两级后置纯膜MBBR的反硝化性能研究
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摘要
为研究纯膜移动床生物膜反应器(MBBR)作为深度反硝化脱氮生物处理工艺的性能,采用两级纯膜MBBR反应器,以某市政污水处理厂二沉池出水为处理对象,以乙酸钠为外加碳源,经过278 d,从启动、处理效果和负荷、碳源利用效率等方面进行了中试。系统历经启动、稳定运行、碳氮比调整和低温运行4个阶段,结果表明:两级后置MBBR反硝化系统总出水ρ(NO_3~--N)<5 mg/L; 10℃时第1级反硝化负荷为0. 45 kg/(m~3·d),第2级反硝化负荷为0. 03～0. 29kg/(m~3·d);在水温为9～28℃时,拟合负荷温度变化系数θ值为1. 026;反应器污泥产率系数为0. 520～0. 542 kg/kg(COD);系统负荷与C/N呈线性关系,C/N适宜控制在4. 0～4. 5,过低则会造成NO_2~--N积累且影响出水NO_3~--N浓度。反应器出水硝态氮浓度低,且脱氮负荷高,表现出较好的低温抗性。
In order to study the performance of pure moving bed biofilm reactor( MBBR) as a deep denitrification process,a two-stage pure MBBR was operated for 278 days to dispose the effluent of second sedimentation of a municipal WWTP. A pilot study was carried out focusing on sodium acetate( as an additional carbon source),startup,treatment effect and load,carbon source utilization efficiency,etc. The whole test cycle was divided into start-up stage,stable operation stage,carbon and nitrogen ratio adjustment stage and low temperature operation stage. It was indicated that the total nitrate concentration in the two-stage post-MBBR was no more than 5 mg/L; the first stage denitrifying load was 0. 45 kg/( m~3·d) and the denitrifying load of the second stage was 0. 03 ～ 0. 29 kg/( m~3·d) under 10 ℃; when the water temperature was in 9 ～ 28 ℃,the temperature change coefficient was 1. 026,showing its good resistance to low temperature; sludge yield coefficient was 0. 520 ～0. 542 kg/kg( COD); the system was greatly affected by carbon source,and the load was in a linear relationship with C/N,which was suitable if controlled in the range of 4. 0 ～ 4. 5. Too low value of C/N would lead to the accumulation of nitrous and affect the nitrate concentration in effluent. The system featured a high nitrate treating load and low concentration in the effluent.
In order to study the performance of pure moving bed biofilm reactor( MBBR) as a deep denitrification process,a two-stage pure MBBR was operated for 278 days to dispose the effluent of second sedimentation of a municipal WWTP. A pilot study was carried out focusing on sodium acetate( as an additional carbon source),startup,treatment effect and load,carbon source utilization efficiency,etc. The whole test cycle was divided into start-up stage,stable operation stage,carbon and nitrogen ratio adjustment stage and low temperature operation stage. It was indicated that the total nitrate concentration in the two-stage post-MBBR was no more than 5 mg/L; the first stage denitrifying load was 0. 45 kg/( m~3·d) and the denitrifying load of the second stage was 0. 03 ～ 0. 29 kg/( m~3·d) under 10 ℃; when the water temperature was in 9 ～ 28 ℃,the temperature change coefficient was 1. 026,showing its good resistance to low temperature; sludge yield coefficient was 0. 520 ～0. 542 kg/kg( COD); the system was greatly affected by carbon source,and the load was in a linear relationship with C/N,which was suitable if controlled in the range of 4. 0 ～ 4. 5. Too low value of C/N would lead to the accumulation of nitrous and affect the nitrate concentration in effluent. The system featured a high nitrate treating load and low concentration in the effluent.
引文
[1]国家环境保护总局水和废水监测分析方法编委会.水和废水监测分析方法[M]. 4版.北京:中国环境科学出版社,2002.
