WO2015070512A1 - 一种两系列厌氧缺氧更替运行的d-a2/o污水处理反应器 - Google Patents
一种两系列厌氧缺氧更替运行的d-a2/o污水处理反应器 Download PDFInfo
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- WO2015070512A1 WO2015070512A1 PCT/CN2014/000764 CN2014000764W WO2015070512A1 WO 2015070512 A1 WO2015070512 A1 WO 2015070512A1 CN 2014000764 W CN2014000764 W CN 2014000764W WO 2015070512 A1 WO2015070512 A1 WO 2015070512A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/286—Anaerobic digestion processes including two or more steps
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2806—Anaerobic processes using solid supports for microorganisms
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
Definitions
- the invention patent relates to a sewage treatment reactor.
- ⁇ 2 /0 and SBR are common processes with high denitrification and dephosphorization.
- SBR has limited the development of this process due to its high automation and intermittent effluent issues.
- the traditional ⁇ 2 /0 process for nitrogen and phosphorus removal is not complicated.
- the anaerobic, anoxic and aerobic three-stage process formed by the improvement of traditional activated sludge can not only effectively remove organic matter, but also simultaneously remove nitrogen. phosphorus.
- the existing ⁇ 2 /0 also has the problem that the efficiency of nitrogen and phosphorus removal is difficult to be further significantly improved. There are two reasons for this: (1) the existence of carbon source competition for denitrification and phosphorus removal; (2) the presence of microbial phosphorus release and The problem of low phosphorus absorption capacity.
- the specific analysis is as follows:
- the existing ⁇ 2 /0 process nitrogen and phosphorus removal is closely related to the reflux ratio. Too low reflux ratio is difficult to have the ideal nitrogen and phosphorus removal efficiency, but too high reflux ratio is also due to the high concentration of DO in the oxygen-deficient (defective) oxygen section, which is difficult to have high denitrification effect and phosphorus release capacity. Therefore, the existing A 2 /0 process controls the reflux ratio of the sludge and mud-water mixture to a lower value, and the ability to release rock and absorb phosphorus is small.
- the DA 2 /0 reactor has the following characteristics:
- the present invention integrates a hydrolysis acidification tank before A 2 /0.
- Most of the poorly soluble organic matter and macromolecular organic matter in the wastewater during hydrolysis and acidification can be degraded into soluble organic matter and small molecular organic matter under hydrolysis and acidification, which can effectively avoid the problem of insufficient A 2 /0 carbon source. This is another key factor for efficient nitrogen and phosphorus removal in the DA 2 /0 reactor.
- the DA 2 /0 reactor integrates the principles of the A 2 /0 process and the SBR process. Overall, the DA 2 /0 reactor has a significant A 2 /0 sludge reflux system and nitrification reflux characteristics; from a local perspective, the DA 2 /0 anaerobic, anoxic tank replacement operation has a similar SBR Process influent period, reaction period, sedimentation period and drainage sludge discharge stage. This is a possible factor for efficient nitrogen and phosphorus removal in the DA 2 /0 reactor, which needs further investigation.
- test results of more than 12 months show that the DA 2 /0 reactor is stable and has a high sewage treatment effect, and its COD, nitrogen and phosphorus removal efficiency is much higher than the existing A 2 /0 and SBR processes. .
- the DA 2 /0 reactor of the invention has the technical advantages of high efficiency of nitrogen and phosphorus removal, stable effluent quality and minimal residual sludge yield, which cannot be replaced by other sewage treatment technologies in a short period of time, which will also make The promotion and application of this technology has long-term market guarantee.
- the DA 2 /0 reactor study has not been reported yet, and it is the first.
- the purpose of the present invention is to provide a two-stage anaerobic anoxic replacement operation of a DA 20 sewage treatment reactor, which is characterized by comprising a water tank (1), an acidification tank (2), an anaerobic tank (4), and anoxic acid.
- the domestic sewage in the water tank (1) passes through the acidification tank (2) in turn, which is tired.
- the oxygen pool (4), the anoxic tank (5), the aerobic tank (7) and the secondary settling tank (9) receive purified water from the water outlet (15), and the sludge is discharged from the sludge of the secondary settling tank (9). Mouth (14) is excluded.
