摘要
本文提出了一种回流式生物膜法组合工艺,其以传统的接触氧化法和BAF为基础,同时设置缺氧段,在必要时进行硝化液回流以强化脱氮。该工艺按污水流经次序分为缺氧段(A段)、接触氧化段(O段)‘和BAF段(B段),其中,前两段装填多面空心球填料,而BAF段装填陶粒填料。应用该反应器系统对生活污水进行处理试验,研究了各污染物去除效果及影响因素,确定了该工艺的最优运行参数,并对该工艺中各污染物的去除机理进行了分析,对COD去除动力学模型进行了推导和验证,同时,还对系统的反冲洗机理、方式及强度进行了试验研究。
通过不同试验条件下的污染物去除试验,最终确定出了该生物膜组合工艺在处理生活污水时的最优工艺参数为：水力停留时间(HRT)为6.5 h；O、B段溶解氧(DO)浓度分别控制在3-4 mg／L和6-7 mg/L；回流比为150%。在最优工艺参数条件下,当进水COD平均负荷和氨氮平均负荷分别为290.8 mg/L和42.2mg/L时,反应器对COD、氨氮、总氮及浊度的平均去除率分别为90.83%、98.97%、76.27%及88.66%,此时,反应器出水COD、氨氮、总氮及浊度分别为22～31 mg/L,0.2～0.75 mg/L、9.6～13.3 mg/L及6-10 NTU,其均值分别为26.4 mg/L、0.43 mg/L、11.15 mg/L、7.8 NTU,均满足GB18918-2002中所规定的一级A要求,且可满足部分城市杂用水(GB/T18920-2002)和景观用水(GB/T18921-2002)的标准。反应器对总磷的去除效果较差,其平均去除率仅为37.98%,出水总磷浓度为1.4-1.9 mg/L。
试验结果表明,HRT、DO、R、水温、进水有机负荷和氨氮负荷对污染物的去除均有不同程度的影响。HRT对氨氮的去除影响较大,随着HRT的减小系统氨氮去除率大大降低；O段DO的变化对各项污染物去除的影响较小,而B段DO的变化对氨氮的去除影响较大,当B段DO低于6 mg/L时,该段氨氮去除率大大降低；受回流比变化影响最大的指标是总氮去除,其去除率随回流比的增大呈现先升高后降低的趋势；在HRT为6.5 h时,系统对COD和氨氮的去除率均随水温升高呈现增高趋势,但在HRT为4.25 h时,系统对COD的去除随水温升高有所增高,而此时氨氮的去除率并未明显受到水温变化的影响；进水COD负荷对A-O段COD和氨氮的去除均有影响,前者随进水COD负荷的增加呈现先增加后略有降低的趋势,而后者大体上随COD负荷的增加呈降低趋势；进水COD负荷对B段反应器污染物去除的影响并不明显；A-O段氨氮去除率受其进水氨氮负荷影响较大,该段出水氨氮浓度随进水氨氮负荷的增加呈线性增加趋势。
通过理论推导及试验推求,最终确定了A-O段反应器和B段反应器的COD去除动力学模型分别为：C=C0e-(-0.117R2+0.2958R-0.0037T12+0.1559T1+0.2361)h1和C=C1e-(0.0861R2-0.2837R+0.1834T22-0.5895T2+0.8856)h2；整个系统的COD去除动力学模型为：C2=C0e0.1377R2-0·.2789R-0．0205T2-0.019T-13904。
通过分析及试验验证分别确定了A-O、B段反应器的反冲洗方式及强度。A-O反应器的反冲洗方式和强度：先气、水同时冲洗,再单独用水反冲洗；确定气-水同时反冲洗时的气冲洗强度为12 L／(m2·s),水冲洗强度为4 L／(m2·s),冲洗时间5min,单独水冲洗阶段的水冲洗强度4 L／(m2·s),时间9 min。B反应器的反冲洗方式及强度：先单独气冲洗,再气-水同时反冲洗,最后单独用水漂洗；确定单独气洗阶段的反冲洗强度为18 L／(m2·s),时间4 min,气、水同时冲洗阶段的气洗强度18 L／(m2·s),水冲洗强度为4 L／(m2·s),时间8 min,单独水冲洗阶段的反冲洗强度为4 L／(m2·s),时间3 min。
试验研究表明,该工艺可实现对COD、氨氮、总氮和悬浮物的有效去除,同时对总磷也有一定的去除效果,且该工艺具有占地面积小、操作简单、抗冲击负荷能力强、处理出水水质稳定、尤其是脱氮效果较好等优点,验证了该工艺在分散式污水处理与回用中的可行性。
In this dissertation, a new wastewater treatment process-a combined biofilm reactor was introduced, which was based on the traditional Contact Oxidation Method and BAF and was added anoxic zone. For enhancing nitrogen removal, nitrifying fluid return could be carried out. According to the order of the sewage flow, it was divided into three zones:the anaerobic zone (A), the contact oxidation zone (O) and the BAF (B). Both A and O zones were packed with polypropylene multi-faceted hollow balls and B zone was packed with ceramsite. A lab-scale experiment treating domestic sewage in the combined reactor was conducted. Contaminants removal was investigated and the optimum operational parameters were determined. The mechanics of contaminants removal were analyzed in detail, and kinetic models of COD removal were deduced and inspected. In addition, the mechanics, styles and intensity of backwashing were studied in this experiment.
