CN103539260B - Method for enhancing anammox granular sludge in UASB - Google Patents
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- 239000010802 sludge Substances 0.000 title claims abstract description 146
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims abstract description 14
- 230000002708 enhancing effect Effects 0.000 title 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002245 particle Substances 0.000 claims abstract description 40
- 238000010992 reflux Methods 0.000 claims abstract description 37
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 31
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 11
- 238000005728 strengthening Methods 0.000 claims abstract description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims abstract description 10
- 230000006641 stabilisation Effects 0.000 claims abstract description 8
- 238000011105 stabilization Methods 0.000 claims abstract description 8
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 230000007423 decrease Effects 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 claims description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical group N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 6
- 230000014759 maintenance of location Effects 0.000 claims description 2
- 239000000758 substrate Substances 0.000 claims description 2
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- 239000010865 sewage Substances 0.000 abstract description 2
- 238000004062 sedimentation Methods 0.000 description 5
- 230000003247 decreasing effect Effects 0.000 description 4
- 244000005700 microbiome Species 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000013486 operation strategy Methods 0.000 description 1
- -1 polyethylene Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
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Abstract
一种UASB内强化厌氧氨氧化颗粒污泥的方法属于城市生活污水脱氮处理与再生领域。本发明采用UASB反应器，通过提高进水流量和回流比，经过颗粒污泥形成阶段、颗粒污泥强化阶段、颗粒污泥稳定阶段，在70d内，实现了总氮去除负荷达到6.5kgN/m3/d，平均粒径为2.0mm，成功强化了厌氧氨氧化颗粒污泥，比王俊敏等（2011）利用UASB反应器培养的厌氧氨氧化颗粒污泥的平均粒径大1.27mm，总氮去除负荷高0.77kgN/m3/d。
A method for strengthening anaerobic ammonium oxidation granular sludge in UASB belongs to the field of denitrification treatment and regeneration of urban domestic sewage. The present invention adopts UASB reactor, by increasing the influent flow rate and reflux ratio, through the granular sludge formation stage, granular sludge strengthening stage, and granular sludge stabilization stage, within 70 days, the total nitrogen removal load reaches 6.5kgN/m 3 /d, with an average particle size of 2.0 mm, which successfully strengthened the anammox granular sludge, which was 1.27 mm larger than the average particle size of the anammox granular sludge cultivated by Wang Junmin et al. (2011) using UASB reactors. The total nitrogen removal load is 0.77kgN/m 3 /d higher.
Description
技术领域technical field
本发明属于城市生活污水脱氮处理与再生领域。The invention belongs to the field of denitrification treatment and regeneration of urban domestic sewage.
背景技术Background technique
厌氧氨氧化（Anaerobic Ammonium Oxidation，ANAMMOX）工艺是近几年发现的新型生物脱氮技术，是指在厌氧条件下，厌氧氨氧化菌直接以NH4 +为电子供体，以NO3 -或NO2 -为电子受体，将NH4 +，NO3 -或NO2 -转变成N2的生物学过程。因其具有可高负荷运行，节省曝气、耗能少，无需外加有机碳源、无二次污染，剩余污泥产量低，运行、基建费用低等优点，一经问世就受到了世界各国的广泛关注，具有很高的科学研究与实用价值。但厌氧氨氧化菌生长速率低，倍增时间长，加之传统的活性污泥法与生物膜法由于污泥沉降性能差，易造成污泥流失，导致反应器内微生物浓度降低，脱氮性能下降。研究表明，由于颗粒污泥沉降性能良好，不易被洗出，可使其内部的微生物有效持留在反应器内，增加微生物浓度，提高脱氮效率。Anaerobic Ammonium Oxidation (ANAMMOX) process is a new type of biological denitrification technology discovered in recent years. It means that under anaerobic conditions, anaerobic ammonium oxidation bacteria directly use NH 4 + as the electron donor and NO 3 - or NO 2 - is an electron acceptor, which is the biological process of converting NH 4 + , NO 3 - or NO 2 - into N 2 . Because of its advantages of high-load operation, saving aeration, less energy consumption, no need to add organic carbon sources, no secondary pollution, low residual sludge output, low operation and infrastructure costs, it has been widely accepted by countries all over the world once it came out. attention, has high scientific research and practical value. However, the growth rate of anammox bacteria is low and the doubling time is long. In addition, the traditional activated sludge method and biofilm method are prone to sludge loss due to poor sludge settling performance, resulting in a decrease in the concentration of microorganisms in the reactor and a decrease in denitrification performance. . Studies have shown that due to the good sedimentation performance of granular sludge, it is not easy to be washed out, which can effectively keep the microorganisms inside the reactor, increase the concentration of microorganisms, and improve the efficiency of nitrogen removal.