- the acidification tank (2) has a suspended membrane packing (3), and the anaerobic tank (4) and the anoxic tank (5) each have a stirrer (6), and the aerobic tank (7) has an aeration Head (8).
- the aerobic tank (7) has a vacuum pump (12).
- the acidification tank (2), the anaerobic tank (4), the anoxic tank (5) and the aerobic tank (7) each have a sludge discharge port (10).
- the acidification tank (2), the anaerobic tank (4), and the anoxic tank (5) each have two series.
- the process principle is as follows: the influent water is passed through a constant flow pump to a hydrolysis acidification tank provided with an elastic three-dimensional filler, and the hydrolysis acidified bacteria degrades the macromolecular organic matter and the poorly soluble organic matter in the sewage into small molecular organic substances and easily degradable organic substances; and then flows to the phase A phase.
- the nitrification liquid and the sludge refluxed in the aerobic tank and the sedimentation tank are stirred in the mixer to make the activated sludge microorganisms sufficiently contact with the pollutant matrix in the sewage to cause organic matter degradation, denitrification and release.
- the acidification tank (2), the anaerobic tank (4), the anoxic tank (5) and both have two series, and when one of the phases is in operation, the other phase is in a resting state. The next time you change the operating state, the opposite is true. Throughout the test process, the two series of successively replaced the operation to achieve the purification of sewage.
- the DA 20 described in this patent represents two series of anaerobic anoxic replacement operating A70.
- the structure of DA 2 /0 is characterized by the design of two independent series of sludge return systems and nitrifying liquid reflux systems.
- the two series of alternate operation modes have largely solved the belt from the nitrifying liquid.
- the DO in the anoxic tank affects the effect of denitrification and denitrification, thereby ensuring efficient denitrification in the system.
- the reflux ratio R of the larger flow rate is a key factor. The result will inevitably ensure that one of the phases of the system is normally influent and maintains phosphorus and nitrogen removal. At the same time, the phase in the resting phase undergoes excessive phosphorus release and sufficient denitrification due to excessive hypoxia.
- the present invention integrates a hydrolysis acidification tank before A 2 /0.
- Most of the poorly soluble organic matter and macromolecular organic matter in the wastewater during hydrolysis and acidification can be degraded into soluble organic matter and small molecular organic matter under hydrolysis and acidification, which can effectively avoid the problem of insufficient A 2 /0 carbon source. This is a key factor for efficient nitrogen and phosphorus removal in the DA 2 /0 reactor.
- Figure 1 is a schematic view of a reaction apparatus system of the present invention
- Figure 2 is a process flow diagram of the present invention.
- a two-stage anaerobic anoxic replacement operation of a DA 20 sewage treatment reactor characterized by comprising a water tank (1), an acidification tank (2), an anaerobic tank (4), an anoxic tank (5), an aerobic
- the pool (7) and the secondary settling tank (9) the domestic sewage in the water tank (1) is sequentially passed through the acidification tank (2), the anaerobic tank (4), the anoxic tank (5), the aerobic tank ( 7) and the secondary settling tank (9) obtain purified water from the water outlet (15), and the sludge is excluded from the sludge discharge port (14) of the secondary settling tank (9).
- the acidification tank (2) has a suspended membrane packing (3), an anaerobic tank (4) and an anoxic tank (5) There is a stirrer (6) having an aeration head (8) therein.
- the aerobic tank (7) has a vacuum pump (12).
- the acidification tank (2), the anaerobic tank (4), the anoxic tank (5) and the aerobic tank (7) have a drain port (10) on the same side.
- the acidification tank (2), the anaerobic tank (4), the anoxic tank (5) and the secondary settling tank (A in Fig. 2 is a phase, and B is a phase).
- the operation of sewage in the reactor is as follows: after the hydrolysis and acidification of the sewage in the hydrolysis acidification tank, the sewage will enter the anaerobic cell compartment with the return sludge from the secondary sedimentation tank, and the outflow sewage will enter the hypoxia with the mixture from the aerobic tank. After the biochemical reaction is fully mixed by anaerobic/anoxic pool agitation, the muddy water mixture flows to the aerobic tank; a part of the mixture in the aerobic tank is returned to the anoxic tank, and the other part is discharged from the overflow to the second sink.
