage, and sewage generated by chemical product refinement [1]. Coking wastewater is a series of phenolic substances, cyanide, petroleum substances, sulfides, ammonia nitrogen and other organic compounds emitted during the coking industry. The industrial wastewater has different water quality depending on the nature of the raw coal used in the production process, the processing technology (including coking and product recovery process), and the carbonization temperature. Generally, coking wastewater can be divided into high-concentration organic wastewater and high-solids suspended wastewater according to wastewater quality. High-concentration organic wastewater, also known as phenol-containing wastewater, mainly contains phenol, cyanide, benzene, ammonia, oil, and high solid suspension. The remaining ammonia water contains high concentrations of ammonia, phenol, cyanide, and oil, which are the main sources of coking wastewater [2]. The remaining ammonia water is combined with direct cooling water for gas cooling, direct steam condensation separation water for crude benzene processing, direct steam condensation separation water for tar refinement, and washing water containing phenol and cyanide [3]. The wastewater of sulfide and oil is collectively referred to as phenol cyanide wastewater. This wastewater has large amounts of water and a complex composition, and it is a typical refractory wastewater in the coking industry. The main organic substances in coking wastewater are phenols, benzenes, heterocyclic compounds, and polycyclic compounds [4]. Among these substances, phenolic compounds, which water after wastewater treatment cannot meet the requirement of discharge standard, the water quality of the basin will be polluted and deteriorated, causing deterioration of water quality and ecological damage. Pollution control of large industrial enterprises on both sides of the river is the focus of healthy watershed management. The control of pollutants entering into the river can be achieved by controlling the drainage water quality of enterprises on both sides of the river. Therefore, the advanced treatment of coking wastewater is strengthened to meet the discharge standard. This has positive implications for healthy watershed management and point source pollution control.
In this study, coagulation, O 3 catalytic oxidation, and their combinations were used to pretreat coking wastewater. The effects of O 3 oxidation and O 3 catalytic oxidation on coking wastewater were compared. The effects of catalyst dosage ratio, O 3 dosage, O 3 mass flow rate, reaction temperature, and hydrogen peroxide (H 2 O 2 ) dosage on the catalytic oxidation performance of O 3 were evaluated. Moreover, the effect of coking wastewater on a separate coagulation process was assessed. The treatment effect of combined coagulation + O 3 catalytic oxidation on coking wastewater was investigated, and the possible degradation mechanism was analyzed through ultraviolet (UV) spectroscopy and gas chromatography-mass spectrometry (GC-MS).

Experimental Materials
The experimental wastewater used in this study was obtained from the ammonia distillation tower of a coking plant in Zhangjiagang City, Jiangsu Province. COD reached 3900-4200 mg·L −1 , the chroma was more than 500 times, and pH was 10 ± 0.5. The raw water quality of coking wastewater is shown in Table 1.

Test Methods
An O 3 generator (Ozone generator, CF-G-3-010g, Qingdao Guolin Company, Qingdao, China) and an O 3 detector (LontecLT-200B, Qingdao Langke Electronic Technology Co., Ltd., Qingdao, China) using pure oxygen were employed in this study. O 2 /O 3 mixed gas was generated by the O 3 generator for the gas source. The O 2 /O 3 mixed gas was placed in a homemade plexiglass reactor in a digital thermostatic water bath (85-2, Jiangsu Jinyi Instrument Technology Co., Ltd., Changzhou, China). An electronic balance (P224, Sartorius, Göttingen, Germany) was used to measure a certain amount of catalyst solids, and a cylinder was adopted to obtain a certain amount of wastewater. A peristaltic pump (YZ1515X, Lange Constant Flow Pump Co., Ltd., Baoding, China) was utilized to recycle the wastewater inside the O 3 reactor. The same electronic balance was utilized to weigh a certain amount of coagulant, which was added with a specific amount of distilled water and made to pass through a temperature-controlled magnetic stirrer (HH-S1, Jiangsu Gold Yi Instrument Technology Co., Ltd., Huaian, China). Stirring was performed for 10 min to obtain a coagulant. The pretreatment of coking wastewater through O 3 catalytic oxidation was investigated via a single-factor optimization test to determine the effect of catalyst addition amount, O 3 dosage, H 2 O 2 dosage, and initial reaction temperature on the treatment of phenol in distilled ammonia wastewater. In optimal reaction conditions, coagulation and sedimentation pretreatment of coking wastewater were investigated via a single-factor optimization test to assess the effect of single and composite coagulants on COD and phenol treatment in steamed ammonia wastewater and determine the best response in the single-factor optimization test. Then, the O 3 catalytic oxidation test, coagulation reaction experiment, and H 2 O 2 under optimal conditions were combined to determine the optimal reaction conditions of the combined process.
The experimental values are the average of three experiments with a relative error of less than 10%.
Water quality analysis was conducted using standard methods. The concentration of the phenol solution was determined with a UV spectrophotometer. The absorbance of the standard-concentration phenol solution was determined with a UV-visible spectrophotometer (UV2600, Shimadzu Corporation, Kyoto, Japan). The phenol concentration for the concentration-absorbance standard curve was determined based on the absorbance and standard curve of the phenol solution to be tested. COD was determined based on the national standard GB 11914-1989, and the color of wastewater was determined based on the national standard GB11903-89.