目前普遍认为,水力剪切力是影响颗粒污泥形成和颗粒污泥性质的关键因素之一。丛岩等（2013）以好氧硝化颗粒污泥与厌氧氨氧化生物膜做为接种污泥,在缺氧条件下利用EGSB反应器培养厌氧氨氧化颗粒污泥。通过调节HRT来培养颗粒污泥，反应器运行80d后,培养出成熟的厌氧氨氧化颗粒污泥,平均粒径0.556mm；89d时,总氮去除负荷达4.758kgN/m3/d。王俊敏等（2011）采用UASB，逐步降低HRT，经过70天，HRT由1.26h缩短至0.14h,获得的容积氮去除速率为5.73kgN/m3/d;在此工况下获得的厌氧氨氧化污泥颗粒呈红褐色,粒径分布主要集中在0.5～0.9mm,平均粒径为0.73mm。It is generally believed that hydraulic shear force is one of the key factors affecting the formation and properties of granular sludge. Cong Yan et al. (2013) used aerobic nitrification granular sludge and anammox biofilm as seed sludge, and used EGSB reactor to cultivate anammox granular sludge under anoxic conditions. The granular sludge was cultivated by adjusting the HRT. After the reactor operated for 80 days, a mature anammox granular sludge was cultivated, with an average particle size of 0.556mm; at 89 days, the total nitrogen removal load reached 4.758kgN/m 3 /d. Wang Junmin et al. (2011) used UASB to gradually reduce the HRT. After 70 days, the HRT was shortened from 1.26h to 0.14h, and the obtained volumetric nitrogen removal rate was 5.73kgN/m 3 /d; the anaerobic The ammonia oxidation sludge particles are reddish brown, the particle size distribution is mainly concentrated in 0.5-0.9mm, and the average particle size is 0.73mm.
虽然增大剪切力，即降低水力停留时间HRT，增大断面流速，增加进水流量，可以加快并强化颗粒污泥的形成，但当污泥去除负荷达到一定程度稳定后，继续增大进水流量，会导致去除率下降，出水水质恶化、不达标。利用UASB出水再回流的方法，不仅起到对原水稀释的作用，最主要的是在不增加进水流量的前提下，增大断面流速，从而提高水流剪切力，强化颗粒污泥，使已形成的颗粒污泥具有更好的沉降性能。Although increasing the shear force, that is, reducing the hydraulic retention time HRT, increasing the cross-sectional velocity, and increasing the influent flow rate can accelerate and strengthen the formation of granular sludge, when the sludge removal load reaches a certain level of stability, continue to increase If the water flow rate is too high, the removal rate will decrease, and the effluent quality will deteriorate and fail to meet the standard. The method of using UASB outlet water and reflowing not only plays the role of diluting the raw water, but also increases the cross-sectional flow velocity without increasing the influent flow rate, thereby increasing the shear force of the water flow and strengthening the granular sludge. The formed granular sludge has better settling properties.
发明内容Contents of the invention
本发明目的在于在保证出水水质的前提下，提供一种强化颗粒污泥的方法。The purpose of the present invention is to provide a method for strengthening granular sludge on the premise of ensuring the quality of effluent water.