- the mud water is separated in the pool, the supernatant is discharged from the effluent, and the sludge is partially returned to the anaerobic tank, and the excess sludge is discharged outside the system.
- the unified phase is operating in the above operating state, the other phase is in a rest state.
- the two series of replacement operations realized the treatment of pollutants and the purification of sewage.
- the wastewater treatment capacity of the DA 20 reactor is increased by about 10%
- the COD removal rate is increased by about 5%
- the TN removal rate is increased by about 10%
- the ammonia nitrogen removal rate is improved.
- the TP removal rate is increased by about 15%. From the experimental analysis results, the dephosphorization and dephosphorization and COD removal efficiency of the DA 2 0 reactor is very significant.
- an ecological tank culture ornamental goldfish was set up at the outlet end of the reactor, and the survival rate of the goldfish was observed to further verify whether the water quality was stable. The 2-month observations show that the survival rate of ornamental goldfish is over 90%.
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- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
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Abstract
本发明涉及一种两系列厌氧缺氧更替运行的D-A2/O污水处理反应器,其特征在于包括水箱(1),酸化池(2),厌氧池(4),缺氧池(5),好氧池(7)和二沉池(9)。本发明的D-A2/O反应器具有高效的脱氮除磷效果、出水水质稳定、极小的剩余污泥产率等技术优势。
Description
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一种两系列厌氧缺氧更替运行的 D-A2/0污水处理反应器 技术领域
本发明专利涉及一种污水处理反应器 。
背景技术
Α2/0和 SBR是具有较高脱氮脱磷功效的常见工艺。相比较而言, SBR因其 较高的自动化控制和间歇性出水等问题而使得该工艺的发展受到限制。 传统 Α2/0工艺脱氮除磷原理并不复杂, 经传统活性污泥改进而形成的厌氧、 缺氧、 好氧三段法的此工艺不仅能有效去除有机物,亦可同步脱氮除磷。但是现有 Α2/0 亦存在脱氮除磷效率难以进一步显著提升的问题, 究其原因有二: (1 )存在脱氮 与除磷的碳源竞争问题; (2 )存在微生物释磷和吸磷能力较低的问题。具体分析 如下:
以往的研究成果表明, Α2/0工艺中缺氧段的反硝化作用是除氮的主要途径, 其关键在于缺氧段中是否有充足的碳源; 同时,聚磷菌亦需摄取厌氧段中易降解 有机物作释磷反应,方可在好氧段中过量吸磷而达到除磷之目的。当进水中的碳 源缺乏, 即进水为低 C/N 比低时, Α2/0工艺脱氮除磷碳源竞争问题尤为明显。 从工艺流程来看,聚磷菌在厌氧段的释磷作用几乎消耗掉进水中的绝大部分易降 解的有机物,故缺氧段仅剩的少量慢速或难降解的有机物难以满足反硝化脱氮作 用而导致脱氮效果较差。 从同一厌氧(缺氧)段来看, 反硝化菌优先于聚磷菌利 用有机碳源进行脱氮作用,从而导致聚磷菌释磷效果降低,其结果必然导致好氧 段的吸磷效果不显著。 因此, 现有 Α2/0工艺的碳源竞争问题成为该工艺脱氮除 磔的限制性因素。
现有 Α2/0工艺脱氮除磷与回流比密切相关。 过低的回流比难有理想的脱氮 除磷功效, 但过高的回流比亦因造成厌(缺)氧段 DO浓度过高而难有较高的脱 氮效果和释磷能力。 因此, 现有 A2/0工艺均控制污泥、 泥水混合液回流比于较 低值, 其释磯和吸磷能力较小。
若能釆取措施解决 A2/0工艺运行过程中的碳源竞争, 并显著提升其释磷和 吸磷能力, 则可大大提高该工艺的脱氮除磷功效。基于此种观点, 本研究设计了
D-A2/0反应器, 其特点如下:
( 1 )从反应器的结构特点来看, D-A O的结构特点在于设计了独立两系列 污泥回流***和硝化液回流***,两系列更替运行的方式在很大程度上解决了由 硝化液中带入缺氧池中的 DO影响反硝化脱氮的效果,从而保证***内高效脱氮 效能较大流量的回流比 R是关键因素。 其结果必然确保***其中一相正常进水 并保持释磷和脱氮的同时,处于静歇的一相因过度缺氧而进行超量的释磷作用和 充分的脱氮作用。厌氧段聚磷菌超量的释磷作用必然致使聚磷菌在好氧段的超量 吸磷, 最终以排放剩余污泥的形式而实现***更为显著的除磷功效。 此应为 D-A2/0反应器高效脱氮除磷的最关键因素。
(2 )从反应器的流程特点来看, 本发明于 A2/0前集成了水解酸化池。水解 酸化过程中污水中的大多数难溶性有机物和大分子有机物可在水解酸化作用下 降解为可溶性有机物和小分子有机物, 可有效避免后续 A2/0碳源不足的问题。 此为 D-A2/0反应器高效脱氮除磷的又一关键因素。
( 3)从反应器的运行特点来看, D-A2/0反应器集成了 A2/0工艺与 SBR工 艺的原理。从整体而言, D-A2/0反应器具有显著的 A2/0污泥回流***和硝化液 回流特点; 从局部而言, D-A2/0厌氧、 缺氧池更替运行方式具有类似于 SBR工 艺进水期、 反应期、 沉淀期和排水排泥期等阶段。 此为 D-A2/0反应器高效脱氮 除磷的可能性因素, 尚须进一步探究。
由 12个多月的试验运行结果表明, D-A2/0反应器运行稳定并具有较高的污 水处理效果, 其 COD、 氮和磷的去除功效远高于现有的 A2/0和 SBR工艺。
本发明的 D-A2/0反应器具有高效的脱氮除磷效果、 出水水质稳定、 极小的 剩余污泥产率等技术优势,这是其他污水处理技术短时期无法取代的,这也将使 得该技术的推广和应用具有长期的市场保障。 D-A2/0反应器研究目前尚未见报 道, 实为首创。
发明内容
本发明专利的目的在于提供一种两系列厌氧缺氧更替运行的 D-A20污水处理 反应器, 其特征在于包括水箱 (1 ), 酸化池 (2), 厌氧池 (4), 缺氧池 (5),好 氧池 (7 ) 和二沉池 (9)。 所述水箱(1 ) 中的生活污水依次经过酸化池 (2),厌
氧池(4), 缺氧池(5), 好氧池(7)和二沉池(9)从出水口 (15) 中得到净水, 污泥由二沉池 (9) 的污泥排放口 (14) 排除。
所述酸化池 (2) 中具有悬浮挂膜填料 (3), 厌氧池 (4) 和缺氧池 (5) 均 具有搅拌器 (6), 所述好氧池 (7) 中具有曝气头 (8)。
所述好氧池 (7) 和缺氧池 (5) 之间具有混合液回流泵 (11), 将泥水混合 液回流至缺氧池 (5); 二沉池 (9) 和厌氧池 (4) 之间具有污泥回流泵 (13), 将污泥回流至厌氧池 (4)。
所述好氧池 (7) 具有真空泵 (12)。
所述酸化池(2), 厌氧池(4), 缺氧池(5)和好氧池(7) 的均具有排泥口 (10)。