Effect of Catalyst and O 3 on O 3 Catalytic Oxidation and Phenol Removal
The effect of the catalyst and O 3 on the catalytic oxidation of O 3 to phenol is shown in Figure 1. The test conditions were as follows: The starting phenol concentration of the wastewater was 1060 mg·L −1 , the reaction temperature was 25 • C, and the O 3 mass flow rate was 2 mg·min −1 . As shown in Figure 1, the phenol removal ratio could reach up to 11.2% with the increase in reaction time when no catalyst was added to the reaction system and the O 3 dosage was 250 mg·L −1 . When the O 3 dosage increased to 500 mg·L −1 , the removal efficiency of phenol increased significantly, and the highest removal ratio was 24.2%. The removal ratio of phenol was remarkably improved when a catalyst was added to the reaction system. The removal ratio of O 3 was 15.9% when the dosage was 250 mg·L −1 , and the removal ratio was 30.9% when the O 3 dosage was 500 mg·L −1 . catalyst was added to the reaction system. The removal ratio of O3 was 15.9% when the dosage was 250 mg·L −1 , and the removal ratio was 30.9% when the O3 dosage was 500 mg·L −1 . O3 is the direct driving force of the degradation of organic matter, and its dosage directly affects the rate and effect of its catalytic oxidation [22]. As shown in Figure 1, the removal effect of phenol on the reaction system was remarkably improved when the O3 dosage was increased. O3 can directly react with organic substances in water in the form of molecules, and an increase in O3 dosage can accelerate the reaction [23]. The removal ratio of phenol rapidly increased when the catalyst was added to the reaction system because the catalyst offered an active site for the catalytic oxidation of O3, which could provide a three-phase reaction interface by adsorbing O3, water, and organic matter and increase O3 doping. The amount was beneficial to the mass transfer of the three-phase interface, which accelerated the reaction rate and further increased the removal ratio of phenol in the coking wastewater of the reaction system [24]. In summary, the catalyst is an indispensable factor of the O3 catalytic oxidation reaction system. Increasing the O3 dosage aids in improving the removal ratio of phenol.

Effect of Catalyst Dosage Ratio on O3 Catalytic Oxidation Performance of Phenol Removal
The effect of catalyst dosage ratio on the catalytic removal of phenol by O3 oxidation is shown in Figure 2. The test conditions were as follows: The initial phenol concentration of the wastewater was 1060 mg·L −1 , the O3 dosage was 500 mg·L −1 , the O3 mass flow rate was 4.1 mg·min −1 , and the reaction temperature was 25 °C. As shown in Figure 2, the removal efficiency of phenol in the reaction system increased with the increase in catalyst addition ratio. The removal ratio of phenol was optimal when the catalyst dosage ratio was increased to 5:1, which is 34.3%.
As shown in Figure 2, the removal ratio of phenol rapidly increased with the increase in the volume ratio of the catalyst probably because the initial concentration of phenol was high, and the reaction system was in the case where the O3 dosage was unchanged [25]. The effective site of the surface increased with the increase in catalyst dosage and helped in catalyzing O3 in order to produce a high concentration of OH, which made the reaction thorough. In summary, the optimum catalyst dosage ratio of the O3 catalytic oxidation reaction system was 5:1. O 3 is the direct driving force of the degradation of organic matter, and its dosage directly affects the rate and effect of its catalytic oxidation [22]. As shown in Figure 1, the removal effect of phenol on the reaction system was remarkably improved when the O 3 dosage was increased. O 3 can directly react with organic substances in water in the form of molecules, and an increase in O 3 dosage can accelerate the reaction [23]. The removal ratio of phenol rapidly increased when the catalyst was added to the reaction system because the catalyst offered an active site for the catalytic oxidation of O 3 , which could provide a three-phase reaction interface by adsorbing O 3 , water, and organic matter and increase O 3 doping. The amount was beneficial to the mass transfer of the three-phase interface, which accelerated the reaction rate and further increased the removal ratio of phenol in the coking wastewater of the reaction system [24]. In summary, the catalyst is an indispensable factor of the O 3 catalytic oxidation reaction system. Increasing the O 3 dosage aids in improving the removal ratio of phenol.