本发明是在28～32℃条件下，以人工配水为基础用水，采用上部装有填料，下部为活性污泥区的UASB为实验装置，进水基质为氨氮和亚硝酸盐氮，通过调整进水流量和出水回流比的运行策略来强化颗粒污泥的形成。总氮去除负荷为反应器单位体积每天所能去除的总氮质量；回流比为出水回流流量与进水流量的比值；污泥浓度为取反应器内污泥混合液，称干污泥重，干污泥重与污泥混合液体积的比值；SV2即2分钟污泥沉降比，取自反应器污泥置于量筒内，2分钟后污泥所占体积与取出污泥总体积的比值，即为2分钟污泥沉降比；SV10即10分钟污泥沉降比，取自反应器污泥置于量筒内，10分钟后污泥所占体积与取出污泥总体积的比值，即为10分钟污泥沉降比；具体步骤如下：The present invention is based on artificial water distribution under the condition of 28-32°C, adopts UASB with filler in the upper part and activated sludge area in the lower part as the experimental device, and the influent matrix is ammonia nitrogen and nitrite nitrogen. The operation strategy of water flow rate and effluent return ratio is used to enhance the formation of granular sludge. The total nitrogen removal load is the total nitrogen mass that can be removed per unit volume of the reactor per day; the reflux ratio is the ratio of the effluent reflux flow rate to the influent flow rate; the sludge concentration is the sludge mixture in the reactor, which is called the dry sludge weight, The ratio of the dry sludge weight to the volume of the sludge mixture; SV2 is the sludge sedimentation ratio in 2 minutes, taken from the reactor sludge and placed in the measuring cylinder, the ratio of the volume occupied by the sludge to the total volume of the sludge taken out after 2 minutes, It is the sludge sedimentation ratio in 2 minutes; SV10 is the sludge sedimentation ratio in 10 minutes, which is taken from the reactor sludge and placed in the measuring cylinder. The ratio of the volume occupied by the sludge to the total volume of the sludge taken out after 10 minutes is 10 minutes Sludge sedimentation ratio; specific steps are as follows:
一种UASB内强化厌氧氨氧化颗粒污泥的方法，其特征是：在28℃～32℃条件下，试验装置包括进水装置、主体反应器UASB、回流装置；UASB由底部布水区、中间反应区、顶部三相分离器组成；反应区径深比为1:10～1:15，分为下部活性污泥区和上部填料区，下部活性污泥区和上部填料区体积比为1:1～2:1；A method for strengthening anaerobic ammonium oxidation granular sludge in a UASB, characterized in that: under the condition of 28°C to 32°C, the test device includes a water inlet device, a main reactor UASB, and a reflux device; the UASB consists of a bottom water distribution area, It consists of a middle reaction zone and a top three-phase separator; the diameter-to-depth ratio of the reaction zone is 1:10 to 1:15, and it is divided into a lower activated sludge zone and an upper packing zone, and the volume ratio of the lower activated sludge zone and the upper packing zone is 1 :1～2:1;
1)颗粒污泥形成阶段，接种厌氧氨氧化絮状污泥，连续流运行，进水基质为氨氮和亚硝酸盐氮，通过调整进水流量，控制反应器的水力停留时间HRT在1.0～2.0h，控制反应器的断面流速在0.005cm/s～0.020cm/s；若反应器总氮去除率连续3d以上超过75%，则通过增加进水流量来提高断面流速，每次提高不超过35%，直到反应器的断面流速提高到0.0200～0.0300cm/s，当连续3d以上总氮去除负荷超过4.0kgN/m3/d时，将活性污泥区污泥取出，测定污泥浓度、SV和平均粒径，然后将污泥接回反应器；若SV2减去SV10的差值与SV2的比值不超过10%，污泥平均粒径超过1mm，认为颗粒污泥形成；1) In the granular sludge formation stage, anaerobic ammonium oxidation flocculent sludge is inoculated and operated in continuous flow. The influent substrate is ammonia nitrogen and nitrite nitrogen. By adjusting the influent flow rate, the hydraulic retention time of the reactor is controlled at 1.0~ 2.0h, control the cross-sectional flow velocity of the reactor at 0.005cm/s～0.020cm/s; if the total nitrogen removal rate of the reactor exceeds 75% for more than 3 days in a row, increase the cross-sectional flow velocity by increasing the influent flow rate, and each time the increase does not exceed 35%, until the cross-sectional flow rate of the reactor increases to 0.0200-0.0300cm/s, when the total nitrogen removal load exceeds 4.0kgN/m 3 /d for more than 3 consecutive days, the sludge in the activated sludge area is taken out, and the sludge concentration, SV and average particle size, and then return the sludge to the reactor; if the ratio of the difference between SV2 minus SV10 to SV2 does not exceed 10%, and the average particle size of the sludge exceeds 1mm, it is considered that granular sludge is formed;