[2] Shrestha A,Riffat R,Bott C,et al. Denitrification stoichiometry and kinetics of moving bed biofilm reactor[J]. Proceedings of the Water Environment Federation,2009(4):153-165.
[3] Stinson B,Peric M,Neupane D,et al. Design and operating considerations for a post denitrification MBBR to achieve limit of technology effluent NOx<1 mg/L and effluent TP <0. 18 mg/L[J].Proceedings of the Water Environment Federation,2009(30):1225-1254.
[4]周永刚.反硝化生物滤池在污水厂升级改造中的应用[J].中国给水排水,2014,30(24):49-52.
[5]曹相生,钱栋,孟雪征.乙酸钠为碳源时的污水反硝化规律研究[J].中国给水排水,2011,27(21):76-79.
[6] Taljemark K,Aspegren H,Gruvberger C,et al. 10 years of experiences of an MBBR process for post-denitrification[J].Proceedings of the Water Environment Federation,2004(16):355-366.
[7] Motsch S,Fetherolf D,Guhse G,et al. MBBR and IFAS pilot program for denitrification at fairfax county’s noman cole pollution control plant[J]. Water Practice,2007,1(5):1-11.
[8]付昆明,曹相生,孟雪征,等.污水反硝化过程中亚硝酸盐氮的积累规律[J].环境科学,2011,32(6):1660-1664.
[9]谢丽,蔡碧婧,杨殿海,等.亚硝酸积累条件下反硝化脱氮过程动力学模型[J].同济大学学报,2009,37(2):224-228.
[10]高景峰,彭永臻,王淑莹,等.不同碳源及投量对SBR法反硝化速率的影响[J].给水排水,2001,27(5):55-59.
[11]李金诗.不同碳源、C/N比对系统反硝化影响研究[D].武汉:武汉理工大学,2011.
[12] Glass C,Silverstein J A,Oh J. Inhibition of denitrification in activated sludge by nitrite[J]. Water Environment Research,1997,69(6):1086-1093.
[2] Shrestha A,Riffat R,Bott C,et al. Denitrification stoichiometry and kinetics of moving bed biofilm reactor[J]. Proceedings of the Water Environment Federation,2009(4):153-165.
[3] Stinson B,Peric M,Neupane D,et al. Design and operating considerations for a post denitrification MBBR to achieve limit of technology effluent NOx<1 mg/L and effluent TP <0. 18 mg/L[J].Proceedings of the Water Environment Federation,2009(30):1225-1254.
[4]周永刚.反硝化生物滤池在污水厂升级改造中的应用[J].中国给水排水,2014,30(24):49-52.
[5]曹相生,钱栋,孟雪征.乙酸钠为碳源时的污水反硝化规律研究[J].中国给水排水,2011,27(21):76-79.
[6] Taljemark K,Aspegren H,Gruvberger C,et al. 10 years of experiences of an MBBR process for post-denitrification[J].Proceedings of the Water Environment Federation,2004(16):355-366.
[7] Motsch S,Fetherolf D,Guhse G,et al. MBBR and IFAS pilot program for denitrification at fairfax county’s noman cole pollution control plant[J]. Water Practice,2007,1(5):1-11.
[8]付昆明,曹相生,孟雪征,等.污水反硝化过程中亚硝酸盐氮的积累规律[J].环境科学,2011,32(6):1660-1664.
[9]谢丽,蔡碧婧,杨殿海,等.亚硝酸积累条件下反硝化脱氮过程动力学模型[J].同济大学学报,2009,37(2):224-228.
[10]高景峰,彭永臻,王淑莹,等.不同碳源及投量对SBR法反硝化速率的影响[J].给水排水,2001,27(5):55-59.
[11]李金诗.不同碳源、C/N比对系统反硝化影响研究[D].武汉:武汉理工大学,2011.
[12] Glass C,Silverstein J A,Oh J. Inhibition of denitrification in activated sludge by nitrite[J]. Water Environment Research,1997,69(6):1086-1093.