Effect of Catalyst Dosage Ratio on O 3 Catalytic Oxidation Performance of Phenol Removal
The effect of catalyst dosage ratio on the catalytic removal of phenol by O 3 oxidation is shown in Figure 2. The test conditions were as follows: The initial phenol concentration of the wastewater was 1060 mg·L −1 , the O 3 dosage was 500 mg·L −1 , the O 3 mass flow rate was 4.1 mg·min −1 , and the reaction temperature was 25 • C. As shown in Figure 2, the removal efficiency of phenol in the reaction system increased with the increase in catalyst addition ratio. The removal ratio of phenol was optimal when the catalyst dosage ratio was increased to 5:1, which is 34.3%. The effect of O3 dosage rate on the catalytic removal of phenol by O3 is shown in Figure 3. The test conditions were as follows: The initial phenol concentration of the wastewater was 1060 mg·L −1 , the O3 dosage was 500 mg·L −1 , the catalyst dosage ratio was 5:1, and the reaction temperature was As shown in Figure 2, the removal ratio of phenol rapidly increased with the increase in the volume ratio of the catalyst probably because the initial concentration of phenol was high, and the reaction system was in the case where the O 3 dosage was unchanged [25]. The effective site of the surface increased with the increase in catalyst dosage and helped in catalyzing O 3 in order to produce a high concentration of OH, which made the reaction thorough. In summary, the optimum catalyst dosage ratio of the O 3 catalytic oxidation reaction system was 5:1.

Effect of O 3 Mass Flow on O 3 Catalytic Oxidation Performance of Phenol Removal
The effect of O 3 dosage rate on the catalytic removal of phenol by O 3 is shown in Figure 3. The test conditions were as follows: The initial phenol concentration of the wastewater was 1060 mg·L −1 , the O 3 dosage was 500 mg·L −1 , the catalyst dosage ratio was 5:1, and the reaction temperature was 25 • C. As shown in Figure 3, the removal ratio of phenol increased with the decrease in O 3 dosage rate, but the reaction equilibrium time was extended. Phenol removal occurred when the O 3 mass flow rate was 5.6 mg·min −1 and the reaction time was 90 min. The rate of phenol removal was 35.2% when the mass flow rate of O 3 was 2.1 mg·min −1 and the reaction time was 240 min. The phenol removal ratio was 34.8% when the mass flow rate of O 3 was 4.1 mg·min −1 and the reaction time was 120 min. The effect of O3 dosage rate on the catalytic removal of phenol by O3 is shown in Figure 3. The test conditions were as follows: The initial phenol concentration of the wastewater was 1060 mg·L −1 , the O3 dosage was 500 mg·L −1 , the catalyst dosage ratio was 5:1, and the reaction temperature was 25 °C. As shown in Figure 3, the removal ratio of phenol increased with the decrease in O3 dosage rate, but the reaction equilibrium time was extended. Phenol removal occurred when the O3 mass flow rate was 5.6 mg·min -1 and the reaction time was 90 min. The rate of phenol removal was 35.2% when the mass flow rate of O3 was 2.1 mg·min −1 and the reaction time was 240 min. The phenol removal ratio was 34.8% when the mass flow rate of O3 was 4.1 mg·min -1 and the reaction time was 120 min. The removal ratio of phenol increased with the decrease in O3 dosage rate. However, the reaction rate significantly decreased, and the removal ratio was stable. When the O3 dosage rate was too large, it accelerated the reaction rate and made the reaction reach equilibrium quickly; however, it easily caused the O3 that participated in the reaction to directly overflow from the reaction The removal ratio of phenol increased with the decrease in O 3 dosage rate. However, the reaction rate significantly decreased, and the removal ratio was stable. When the O 3 dosage rate was too large, it accelerated the reaction rate and made the reaction reach equilibrium quickly; however, it easily caused the O 3 that participated in the reaction to directly overflow from the reaction system. Conversely, the decrease in O 3 dosing rate was beneficial to the increase in O 3 [26]. The reaction time between water and organic matter, that is, in three phases, made the reaction thorough [27]. Considering the economic cost and time benefit, the optimal O 3 mass flow rate of the O 3 catalytic oxidation reaction system was 4.1 mg·min −1 .