2)颗粒污泥强化阶段，继续提高断面流速，增设回流装置，保持出水回流比R=1.15～1.30，控制HRT在0.33～0.48h，控制反应器的断面流速在0.2000cm/s～0.2900cm/s；若反应器总氮去除率连续3d以上超过75%，则提高断面流速，每次提高不超过20%，直到反应器的断面流速提高到0.2900cm/s，连续3d以上总氮去除负荷稳定在6.2kgN/m3/d～6.8kgN/m3/d时，且不再随进水流量的增加而增加为止；每提高一次断面流速，运行7d后，测定污泥浓度、SV10和平均粒径；若污泥浓度、平均粒径较上一次提高断面流速时的污泥浓度、平均粒径有所增长，且SV10减小，但反应器总氮去除负荷不再随进水流量的增加而增加，则认为颗粒污泥强化阶段成功；2) In the granular sludge strengthening stage, continue to increase the cross-sectional flow velocity, add a reflux device, keep the effluent-reflux ratio R=1.15-1.30, control the HRT at 0.33-0.48h, and control the cross-sectional flow velocity of the reactor at 0.2000cm/s-0.2900cm/s s; if the total nitrogen removal rate of the reactor exceeds 75% for more than 3 days in a row, increase the cross-sectional flow rate by no more than 20% each time until the cross-sectional flow rate of the reactor is increased to 0.2900cm/s, and the total nitrogen removal load is stable for more than 3 days in a row At 6.2kgN/m 3 /d～6.8kgN/m 3 /d, and no longer increase with the increase of influent flow rate; each time the cross-sectional flow rate is increased, after 7 days of operation, the sludge concentration, SV10 and average granularity diameter; if the sludge concentration and average particle size increase compared with the previous time when the cross-sectional flow rate was increased, and the SV10 decreases, the total nitrogen removal load of the reactor will no longer increase with the increase of the influent flow rate. increase, it is considered that the granular sludge intensification stage is successful;
3)颗粒污泥稳定阶段，固定进水流量不变，设定起始出水回流比R=1.45～1.55，每7d将污泥取出，测定污泥浓度、SV10和平均粒径，然后将污泥接回反应器；若污泥浓度、平均粒径较上一次提高回流比时的污泥浓度、平均粒径有所增长，而SV10减小，则提高回流比，每次提高不超过20%；直到R=2.05～2.15，测得污泥浓度、SV10较上一次提高回流比时的污泥浓度、SV10相差不超过1%～3%，且平均粒径较上一次提高回流比时的平均粒径相差不超过1%，认为颗粒污泥稳定阶段完成。3) In the granular sludge stabilization stage, the influent flow rate is fixed, the initial effluent reflux ratio is set to R=1.45~1.55, the sludge is taken out every 7 days, the sludge concentration, SV10 and average particle size are measured, and then the sludge Connect back to the reactor; if the sludge concentration and average particle size increase compared with the previous time when the reflux ratio was increased, and the SV10 decreases, then increase the reflux ratio by no more than 20% each time; Until R=2.05～2.15, the difference between the measured sludge concentration and SV10 is no more than 1% to 3% compared with the sludge concentration and SV10 when the reflux ratio was increased last time, and the average particle size is compared with the average particle size when the reflux ratio was increased last time. If the diameter difference does not exceed 1%, it is considered that the granular sludge stabilization stage is completed.
与现有强化厌氧氨氧化颗粒污泥的方法相比，本发明具有以下有益效果：Compared with the existing method for strengthening the anammox granular sludge, the present invention has the following beneficial effects:
1、厌氧氨氧化颗粒污泥经强化后，粒径更大，污泥沉降性能更好，抗水力冲击能力更强，污泥流失现象明显减弱，反应器内污泥浓度增加，脱氮性能增强。1. After strengthening the anaerobic ammonium oxidation granular sludge, the particle size is larger, the sludge settlement performance is better, the hydraulic shock resistance is stronger, the sludge loss phenomenon is obviously weakened, the sludge concentration in the reactor is increased, and the denitrification performance is improved. enhanced.