所述酸化池 (2), 厌氧池 (4), 缺氧池 (5)均具有两系列。
所述水解酸化池、 厌氧池、 缺氧池和好氧池各室的体积比 νΑ4¾ VR : Vttft 池: V好 = (1-2) : (1-2) : (1-2) : (2-4)。 其中水解酸化池具体尺寸分别为: 长 X宽 X高 =250 X 320 X 800 (单位匪); 厌氧池长 X宽 X高 =250 X 250 X 800 (单位 mm); 缺氧池: 长 X宽 X高 =250X320 X 800 (单位誦); 好氧池: 长 X宽 X高 =450 X 500X800 (单位讓); 所述二沉池 (9) 具有一柱体部 (9-1)和椎体部 (9-2), 其二沉池的柱体部直径 D=300mm, 高 h=600ram, 锥体部大端直径1)1=300皿小端直径 D2=150ram, 每格室内均投入已驯化好的活性污泥。
其工艺原理为:进水经恒流泵至设置弹性立体填料的水解酸化池,水解酸化 细菌将污水中的大分子有机物和难溶性有机物降解为小分子有机物和易降解有 机物; 继而流至 A相厌氧池和缺氧池中, 与好氧池、 沉淀池回流的硝化液、 污泥 在搅拌机连搅拌使活性污泥微生物与污水中的污染物基质充分接触而发生有机 物降解、脱氮和释磷反应; 缺氧池的泥水混合液流至好氧池进行吸磷反应。所述 酸化池 (2), 厌氧池 (4), 缺氧池 (5) 和均具有两系列, 当其中一相处于运行 状态时,另一相处于静歇状态。下一个更替运行状态时,则相反。整个试验过程, 两系列依次更替运行实现了污水的净化。
本专利中所述的 D-A20代表两系列厌氧缺氧更替运行式 A70。
有益效果:
①集成了水解酸化段以满足脱氮除磷的碳源,使设计的反应器在不需额外投
加碳源节省运行费用; ②设计了独立两系列污泥回流***和硝化液回流***,采 用独立两系列厌氧 /厌氧更替运行方式而提高脱氮除磷功效。 在推广应用时, 较 容易实现本研究成果的技术转化。 只需在现有 A2/0工艺的基础上, 增加一相水 解酸化池、 厌氧池和缺氧池, 即可实现 D-A2/0反应器的创建, 其脱氮除磷功效 的显著提高。
从反应器的结构特点来看, D-A2/0的结构特点在于设计了独立两系列污泥 回流***和硝化液回流***,两系列更替运行的方式在很大程度上解决了由硝化 液中带入缺氧池中的 DO影响反硝化脱氮的效果,从而保证***内高效脱氮效能 较大流量的回流比 R是关键因素。 其结果必然确保***其中一相正常进水并保 持释磷和脱氮的同时,处于静歇的一相因过度缺氧而进行超量的释磷作用和充分 的脱氮作用。 厌氧段聚磷菌超量的释磷作用必然致使聚磷菌在好氧段的超量吸 磷,最终以排放剩余污泥的形式而实现***更为显著的除磷功效。此应为 D-A2/0 反应器高效脱氮除磷的最关键因素。
从反应器的流程特点来看, 本发明于 A2/0前集成了水解酸化池。 水解酸化 过程中污水中的大多数难溶性有机物和大分子有机物可在水解酸化作用下降解 为可溶性有机物和小分子有机物, 可有效避免后续 A2/0碳源不足的问题。 此为 D-A2/0反应器高效脱氮除磷的一个关键因素。
附图说明
下面结合附图及实施方式对本发明作进一步详细的说明:
图 1为本发明的反应装置***示意图;
图 2为本发明的工艺流程图。
具体实施方式
下面结合具体实施例, 进一步阐述本发明。
一种两系列厌氧缺氧更替运行的 D-A20污水处理反应器, 其特征在于包括水 箱 (1 ), 酸化池 (2), 厌氧池 (4), 缺氧池(5), 好氧池 (7 ) 和二沉池 (9), 所述水箱(1 ) 中的生活污水通过泵依次经过酸化池 (2), 厌氧池 (4), 缺氧池 ( 5),好氧池(7 )和二沉池(9)从出水口(15)中得到净水,污泥由二沉池(9 ) 的污泥排放口 (14) 排除。
所述酸化池 (2 ) 中具有悬浮挂膜填料 (3), 厌氧池 (4) 和缺氧池 (5 ) 均
具有搅拌器 (6), 所述好氧池 (7) 中具有曝气头 (8)。
所述好氧池 (7) 和缺氧池 (5) 之间具有混合液回流泵 (11), 将回流液回 流至缺氧池 (5); 二沉池 (9) 和厌氧池 (4) 之间具有污泥回流泵 (13), 将污 泥回流至厌氧池 (4)。
所述好氧池 (7) 具有真空泵 (12) .