Effect of O 3 Dosage on O 3 Catalytic Oxidation Performance of Phenol Removal
The effect of O 3 dosage on the catalytic removal of phenol by O 3 is shown in Figure 4. The test conditions were as follows: the starting phenol concentration of the wastewater was 1060 mg·L −1 , the O 3 mass flow rate was 4.1 mg·min −1 , the catalyst dosage ratio was 5:1, and the reaction temperature was 25 • C. As shown in Figure 4, the increase in phenol removal was not obvious with the increase in O 3 dosage. The phenol removal ratio steadily rose with the increase in O 3 dosage. The phenol removal ratio reached 34.8% when the dosage was 500 mg·L −1 . The increase in phenol removal ratio was reduced by the increase in O 3 dosage.
As shown in Figure 4, the removal ratio of phenol increased with the increase in O 3 dosage because the content of •OH in the reaction system was remarkably increased by the increase in O 3 concentration, which was beneficial to the sufficient contact of •OH with organic molecules [28]. It promoted the cleavage of macromolecular chains and groups, such as benzene rings. Thus, macromolecular substances were easily oxidized into small molecular substances, thereby improving the removal effect of phenol [29]. The growth rate of the phenol removal ratio was reduced by the increase in O 3 dosage because the content of phenol in the reaction system decreased as the reaction progressed, and the collision probability of •OH formed by O 3 decreased [30]. The possibility of reaction with other substances increased, resulting in a decrease in rate. Taking into account the economic cost, the optimal O 3 dosage of the O 3 catalytic oxidation reaction system was 500 mg·L −1 .
the increase in O3 dosage. The phenol removal ratio steadily rose with the increase in O3 dosage. The phenol removal ratio reached 34.8% when the dosage was 500 mg·L −1 . The increase in phenol removal ratio was reduced by the increase in O3 dosage.
As shown in Figure 4, the removal ratio of phenol increased with the increase in O3 dosage because the content of •OH in the reaction system was remarkably increased by the increase in O3 concentration, which was beneficial to the sufficient contact of •OH with organic molecules [28]. It promoted the cleavage of macromolecular chains and groups, such as benzene rings. Thus, macromolecular substances were easily oxidized into small molecular substances, thereby improving the removal effect of phenol [29]. The growth rate of the phenol removal ratio was reduced by the increase in O3 dosage because the content of phenol in the reaction system decreased as the reaction progressed, and the collision probability of •OH formed by O3 decreased [30]. The possibility of reaction with other substances increased, resulting in a decrease in rate. Taking into account the economic cost, the optimal O3 dosage of the O3 catalytic oxidation reaction system was 500 mg·L −1 . The effect of reaction temperature on O3 catalytic oxidation to phenol is shown in Figure 5. The test conditions were as follows: the initial phenol concentration of the wastewater was 1060 mg·L −1 , the O3 dosage was 500 mg·L −1 , the O3 mass flow rate was 4.1 mg·min −1 , and the catalyst dosage ratio was 5:1. As shown in Figure 5, the removal effect of phenol initially increased then decreased with the increase in reaction temperature. The optimum removal ratio of phenol was 36.8% when the reaction temperature was 35 °C. The effect of reaction temperature on O 3 catalytic oxidation to phenol is shown in Figure 5. The test conditions were as follows: the initial phenol concentration of the wastewater was 1060 mg·L −1 , the O 3 dosage was 500 mg·L −1 , the O 3 mass flow rate was 4.1 mg·min −1 , and the catalyst dosage ratio was 5:1. As shown in Figure 5, the removal effect of phenol initially increased then decreased with the increase in reaction temperature. The optimum removal ratio of phenol was 36.8% when the reaction temperature was 35 • C. As shown in Figure 5, the removal ratio of phenol increased then decreased with the increase in reaction temperature. An appropriate reaction temperature can increase the activity of hydroxyl radicals, increase the degradation rate of phenol in the reaction system, increase the reaction temperature to some extent, help reduce the activation energy of the catalytic degradation reaction, and make the reaction of OH and organic matter complete [31]. Continuous increase in reaction temperature aggravates the decomposition effect of O3, resulting in a decrease in the actual O3 concentration and a decrease in the removal ratio of phenol [32]. In summary, the optimum reaction temperature for the O3 catalytic oxidation reaction system was 35 °C. The effect of H2O2 dosage on the catalytic removal of phenol by O3 is shown in Figure 6. The test conditions were as follows: the initial phenol concentration of the wastewater was 1060 mg·L −1 , the O3 dosage was 500 mg·L −1 , the O3 mass flow rate was 4.1 mg·min -1 , the catalyst dosage ratio was 5:1, and the reaction temperature was 35 °C. As shown in the figure, the addition of H2O2 to the O3 As shown in Figure 5, the removal ratio of phenol increased then decreased with the increase in reaction temperature. An appropriate reaction temperature can increase the activity of hydroxyl radicals, increase the degradation rate of phenol in the reaction system, increase the reaction temperature to some extent, help reduce the activation energy of the catalytic degradation reaction, and make the reaction of OH and organic matter complete [31]. Continuous increase in reaction temperature aggravates the decomposition effect of O 3 , resulting in a decrease in the actual O 3 concentration and a decrease in the removal ratio of phenol [32]. In summary, the optimum reaction temperature for the O 3 catalytic oxidation reaction system was 35 • C.

Effect of H 2 O 2 Dosage on O 3 Catalytic Oxidation Performance of Phenol Removal
The effect of H 2 O 2 dosage on the catalytic removal of phenol by O 3 is shown in Figure 6. The test conditions were as follows: the initial phenol concentration of the wastewater was 1060 mg·L −1 , the O 3 dosage was 500 mg·L −1 , the O 3 mass flow rate was 4.1 mg·min −1 , the catalyst dosage ratio was 5:1, and the reaction temperature was 35 • C. As shown in the figure, the addition of H 2 O 2 to the O 3 catalytic oxidation reaction system effectively promoted the removal of phenol. The removal ratio of phenol was remarkably improved with the increase in H 2 O 2 dosage, but the growth rate did not show a large increase. The phenol removal ratio increased from 41.1% to 58.4%, the H 2 O 2 dosage increased to 10.0 mg·L −1 , and the phenol removal ratio increased by 3.8% with the increase in H 2 O 2 dosage from 1.0 mg·L −1 to 8.0 mg·L −1 .
As shown in Figure 6, the increase in H 2 O 2 dosage within a certain range accelerated the degradation rate of phenol because H 2 O 2 reacts with Fe 3+ in the reaction system to form Fe 2+ . Fe 2+ can further form •OH with H 2 O 2 , and H 2 O 2 and O 3 can form •OH, which remarkably increases the concentration of •OH in the solution and promotes the degradation of phenol [33]. Excess H 2 O 2 that participates in the reaction has a certain degree of reducibility when the H 2 O 2 dosage exceeds a certain amount [34]. Excess H 2 O 2 inhibits the removal of phenol from the reaction system. In summary, the optimal H 2 O 2 dosage of the O 3 catalytic oxidation reaction system was 8.0 mg·L −1 .

