WO2012155790A1 - 一种利用微生物处理煤化工废水总氮的方法 - Google Patents

一种利用微生物处理煤化工废水总氮的方法 Download PDF

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WO2012155790A1
WO2012155790A1 PCT/CN2012/075034 CN2012075034W WO2012155790A1 WO 2012155790 A1 WO2012155790 A1 WO 2012155790A1 CN 2012075034 W CN2012075034 W CN 2012075034W WO 2012155790 A1 WO2012155790 A1 WO 2012155790A1
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pool
tank
anammox
wastewater
aerobic tank
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PCT/CN2012/075034
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English (en)
French (fr)
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凌亮
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Ling Liang
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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
    • 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
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process

Definitions

  • the invention relates to the field of biochemical environmental protection, in particular to a method for treating total nitrogen in coal chemical wastewater by using microorganisms. Background technique
  • nitrogen is one of the main elements that cause eutrophication in closed waters such as the lake. It causes the proliferation of algae, which leads to eutrophication of water bodies. The death of a large number of algae consumes oxygen in the water, and some algal protein toxins can be enriched in living organisms and poisoned through the food chain.
  • Countries have stricter restrictions on the emission of nitrogenous substances in wastewater. And with the continuous development of industrial and agricultural production, the water pollution caused by nitrogen is becoming more and more serious.
  • the continuous tightening of wastewater discharge standards is a common development trend in the world.
  • the removal of nitrogen and phosphorus for the purpose of controlling eutrophication has become the main goal of all countries. At present, developed countries such as the United States, France, Japan, etc. all have requirements for the treatment of total nitrogen in effluent, while China currently only has emission requirements for ammonia nitrogen.
  • the “Emission Standards for Pollutants in Urban Sewage Treatment Plants” (GB18918-2002) is the latest standard, which has a greater degree of improvement in systemicity, integrity and operability than the Integrated Wastewater Discharge Standard.
  • the standard is divided into four levels.
  • the first-class B standard is mainly implemented.
  • the requirements for total nitrogen are proposed, and the requirements for ammonia nitrogen and phosphorus are adjusted.
  • the Ministry of Environmental Protection issued the “Coke Emission Standard for Coking Industry” (draft for comments), which increased the total nitrogen assessment index for wastewater discharge from coking enterprises, and directly discharged wastewater requirements: total nitrogen 15mg/L ; indirect discharge wastewater requirements : Total nitrogen 30mg/L. It is foreseeable that the requirements for total nitrogen emissions will gradually receive the attention of the state in the future, and their emission standards will be similar to those of developed countries.
  • the classical A/0 denitrification process sets the anoxic, aerobic and sedimentation tanks in sequence, the anoxic tank for anoxic denitrification, and the aerobic tank for aerobic nitrification.
  • the reaction wherein the aerobic tank effluent is returned to the anoxic tank through the nitrifying liquid return line to provide N0 3 - or N0 2 - for denitrification.
  • the aerobic tank placed on the layout the N0 3 — or N0 2 — in the effluent cannot be completely and completely returned to the front anoxic tank, so that the effluent of the whole system must contain a certain concentration under normal conditions.
  • N0 3 — or N0 2 — when the denitrification in the anoxic cell at the front end of the system is not normal, the N0 3 — or M in the effluent will definitely be quite high.
  • the sediment in the sedimentation tank immediately following the aerobic tank in the layout must have a large amount of N0 3 - or N0 2 -, which is also indirect when draining mud. Causes N0 3 — or N0 2 — to pollute the environment.
  • the technical problem to be solved by the present invention is that the technical problem of the total effluent total nitrogen cannot be effectively controlled when the high-concentration nitrogen wastewater or other wastewater is treated by the A/0 process.