所述酸化池(2), 厌氧池(4), 缺氧池(5)和好氧池(7) 的同侧均具有排 泥口 (10)。
所述酸化池 (2), 厌氧池 (4), 缺氧池 (5) 和二沉池 (图 2中 A为一相, B 为一相)。
所述水解酸化池、 厌氧池、 缺氧池和好氧池各室的体积比 VR : 池: V好氧池 =1.3:1:1: 3.720其中水解酸化池具体尺寸分别为:长 X宽 X高 =250 X 320 Χ800(单位匪); 厌氧池长 X宽 X高 =250X250 X 800 (单位 mm); 缺氧池: 长 X宽 X高 =250X320 X 800 (单位匪;); 好氧池: 长 宽 高=450 500 800(单位腿); 所述二沉池(9)具有一柱体部(9-1)和椎体部(9-2), 其二沉池的柱体部直径 D=300ram, 高 h=600匪, 锥体部大端直径1)1=300隱小端直径 =150匪, 每格室内均 投入已驯化好的活性污泥。
污水在反应器中运行情况是:污水经水解酸化池格室水解酸化后会同来自二 沉池的回流污泥进入厌氧池格室,出流污水再会同来自好氧池的混合液进入缺氧 池格室; 经厌氧 /缺氧池搅拌充分混合生化反应后, 泥水混合液流至好氧池; 好 氧池一部分混合液回流至缺氧池,另一部分由溢流堰出流至二沉池中进行泥水分 离, 上清液由出水堰流出, 污泥部分回流至厌氧池, 剩余污泥排出***外。 当系 统一相以上述运行状态运行时, 另一相则处于静歇状态。整个试验过程, 两系列 更替运行实现了污染物的处理及污水的净化。
12个月小试试验结果详见表 1。 表 1 试验结果
^^目 COD TN 氨氮 TP DO 名 mg/L mg/L mg/L mg/L mg/L 进水 150-445 17.76-58.16 13.72-48.53 1.62-9.80 0.0 酸化池 134-380 16.81-37 12.06-36.57 1.615-3.092 0.0
出水 22.8-36 6.62-10.81 0.28-4.75 0.082-0.391 0.91-2.8 最低去除率 86.36% 76.28% 72.48% 86.53% - 最高去除率 94.87% 88.61% 99.54% 97.23% - 平均去除率 89.32% 80.66% 90.63% 90.84% - 由表 1可知, 本发明的 D-A2/0反应器出水水质稳定在一级 A标至地表水 环境质量 V类之间。 与 A20及改良 A20工艺相比, 相同边界条件下, D-A20反 应器污水处理量提高约 10%, COD去除率提高约 5%, TN去除率提高约 10%, 氨氮去除率提高约 15%, TP去除率提高约 15%。 由试验分析结果可知, D-A20 反应器的脱氮除磷及 COD去除功效十分显著。 试验过程中在反应器出水端设置 生态箱养殖观赏金鱼, 通过观测金鱼的成活率以进一步验证出水水质是否稳定。 2个月的观测结果表明, 观赏金鱼成活率高达 90%以上。
试验条件: 水温 =15-24 Ό ; 水力停留时间 HRT=6-10h ; 混合液回流比 R=200%-400% (好氧池污泥浓度 MLSS=2500-3500mg/L ); 污泥回流比 r= 110%- 150%(回流污泥浓度 MLSS=4000-6800mg/L); 两系列更替运行时间 T=0.5h-3h。
应理解,这些实施例仅用于说明本发明而不用于限制本发明的范围。并且对 于两系列, 三系列或者或多系列的厌氧缺氧更替运行的 D-A2/0污水处理反应器 均在本发明的保护范围之内。 此外应理解, 在阅读了本发明讲授的内容之后,本 领域技术人员可以对本发明作各种改动或修改,这些等价形式同样落于本申请所 附权利要求书所限定的范围。
Claims
1. 一种两系列厌氧缺氧更替运行的 D-A70污水处理反应器, 其特征在于包 括水箱(1), 酸化池(2), 厌氧池(4), 缺氧池(5), 好氧池(7)和二沉池(9), 所述水箱(1) 中的生活污水通过泵依次经过酸化池(2), 厌氧池 (4), 缺氧池 (5),好氧池(7)和二沉池(9)从出水口(15)中得到净水, 污泥由二沉池(9) 的污泥排放口 (14) 排除。
所述酸化池 (2) 中具有悬浮挂膜填料 (3), 厌氧池 (4) 和缺氧池 (5) 均 具有搅拌器 (6), 所述好氧池 (7) 中具有曝气头 (8)。
2.如权利要求 1所述的一种两系列厌氧缺氧更替运行的 D-A70污水处理反应 器, 其特征在于所述好氧池 (7) 和缺氧池 (5) 之间具有混合液回流泵 (11), 将泥水混合液回流至缺氧池(5); 二沉池(9)和厌氧池(4)之间具有污泥回流 泵 (13), 将活性污泥回流至厌氧池 (4)。
3.如权利要求 1所述的一种两系列厌氧缺氧更替运行的 D-A70污水处理反应 器, 其特征在于所述好氧池 (7) 具有真空泵 (12)。