Effect of a Single Coagulant on the Removal of COD and Phenol by Coagulation
The effect of a single coagulant on the removal of COD and phenol by coagulation is shown in Figure 7. The test conditions were as follows: the starting phenol concentration of the wastewater was 1053 mg·L −1 , the COD concentration was 4812 mg·L -1 , the reaction temperature was 25 °C, the reaction pH was 7.5, and the reaction G value was 150. The removal effect of phenol was poor, but a high COD removal ratio was achieved when coking wastewater was treated with a single coagulant. In the comparative test, when compared with the use of polyaluminum chloride (PAC) and composite coagulant coagulants, the use of polyferric sulfate (PFS) as a coagulant achieved better treatment results, and the removal ratios of COD and phenol were 24.06% and 2.18%,

Effect of a Single Coagulant on the Removal of COD and Phenol by Coagulation
The effect of a single coagulant on the removal of COD and phenol by coagulation is shown in Figure 7. The test conditions were as follows: the starting phenol concentration of the wastewater was 1053 mg·L −1 , the COD concentration was 4812 mg·L −1 , the reaction temperature was 25 • C, the reaction pH was 7.5, and the reaction G value was 150. The removal effect of phenol was poor, but a high COD removal ratio was achieved when coking wastewater was treated with a single coagulant.
In the comparative test, when compared with the use of polyaluminum chloride (PAC) and composite coagulant coagulants, the use of polyferric sulfate (PFS) as a coagulant achieved better treatment results, and the removal ratios of COD and phenol were 24.06% and 2.18%, respectively.
As shown in the figure, PFS exhibited the best coagulation effect and a good removal effect on COD and phenol probably because Fe 3+ has the effect of flocculation and sedimentation and possesses certain oxidative properties that can oxidize and degrade organic matter in coking wastewater, thereby reducing its COD content [35]. PAC and composite coagulants do not have the corresponding oxidation properties. In summary, PFS is the best option when using a single coagulant to treat coking wastewater [36].

Effect of a Composite Coagulant on the Removal of COD and Phenol by Coagulation
The effect of a composite coagulant on the removal of COD and phenol by coagulation sedimentation is shown in Figure 8. The test conditions were as follows: The initial phenol concentration of the wastewater was 1053 mg·L −1 , the COD concentration was 4812 mg·L −1 , the reaction temperature was 25 °C, the reaction pH was 7.5, the reaction G value was 150, and the coagulant dosage was 500 mg·L −1 . As shown in the figure, the removal ratio of phenol and COD was low when only PAC was added. The removal of phenol and COD improved when only PFS was added. The removal efficiency of phenol and COD was better than that of PAC when a composite coagulant composed of PFS and polyacrylamide (PAM) was used, but it was not as good

Effect of a Composite Coagulant on the Removal of COD and Phenol by Coagulation
The effect of a composite coagulant on the removal of COD and phenol by coagulation sedimentation is shown in Figure 8. The test conditions were as follows: The initial phenol concentration of the wastewater was 1053 mg·L −1 , the COD concentration was 4812 mg·L −1 , the reaction temperature was 25 • C, the reaction pH was 7.5, the reaction G value was 150, and the coagulant dosage was 500 mg·L −1 . As shown in the figure, the removal ratio of phenol and COD was low when only PAC was added. The removal of phenol and COD improved when only PFS was added. The removal efficiency of phenol and COD was better than that of PAC when a composite coagulant composed of PFS and polyacrylamide (PAM) was used, but it was not as good as that of PFS. The removal ratio of COD showed a downward trend with the decrease in PAM dosage.
The preparation of a composite coagulant directly affects the treatment effect of coking wastewater. Considering that PAM can remarkably increase the viscosity of a composite coagulant, the PFS solution should be prepared first to avoid PAM wrapping the PFS solid [37]. At the same coagulant dosage, the treatment effect using PFS is obviously due to other coagulants and has a certain decolorization effect because Fe 3+ has certain adsorption and oxidation capabilities [38]. Considering that PFS is insoluble in PAM and sufficient Fe 3+ is not released, PAM as a coagulant has no substantial coagulation effect, resulting in a decrease in the treatment effect; however, a certain amount of PAM contributes to the reinforcement [39]. The sedimentation of the body accelerates separation and precipitation [40]. In summary, the ratio of PFS to PAM in the composite coagulant is controlled to some extent for facilitating coagulation and sedimentation treatment of coking wastewater. coagulant dosage, the treatment effect using PFS is obviously due to other coagulants and has a certain decolorization effect because Fe 3+ has certain adsorption and oxidation capabilities [38].
Considering that PFS is insoluble in PAM and sufficient Fe 3+ is not released, PAM as a coagulant has no substantial coagulation effect, resulting in a decrease in the treatment effect; however, a certain amount of PAM contributes to the reinforcement [39]. The sedimentation of the body accelerates separation and precipitation [40]. In summary, the ratio of PFS to PAM in the composite coagulant is controlled to some extent for facilitating coagulation and sedimentation treatment of coking wastewater.