2、提高剪切力，不是单纯依靠提高进水流量，还利用了出水回流。在反应器总氮去除负荷增加的同时，颗粒污泥性能也得到了更快的加强；当总氮去除负荷稳定时，增大回流比，来提高水力剪切力，在保证出水水质的前提下，强化颗粒污泥并达到稳定状态。2. To increase the shear force, not only rely on increasing the inflow flow rate, but also utilize the backflow of the effluent water. When the total nitrogen removal load of the reactor increases, the performance of the granular sludge is also strengthened faster; when the total nitrogen removal load is stable, the reflux ratio is increased to increase the hydraulic shear force, under the premise of ensuring the quality of the effluent , strengthen the granular sludge and reach a steady state.
附图说明Description of drawings
图1是本发明采用的UASB试验装置示意图，UASB反应器上部装有聚乙烯辫带式填料，为生物膜反应区，下部为活性污泥区。Fig. 1 is the schematic diagram of the UASB test device that the present invention adopts, and the UASB reactor top is equipped with polyethylene braid type packing, is the biofilm reaction zone, and the bottom is the activated sludge zone.
图2是采用本发明方法的反应器在整个实验过程中总氮去除率TNR、总氮去除负荷ARR与出水回流比R随时间变化图，试验中出水回流比R不断增大，总氮去除率TNR、总氮去除负荷ARR先不断增大，后到达稳定状态；到颗粒污泥强化阶段成功后，总氮去除负荷平均达到6.5kgN/m3/d，；到颗粒污泥稳定阶段成功后，总氮去除负荷保持在6.5kgN/m3/d。Fig. 2 is the graph of total nitrogen removal rate TNR, total nitrogen removal load ARR and effluent reflux ratio R changing with time in the whole experimental process of the reactor adopting the method of the present invention. TNR and total nitrogen removal load ARR first increase continuously and then reach a steady state; after the granular sludge intensification stage is successful, the total nitrogen removal load reaches an average of 6.5kgN/m 3 /d; after the granular sludge stabilization stage is successful, The total nitrogen removal load was maintained at 6.5kgN/m 3 /d.
图3是采用本发明方法形成的颗粒污泥在培养皿，显示污泥颗粒化状态较好，且污泥平均粒径为2.0mm。Fig. 3 is the granular sludge formed by the method of the present invention in a petri dish, showing that the sludge granulation state is better, and the average particle size of the sludge is 2.0 mm.
具体实施方式Detailed ways
实施例一：Embodiment one:
试验装置主要分为进水装置、主体反应器UASB、回流装置。UASB由底部布水区、中间反应区、顶部三相分离器组成；反应区径深比为1:10～1:15，分为下部活性污泥区和上部填料区，体积比为1:1～2:1。The test device is mainly divided into water inlet device, main reactor UASB, and reflux device. UASB consists of a bottom water distribution area, a middle reaction area, and a top three-phase separator; the diameter-depth ratio of the reaction area is 1:10 to 1:15, and it is divided into a lower activated sludge area and an upper packing area, with a volume ratio of 1:1 ~2:1.
厌氧氨氧化颗粒污泥形成阶段，采用连续流运行，进水氨氮和亚硝酸盐氮浓度分别为100～130mg/L和110～140mg/L，起始HRT为1.90h，进水流量为70mL/min，反应器的断面流速为0.0148cm/s，采用连续流运行，连续运行3d后，总氮去除率超过75%，降低HRT为1.67h，进水流量为80mL/min，断面流速为0.0169cm/s，继续运行，6d后，总氮去除率连续3d超过75%，降低HRT为1.21h，进水流量为110mL/min,断面流速为0.0234cm/s，运行10d后，总氮去除负荷连续3天超过4.0kgN/m3/d，平均值为4.34kgN/m3/d，将活性污泥区污泥取出，测定污泥浓度、SV和平均粒径，得到SV2减去SV10的差值与SV2的比值不超过10%，且污泥平均粒径超过1mm，故颗粒污泥形成阶段成功。Anaerobic ammonia oxidation granular sludge formation stage, using continuous flow operation, the concentration of ammonia nitrogen and nitrite nitrogen in the influent is 100-130mg/L and 110-140mg/L respectively, the initial HRT is 1.90h, and the influent flow rate is 70mL /min, the cross-sectional flow velocity of the reactor is 0.0148cm/s, and continuous flow operation is adopted. After 3 days of continuous operation, the total nitrogen removal rate exceeds 75%, the HRT is reduced to 1.67h, the influent flow rate is 80mL/min, and the cross-sectional flow velocity is 0.0169 cm/s, continue to operate, after 6 days, the total nitrogen removal rate exceeds 75% for 3 consecutive days, reduce the HRT to 1.21h, the influent flow rate is 110mL/min, the cross-sectional flow rate is 0.0234cm/s, after 10 days of operation, the total nitrogen removal load If it exceeds 4.0kgN/m 3 /d for 3 consecutive days, and the average value is 4.34kgN/m 3 /d, take out the sludge from the activated sludge area, measure the sludge concentration, SV and average particle size, and get the difference of SV2 minus SV10 The ratio of the value to SV2 does not exceed 10%, and the average particle size of the sludge exceeds 1mm, so the granular sludge formation stage is successful.