4.如权利要求 1所述的一种两系列厌氧缺氧更替运行的 D-A70污水处理反应 器, 其特征在于所述的酸化池 (2), 厌氧池 (4), 缺氧池 (5)和好氧池 (7)均 具有排泥口 (10)。
5.如权利要求 4所述的一种两系列厌氧缺氧更替运行的 D-A70污水处理反应 器, 其特征在于所述酸化池 (2), 厌氧池 (4), 缺氧池 (5) 均具有两系列。
6.如权利要求 5所述的一种两系列厌氧缺氧更替运行的 D-A2/0污水处理反 应器, 其特征在于所述水解酸化池、 厌氧池、 缺氧池和好氧池各室的体积比 V 解酸化池: V厌織: V缺¾池: V好 = (1-2) : (1-2) : (1-2) : (2-4)。 其中水解酸化池具体 尺寸分别为: 长 X宽 X高 =250X320X800(单位 mm); 厌氧池长 X宽 X高 =250 X 250X800(单位 mm); 缺氧池: 长 X宽 X高 =250X320X800(单位 mm); 好氧池: 长 X宽 X高 =450X500X800(单位 mm); 所述二沉池 (9) 具有一柱体部 (9-1) 和椎体部(9-2), 其二沉池的柱体部直径 D=300mm, 高 h=600mm, 锥体部大端 直径 D^SOOmm小端直径 D2=150mm, 每格室内均投入已驯化好的活性污泥。
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Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110759592A (zh) * | 2019-11-05 | 2020-02-07 | 天津中冀源环保科技有限公司 | 一种无外加碳源的水解酸化+a2/o2的污水处理方法 |
CN111217447A (zh) * | 2019-11-29 | 2020-06-02 | 段林卓 | 一种高寒地区室外冲水厕所污水处理工艺及装置 |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
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CN103601296B (zh) * | 2013-11-15 | 2015-11-25 | 玉溪师范学院 | 一种两相厌氧缺氧交替运行的d-a2/o污水处理反应器 |
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Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1988008410A1 (en) * | 1987-04-21 | 1988-11-03 | Hampton Roads Sanitation District | High-rate biological waste water treatment process using activated sludge recycle |
KR20050097098A (ko) * | 2004-03-30 | 2005-10-07 | 주식회사 한화건설 | 유입흐름제어형 막분리 활성슬러지공법을 이용한하폐수처리공법 |
CN101195506A (zh) * | 2006-12-08 | 2008-06-11 | 同济大学 | 厌氧/缺氧并联式脱氮除磷工艺 |
KR100838846B1 (ko) * | 2007-02-23 | 2008-06-17 | 주식회사 포스코건설 | 하수처리의 반류수 처리방법 |
CN101259979A (zh) * | 2007-12-28 | 2008-09-10 | 凌亮 | 一种利用微生物处理高浓度含氮废水的方法及装置 |
US20110132837A1 (en) * | 2009-12-07 | 2011-06-09 | Ch2M Hill, Inc. | Method and System for Treating Wastewater |
CN103601296A (zh) * | 2013-11-15 | 2014-02-26 | 玉溪师范学院 | 一种两相厌氧缺氧交替运行的d-a2/o污水处理反应器 |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
HU221553B (hu) * | 2000-03-10 | 2002-11-28 | MÉLYÉPTERV Komplex Mérnöki Rt. | Tömbösített szennyvíztisztító berendezés |
CN1242941C (zh) * | 2003-11-04 | 2006-02-22 | 广州大学 | 序批式生物膜***反硝化除磷脱氮处理城市污水的方法 |
CN101857334B (zh) * | 2009-04-07 | 2013-07-17 | 上海达源环境科技工程有限公司 | 一种污水处理装置及其污水处理工艺 |