Coagulation + O3 Catalytic Oxidation Treatment of Coking Wastewater
The effect of coagulation + O3 catalytic oxidation on coking wastewater is shown in Figure 9. The coagulation test conditions were as follows: The initial phenol concentration of the wastewater was 1031 mg·L −1 , the COD concentration was 4881 mg·L -1 , the reaction temperature was 25 °C, the reaction pH was 7.5, the reaction G value was 150, the dosage of the composite coagulant was 500 mg·L −1 , and the composite coagulant ratio of Fe2SO4:PAM was 20:1. The O3 catalytic oxidation test conditions were as follows: the O3 dosage was 500 mg·L −1 , the O3 mass flow was 4.1 mg·min -1 , the catalyst dosage ratio was 5:1, the reaction temperature was 35 °C, and the H2O2 dosage was 3.0 mg·L −1 . As shown in the figure, the removal ratio of phenol was 48.1% and the removal ratio of COD was 30.8% when coking wastewater was treated by O3 catalytic oxidation. The removal ratios of phenol and COD reached 49.0% and 34.5%, respectively, when coking wastewater was treated by combined coagulation + ozone catalytic oxidation. This study used a composite coagulant composed of an inorganic coagulant and an organic polymer coagulant. The price of inorganicorganic composite coagulants is similar to that of traditional inorganic polymer coagulants. However, the flocculation effect is improved, the amount of coagulant is reduced, sludge production is reduced, and the amount of coagulant and the cost of water treatment are reduced due to the enhanced adsorption bridging capacity of inorganic-organic composite coagulants [41]. Compared with organic polymer coagulants, the electric neutralization capability is enhanced, the coagulation effect is improved, and the amount of toxic substances remaining in the water is

Coagulation + O 3 Catalytic Oxidation Treatment of Coking Wastewater
The effect of coagulation + O 3 catalytic oxidation on coking wastewater is shown in Figure 9. The coagulation test conditions were as follows: The initial phenol concentration of the wastewater was 1031 mg·L −1 , the COD concentration was 4881 mg·L −1 , the reaction temperature was 25 • C, the reaction pH was 7.5, the reaction G value was 150, the dosage of the composite coagulant was 500 mg·L −1 , and the composite coagulant ratio of Fe 2 SO 4 :PAM was 20:1. The O 3 catalytic oxidation test conditions were as follows: the O 3 dosage was 500 mg·L −1 , the O 3 mass flow was 4.1 mg·min −1 , the catalyst dosage ratio was 5:1, the reaction temperature was 35 • C, and the H 2 O 2 dosage was 3.0 mg·L −1 . As shown in the figure, the removal ratio of phenol was 48.1% and the removal ratio of COD was 30.8% when coking wastewater was treated by O 3 catalytic oxidation. The removal ratios of phenol and COD reached 49.0% and 34.5%, respectively, when coking wastewater was treated by combined coagulation + ozone catalytic oxidation. This study used a composite coagulant composed of an inorganic coagulant and an organic polymer coagulant. The price of inorganic-organic composite coagulants is similar to that of traditional inorganic polymer coagulants. However, the flocculation effect is improved, the amount of coagulant is reduced, sludge production is reduced, and the amount of coagulant and the cost of water treatment are reduced due to the enhanced adsorption bridging capacity of inorganic-organic composite coagulants [41]. Compared with organic polymer coagulants, the electric neutralization capability is enhanced, the coagulation effect is improved, and the amount of toxic substances remaining in the water is relatively small due to the small dosage [42]. As shown in the figure, the removal ratio of COD increased significantly after coagulation and sedimentation treatment, which may be because the floc formed by coagulation precipitation can adsorb some of the negatively charged organic macromolecules, which is beneficial to its oxidation into small molecular organics [43]. In summary, the use of coagulation and sedimentation pretreatment before O 3 catalytic oxidation can improve the removal ratio of phenol and COD in coking wastewater. floc formed by coagulation precipitation can adsorb some of the negatively charged organic macromolecules, which is beneficial to its oxidation into small molecular organics [43]. In summary, the use of coagulation and sedimentation pretreatment before O3 catalytic oxidation can improve the removal ratio of phenol and COD in coking wastewater.