According to the experimental results under different conditions, the optimum operational parameters were determined as following:HRT was 6.5 h, DO concentrations of O zone and B zone were 3～4 mg/L and 6～7 mg/L, respectively, and nitrifying fluid return ratio(R) was 150%. Under the optimum conditions, with average influent COD of 290.8 mg/L and ammonia of 42.2 mg/L, the average removal efficiency of COD, ammonian, total nitrogen and turbidity were 90.83%,98.97%, 76.27% and 88.66%, respectively, and accordingly, the effluent concentrations were 22～31 mg/L,0.2～0.75 mg/L,9.6～13.3 mg/L and 6～10 NTU, respectively, so their average effluent concentrations were 26.4 mg/L,0.43 mg/L,11.15 mg/L and 8 NTU, respectively, all meeting the A-level standard in GB18918-2002. And some of the four indexes met water quality standard for urban miscellaneous water consumption (GB/T18920-2002) and for scenic environment use (GB/T18921-2002). The removal of total phosphorus was relatively poor, and the average removal efficiency of 37.98% and total phosphorus in effluent of 1.4～1.9 mg/L was just attained.
The experimental results showed that, the changes of HRT, DO, R, temperature, COD concentration and ammonia concentration in influent could influence the removal efficiency of contaminants in varying degrees. The change of HRT made a great effect on ammonia removal, and the removal rate of ammonia dropped greatly with the decrease of HRT. The change of DO made little effect on the removal of contaminants in O zone but made a great effect on the removal of ammonia in B zone. The removal rate of ammonia decreased dramatically when the DO was less than 6 mg/L in B zone. The removal rate of total nitrogen was most obviously influenced by the change of return ratio, presenting the trend of first increase then decrease with the increase of return ratio. With HRT of 6.5 h, the removal rates of COD and ammonia increased with the increase of temperature, while with HRT of 4.25 h, the removal rate of COD increased slightly with the increase of temperature, and the removal of ammonia was hardly affected. COD concentration in influent made different effects on removal rates of COD and ammonia in A-O zone. With the increase of COD concentration, the removal rate of COD ascended firstly, and then descended slightly, but the removal rate of ammonia decreased constantly on the whole. The removal of contaminants in B zone was affected slightly by COD concentration in influent. Ammonia concentration in influent made a great effect on ammonia removal in A-O zone, rendering ammonia concentration in effluent to increase linearly with the increase of ammonia concentration in influent.
By the combined deduction of theory and experiment, the kinetics models of COD removal were achieved as following:C= C0e-(-0.117R2+0.2958R-0.0037T12+0.1559T1+0.2361)h1 (in A-O zone), C=C1e-(0.861R2-0.2837R+0.1834T22-0.5895T2+0.8856)h2 (in B zone). Based on the above two models, the kinetics model C2=C0e0.1377R2-0.2789R-0.0205T2-0.019T-1.3904 of combined biofilm reactor was deduced.
By analyzing in theory and experimental testing, the styles and intensity of backwashing were determined. They were as following:for A-O zone, firstly, simultaneous backwashing with air and water for 5min, under the backwashing intensity of air and water of 12 L/(m2·s) and 4 L/(m2·s), respectively; then, backwashing with water for 9min, under its intensity of 4L/(m2-s). While for B zone, firstly, backwashing with air for 4min, under its intensity of 18 L/(m2-s); then, simultaneous backwashing with air and water for 8 min, under the backwashing intensity of air and water of 18 L/(m2·s) and 4 L/(m2·s), respectively; lastly, backwashing with water for 3min, under its intensity of 4 L/(m2·s).
The experimental results showed the combined biofilm reactor could achieve good removal efficiency of COD, ammonia, total nitrogen and SS, and relatively poor removal efficiency of total phosphorus. And some other advantages, like small footprint, simple operation, good capability of counteracting influent loading fluctuation, steady effluent quality, and especially prominent nitrogen removal were also presented. It was proved that it was feasible for the combined biofilm reactor to be applied in the distributed wastewater treatment for water reuse.
引文
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