CN101880090A (zh) * | 2010-02-03 | 2010-11-10 | 王鹤立 | 一种多功能成套污水处理方法及装置 |
CN101993178B (zh) * | 2010-10-21 | 2012-04-18 | 神马实业股份有限公司 | 一种含己二胺的工业废水的处理方法 |
CN102557325B (zh) * | 2010-12-07 | 2013-06-05 | 光大环保科技发展(北京)有限公司 | 交替式生化池、污水处理方法及污水处理*** |
CN102249412B (zh) * | 2011-05-20 | 2013-02-13 | 中国矿业大学 | 一种多级缺氧厌氧循环尾段缺氧活性污泥处理工艺及*** |
CN102145969B (zh) * | 2011-05-20 | 2012-05-23 | 中国矿业大学 | 一种多级厌氧好氧并流尾段缺氧活性污泥工艺 |
CN102701457B (zh) * | 2012-07-13 | 2014-05-21 | 中国水电顾问集团中南勘测设计研究院 | 一种适合镇、乡集中型污水处理的装置和方法 |
CN103145247A (zh) * | 2013-04-02 | 2013-06-12 | 上海泓济环保工程有限公司 | 复合式hbf模块反应器及污水处理工艺 |
-
2013
- 2013-11-15 CN CN201310566833.XA patent/CN103601296B/zh not_active Expired - Fee Related
-
2014
- 2014-08-13 WO PCT/CN2014/000764 patent/WO2015070512A1/zh active Application Filing
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1988008410A1 (en) * | 1987-04-21 | 1988-11-03 | Hampton Roads Sanitation District | High-rate biological waste water treatment process using activated sludge recycle |
KR20050097098A (ko) * | 2004-03-30 | 2005-10-07 | 주식회사 한화건설 | 유입흐름제어형 막분리 활성슬러지공법을 이용한하폐수처리공법 |
CN101195506A (zh) * | 2006-12-08 | 2008-06-11 | 同济大学 | 厌氧/缺氧并联式脱氮除磷工艺 |
KR100838846B1 (ko) * | 2007-02-23 | 2008-06-17 | 주식회사 포스코건설 | 하수처리의 반류수 처리방법 |
CN101259979A (zh) * | 2007-12-28 | 2008-09-10 | 凌亮 | 一种利用微生物处理高浓度含氮废水的方法及装置 |
US20110132837A1 (en) * | 2009-12-07 | 2011-06-09 | Ch2M Hill, Inc. | Method and System for Treating Wastewater |
CN103601296A (zh) * | 2013-11-15 | 2014-02-26 | 玉溪师范学院 | 一种两相厌氧缺氧交替运行的d-a2/o污水处理反应器 |
Non-Patent Citations (1)
Title |
---|
HUO, WEI: "Study on Technology of hydrolytic acidification-Anaerobic/Anoxic/Aerobic Improved Process", TIANJIN CONSTRUCTION SCIENCE AND TECHNOLOGY, 31 October 2011 (2011-10-31), pages 50 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110759592A (zh) * | 2019-11-05 | 2020-02-07 | 天津中冀源环保科技有限公司 | 一种无外加碳源的水解酸化+a2/o2的污水处理方法 |
CN111217447A (zh) * | 2019-11-29 | 2020-06-02 | 段林卓 | 一种高寒地区室外冲水厕所污水处理工艺及装置 |
CN111217447B (zh) * | 2019-11-29 | 2022-06-03 | 段林卓 | 一种高寒地区室外冲水厕所污水处理工艺及装置 |
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