Effect of H2O2 on the Combined Process of Coagulation + O3 Catalytic Oxidation
The effect of H2O2 on the combined process of coagulation + O3 catalytic oxidation is shown in Figure 10. The experimental conditions of O3 catalytic oxidation were as follows: The initial phenol concentration of wastewater was 1044 mg·L -1 , the COD concentration was 4824 mg·L -1 , the O3 dosage was 500 mg·L -1 , the O3 mass flow rate was 4.1 mg·min -1 , and the catalyst dosage ratio was 5:1. The reaction temperature was 35 °C, and the H2O2 dosage was 3.0 mg·L -1 . The coagulation and sedimentation test conditions were as follows: The reaction temperature was 25 °C, the reaction pH was 7.5, reaction G value was 150, the composite coagulant dosage was 500 mg·L -1 , and the composite coagulant ratio was Fe2SO4:PAM = 20:1. As shown in the figure, the removal ratios of phenol and COD in the reaction system were 36.6% and 14.5%, respectively, when H2O2 was not

Effect of H 2 O 2 on the Combined Process of Coagulation + O 3 Catalytic Oxidation
The effect of H 2 O 2 on the combined process of coagulation + O 3 catalytic oxidation is shown in Figure 10. The experimental conditions of O 3 catalytic oxidation were as follows: The initial phenol concentration of wastewater was 1044 mg·L −1 , the COD concentration was 4824 mg·L −1 , the O 3 dosage was 500 mg·L −1 , the O 3 mass flow rate was 4.1 mg·min −1 , and the catalyst dosage ratio was 5:1. The reaction temperature was 35 • C, and the H 2 O 2 dosage was 3.0 mg·L −1 . The coagulation and sedimentation test conditions were as follows: The reaction temperature was 25 • C, the reaction pH was 7.5, reaction G value was 150, the composite coagulant dosage was 500 mg·L −1 , and the composite coagulant ratio was Fe 2 SO 4 :PAM = 20:1. As shown in the figure, the removal ratios of phenol and COD in the reaction system were 36.6% and 14.5%, respectively, when H 2 O 2 was not added. The removal ratios of phenol and COD in the reaction system became 47.3% and 30.7%, respectively, when H 2 O 2 was added.
As shown in Figure 10, the combined process of coagulation + O 3 catalytic oxidation was clearly superior to the combined process of coagulation + O 3 catalytic oxidation, probably because O 3 catalytic oxidation can effectively remove coking after coagulation precipitation [44]. The particulate suspension and some macromolecular organic matter in the wastewater help reduce the consumption of O 3 in the particulate suspension and macromolecular organic matter, and the reaction of oxidative degradation of organic matter is thorough [45]. In summary, the addition of H 2 O 2 helps improve the removal ratio of phenol and COD in coking wastewater, and the best combined process is coagulation + O 3 catalytic oxidation with the addition of H 2 O 2 . added. The removal ratios of phenol and COD in the reaction system became 47.3% and 30.7%, respectively, when H2O2 was added. As shown in Figure 10, the combined process of coagulation + O3 catalytic oxidation was clearly superior to the combined process of coagulation + O3 catalytic oxidation, probably because O3 catalytic oxidation can effectively remove coking after coagulation precipitation [44]. The particulate suspension and some macromolecular organic matter in the wastewater help reduce the consumption of O3 in the particulate suspension and macromolecular organic matter, and the reaction of oxidative degradation of organic matter is thorough [45]. In summary, the addition of H2O2 helps improve the removal ratio of phenol and COD in coking wastewater, and the best combined process is coagulation + O3 catalytic oxidation with the addition of H2O2.