厌氧氨氧化颗粒污泥强化阶段，采用连续流运行，进水氨氮和亚硝酸盐氮浓度分别为45～55mg/L和70～80mg/L，保持回流比R=1.28。起始HRT为0.48h，进水流量为420mL/min，出水回流流量为540mL/min，反应器的断面流速为0.2000cm/s。连续运行3d后，总氮去除负荷连续三天超过5.0kgN/m3/d，平均值为5.33kgN/m3/d，总氮去除率连续3d超过75%，运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、平均粒径较上一次提高断面流速时的污泥浓度、平均粒径有所增长，且SV10减小。降低HRT为0.40，进水流量为504mL/min，出水回流流量为645mL/min，反应器的断面流速为0.2442cm/s。连续运行3d后，总氮去除负荷连续3天超过6.0kgN/m3/d，平均值为6.5kgN/m3/d，总氮去除率连续3d超过75%，运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、平均粒径较上一次提高断面流速时的污泥浓度、平均粒径有所增长，且SV10减小。继续降低HRT为0.33，进水流量为605mL/min，回流流量为774mL/min，反应器的断面流速为0.2900cm/s。连续运行3d后，总氮去除负荷稳定在6.5kgN/m3/d左右。运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、平均粒径较上一次提高断面流速时的污泥浓度、平均粒径有所增长，且SV10减小。颗粒污泥平均粒径接近1.4mm。颗粒污泥性能加强，而反应器总氮去除负荷不再升高，说明颗粒污泥强化阶段完成。Anaerobic ammonium oxidation granular sludge enhancement stage adopts continuous flow operation, the concentration of ammonia nitrogen and nitrite nitrogen in the influent is 45-55mg/L and 70-80mg/L respectively, and the reflux ratio R=1.28 is maintained. The initial HRT is 0.48h, the influent flow rate is 420mL/min, the effluent reflux flow rate is 540mL/min, and the cross-sectional flow velocity of the reactor is 0.2000cm/s. After 3 days of continuous operation, the total nitrogen removal load exceeded 5.0kgN/m 3 /d for three consecutive days, with an average of 5.33kgN/m 3 /d, and the total nitrogen removal rate exceeded 75% for 3 consecutive days. After 7 days of operation, the activated sludge The sludge was taken out from the area, and the sludge concentration, SV10 and average particle size were measured. The sludge concentration and average particle size increased compared with the previous time when the cross-sectional flow velocity was increased, and the SV10 decreased. Reduce the HRT to 0.40, the influent flow rate is 504mL/min, the effluent return flow rate is 645mL/min, and the cross-sectional flow velocity of the reactor is 0.2442cm/s. After 3 days of continuous operation, the total nitrogen removal load exceeded 6.0kgN/m 3 /d for 3 consecutive days, with an average of 6.5kgN/m 3 /d, and the total nitrogen removal rate exceeded 75% for 3 consecutive days. After 7 days of operation, the activated sludge The sludge was taken out from the area, and the sludge concentration, SV10 and average particle size were measured. The sludge concentration and average particle size increased compared with the previous time when the cross-sectional flow velocity was increased, and the SV10 decreased. Continue to reduce the HRT to 0.33, the influent flow rate is 605mL/min, the reflux flow rate is 774mL/min, and the cross-sectional flow velocity of the reactor is 0.2900cm/s. After 3 days of continuous operation, the total nitrogen removal load stabilized at about 6.5kgN/m 3 /d. After 7 days of operation, the sludge in the activated sludge area was taken out, and the sludge concentration, SV10 and average particle size were measured, and the sludge concentration and average particle size were increased compared with the sludge concentration and average particle size when the section flow velocity was increased last time. , and SV10 decreases. The average particle size of granular sludge is close to 1.4mm. The performance of granular sludge is enhanced, but the total nitrogen removal load of the reactor is no longer increased, indicating that the granular sludge intensification stage is completed.