Mechanism Analysis
3.4.1. UV Analysis Figure 11 shows the UV-vis spectrum of the coking wastewater raw water and the effluent of each process. As shown in the figure, the UV light absorption of the raw water of coking  Figure 11 shows the UV-vis spectrum of the coking wastewater raw water and the effluent of each process. As shown in the figure, the UV light absorption of the raw water of coking wastewater was mainly concentrated in the UV region of 190-400 nm. Combined with the source of coking wastewater, we can infer that the main component of the wastewater was aromatic compound. UV254 is a parameter that indicates the content of aromatic compounds in water (including natural organic compounds containing aromatic structures, such as benzenes, phenols, and humus) [46]. UV254 drops the fastest because O 3 can react with C=C on the aromatic ring, resulting in the ring opening of the aromatic ring. The biodegradability of wastewater is remarkably improved with the oxidative degradation of organic compounds containing benzene rings and macromolecular chain structures [47]. wastewater was mainly concentrated in the UV region of 190-400 nm. Combined with the source of coking wastewater, we can infer that the main component of the wastewater was aromatic compound. UV254 is a parameter that indicates the content of aromatic compounds in water (including natural organic compounds containing aromatic structures, such as benzenes, phenols, and humus) [46]. UV254 drops the fastest because O3 can react with C=C on the aromatic ring, resulting in the ring opening of the aromatic ring. The biodegradability of wastewater is remarkably improved with the oxidative degradation of organic compounds containing benzene rings and macromolecular chain structures [47].   Figure S1 shows the gas chromatogram of the coking wastewater raw water and the effluent of each process. As shown in the figure, phenols, heterocyclic compounds, polycyclic aromatic hydrocarbons, and their derivatives were the main components of pollutants in the coking wastewater [48]. They can be detected after O3 catalytic oxidation. The abundance of most organic compounds decreased to varying degrees, indicating that phenols, polycyclic aromatic hydrocarbons, and heterocyclic compounds were degraded to varying degrees after O3-catalyzed  Figure S1 shows the gas chromatogram of the coking wastewater raw water and the effluent of each process. As shown in the figure, phenols, heterocyclic compounds, polycyclic aromatic hydrocarbons, and their derivatives were the main components of pollutants in the coking wastewater [48]. They can be detected after O 3 catalytic oxidation. The abundance of most organic compounds decreased to varying degrees, indicating that phenols, polycyclic aromatic hydrocarbons, and heterocyclic compounds were degraded to varying degrees after O 3 -catalyzed oxidation [49]. As shown in Table 2, the composition of raw water is complicated. After the raw water has been coagulated, the composition has remained basically unchanged. The organic substances such as phenol are reduced by Coagulation + O 3 catalytic oxidation. After Coagulation + O 3 catalytic oxidation with addition of H 2 O 2 process, the content of organic substances, such as phenol, is further reduced. Phenol, 5-methylfurfural, 4,5-dimethyl-2-hydroxypyrimidine, 2,3,4,5-tetramethyl-2-cyclopentenone, 4,5,6 trimethyl-2 -pyrimidinone, 2-hydroxy-4,4-dimethyl-3-indolyl-2-cyclopentanone, N-phenylformamide, quinoline, 2,3-dihydroindole-4-Alcohol-2-ketone

Application of Coagulation and Ozone Catalytic Oxidation in Healthy Watershed Management
In the healthy watershed management, it is extremely important to strengthen point source pollution in the basin. Point source pollution is mainly a relatively concentrated sewage discharge point such as sewage discharge. Its characteristics are concentrated, polluting, destructive and relatively easy to control. If the point source pollutant load exceeds the water environment capacity, it will cause pollution to the water quality of the basin and damage to the watershed ecology. Therefore, internship point source pollution control and end treatment must meet the needs of watershed environmental protection. Additionally, in view of the lack of clean water in rivers, the water quality standards and requirements of sewage treatment plants should be reasonably improved, and the effluent quality of sewage treatment plants should be upgraded to achieve recreational water for reclaimed water. It can be used as one of the ecological water sources of watersheds or lakes, and overall planning of water transfer measures in the outer basin, to achieve the improvement of water environment in the basin and lake under the most acceptable conditions of economic costs. The technology and results of this research are mainly aimed at point source pollution control technology in watershed management and watershed management. Therefore, applying the results of this study to point source pollution control in healthy watersheds has a positive impact.

Conclusions
In this study, coagulation + O 3 catalytic oxidation was used to pretreat coking wastewater. In the treatment of coking wastewater by O 3 catalytic oxidation alone, increasing the O 3 dosage helped improve the removal ratio of phenol. In the best working condition, the mass flow rate of O 3 was 4.1 mg·min −1 , the reaction temperature was 35 • C, and the catalyst dosage ratio was 5:1. The phenol removal ratio was 36.8% when the O 3 dosage was 500 mg·L −1 . PFS was more suitable for coking wastewater than PAC and composite coagulant when coking wastewater was treated by coagulation, and the ratio of PFS to PAM in the composite coagulant was controlled to some extent. In the combined process, the use of coagulation and precipitation pretreatment before O 3 catalytic oxidation helped to improve the removal ratio of phenol and COD in coking wastewater. The addition of H 2 O 2 significantly improved the treatment effect. The removal ratios of phenol and COD in the O 3 catalytic oxidation + H 2 O 2 + coagulation reaction system reached 47.3% and 30.7%, respectively. At this time, the O 3 dosage was 500 mg·L −1 . The O 3 mass flow rate was 4.1 mg·min −1 , the catalyst dosage ratio was 5:1, the reaction temperature was 35 • C, and the H 2 O 2 dosage was 3.0 mg·L −1 . The coagulation sedimentation test conditions were as follows: The reaction temperature was 25 • C, the reaction pH was 7.5, the reaction G value was 150, the composite coagulant dosage was 500 mg·L −1 , and the composite coagulant ratio was Fe 2 SO 4 :PAM = 20:1. After O 3 -catalyzed oxidation treatment, phenols, polycyclic aromatic hydrocarbons, and heterocyclic compounds were degraded to varying degrees. Hence, O 3 catalytic oxidation can remarkably improve the biodegradability of wastewater. This study uses the actual coking wastewater as the research object, and the research results can provide theoretical basis and engineering reference for the actual project.