厌氧氨氧化颗粒污泥稳定阶段，采用连续流运行，进水氨氮和亚硝酸盐氮浓度分别为45～55mg/L和70～80mg/L，固定进水流量为605mL/min。起始回流比为1.5，回流流量为907.5mL/min，断面流速为0.3211cm/s，连续运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、颗粒污泥平均粒径较上一次提高回流比时污泥浓度、颗粒污泥平均粒径有所增长，且SV10减小；提高回流比R为1.8，回流流量为1089mL/min，断面流速为0.3596cm/s，连续运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、颗粒污泥平均粒径较上一次提高回流比时污泥浓度、颗粒污泥平均粒径有所增长，且SV10减小；继续提高回流比R为2.16，回流流量为1306.8mL/min，断面流速为0.4059cm/s，连续运行7d后，将活性污泥区污泥取出，测定污泥浓度、SV10和平均粒径，得到污泥浓度、颗粒污泥平均粒径较上一次提高回流比时的污泥浓度、颗粒污泥平均粒径有所增长，且SV10减小，颗粒污泥平均粒径为2.0mm；继续提高回流比R为2.59，回流流量为1566.9mL/min，断面流速为0.4611cm/s，连续运行7d后，将活性污泥区污泥取出，测得污泥浓度、SV10较上一次提高回流比时的污泥浓度、SV10相差不超过1%～3%，且平均粒径较上一次提高回流比时的平均粒径相差不超过1%，认为颗粒污泥稳定阶段完成。In the stabilization stage of anaerobic ammonium oxidation granular sludge, continuous flow operation is adopted, the concentrations of ammonia nitrogen and nitrite nitrogen in the influent are 45-55mg/L and 70-80mg/L, respectively, and the fixed influent flow rate is 605mL/min. The initial reflux ratio is 1.5, the reflux flow rate is 907.5mL/min, and the cross-sectional flow velocity is 0.3211cm/s. After 7 days of continuous operation, the sludge in the activated sludge area is taken out, and the sludge concentration, SV10 and average particle size are measured to obtain the sludge Compared with the last time when the reflux ratio was increased, the sludge concentration and the average particle size of the granular sludge increased, and the SV10 decreased; the reflux ratio R was increased to 1.8, and the reflux flow rate was 1089mL/min. The flow rate is 0.3596cm/s. After 7 days of continuous operation, the sludge in the activated sludge area is taken out, and the sludge concentration, SV10 and average particle size are measured to obtain the sludge concentration and the average particle size of the granular sludge. The sludge concentration and the average particle size of granular sludge increased, and the SV10 decreased; continue to increase the reflux ratio R to 2.16, the reflux flow rate to 1306.8mL/min, and the cross-sectional flow rate to 0.4059cm/s. After 7 days of continuous operation, the activity The sludge in the sludge area was taken out, and the sludge concentration, SV10 and average particle size were measured, and the sludge concentration and the average particle size of the granular sludge were increased compared with the sludge concentration and the average particle size of the granular sludge when the reflux ratio was increased last time. , and SV10 decreases, the average particle size of granular sludge is 2.0mm; continue to increase the reflux ratio R to 2.59, the reflux flow rate is 1566.9mL/min, the cross-sectional flow rate is 0.4611cm/s, after continuous operation for 7 days, the activated sludge area The sludge is taken out, and the difference between the measured sludge concentration and SV10 is no more than 1% to 3% compared with the sludge concentration and SV10 when the reflux ratio was increased last time, and the average particle size is not different from the average particle size when the reflux ratio was increased last time. More than 1%, it is considered that the granular sludge stabilization stage is completed.
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