  • the technical solution adopted by the present invention is: a method for treating total nitrogen in coal chemical wastewater by using microorganisms, wherein the wastewater passes through a first aerobic tank, a first sedimentation tank, a facultative oxygen tank, and a second aerobic tank.
  • the second sedimentation tank is subjected to two-stage biochemical treatment, and the first aerobic tank, the anaerobic pool and the second aerobic tank are added with a microbial flora and a microbial carrier, and the characteristics are: the wastewater before entering the first aerobic tank After the Anammox pool, the Anammox pool is filled with anaerobic ammonium oxidizing bacteria and carrier activated carbon, and an aeration device and a stirring device are simultaneously disposed in the pool.
  • the water temperature of the Anammox pool is controlled at 25 to 35 ° C
  • the pH is controlled at 6 to 9
  • DO dissolved oxygen
  • MLVSS effective sludge concentration
  • the sludge from the first sedimentation tank is returned to the Anammox pool, and the sludge from the second sedimentation tank is returned to the anaerobic tank at a reflux ratio of 1: 1-2; the nitrification liquid of the first aerobic tank is returned to the Anammox pool, the second best The nitrification solution of the oxygen pool is refluxed to the anaerobic tank, and the reflux ratio is 1:2-8.
  • the Anammox pool is operated by agitation; when the treated waste water is B/O0.3, the Anammox pool is operated by aeration.
  • B is B0D (bio-oxygen consumption) and C is COD
  • the technical scheme described in the present invention is semi-open, and process steps and equipments that do not biochemical reactions, such as a sedimentation tank and an air flotation tank, can be added in the process flow.
  • the invention sets a first aerobic pool behind the Anammox pool, the first aerobic tank converts the ammonia nitrogen in the wastewater into nitro nitrogen, the first precipitation tank is arranged after the first aerobic tank, and the sludge in the first sedimentation tank is returned to Anammox
  • the first aerobic tank outlet is provided with a nitrifying return pipe to the head of the Anammox pool, and the nitro nitrogen produced in the first aerobic tank is brought to the Anammox pool, and the nitro nitrogen is denitrified in the Anammox pool.
  • the nitro nitrogen brought back and the ammonia nitrogen in the wastewater undergo an anaerobic ammonium oxidation reaction, and the nitro nitrogen and the ammonia nitrogen are directly reacted to complete the denitrification.
  • NH 4 +-N is used as an electron donor
  • N0 2 - -N is an electron acceptor
  • NH 4 +-N, N0 2 - -N are simultaneously converted into N 2
  • Anaerobic ammonium oxidation anaerobic ammonium oxidation is characterized by microbial anaerobic conditions, NH 4 + as an electron donor, N0 2 - or N0 3 - as an electron acceptor, ammonia nitrogen and nitrate nitrogen It becomes nitrogen and is discharged into the atmosphere.
  • the above two anaerobic ammonium oxidation (Anammox) processes have AG ⁇ 0 (G is energy), indicating that the reaction can proceed spontaneously.
  • the anaerobic ammonium oxidation process is a capacity reaction that provides energy for microbial growth.
  • NH 4 + is more reactive with N0 2 than NH 4 + and N0 3 .
  • ammonia oxidizing bacteria can use NH 4 + as an electron donor to reduce NO 2 — NH 2 OH, NH 2 NH 2 , NO and N 2 0 are important intermediate products.
  • Ways ANAMMOX currently estimated in three ways: (1) hydroxylamine (NH 2 OH) and N0 2 - generation reaction of N 2 0, N 2 0 and can be further converted to nitrogen, ammonia is oxidized to hydroxylamine; ( 2) Ammonia reacts with hydroxylamine to form hydrazine (NH 2 NH 2 ), which is converted to nitrogen and produces 4 reducing [H].
  • the ANAMMOX unit In the Anammox/C-A/02 process of the present invention, the ANAMMOX unit is at the forefront, a large amount of NH 4 + will be present in the influent, and another reaction substrate N0 2 will pass through the first aerobic tank. Nitrification is obtained by reflux.
  • the anaerobic pool and the second aerobic tank are the classic A/0 denitrification process combination, and the anaerobic tank completes the denitrification; the second aerobic tank completes the nitrification and provides corresponding denitrification reaction in the anaerobic tank.
  • N0 3 or N0 2 —, wherein the second aerobic tank outlet is provided with a nitrifying liquid return line to the hydration tank inlet.
  • the Anammox pool, the first aerobic tank and the first settling tank constitute the front section of the system, and the rear anaerobic tank, the second aerobic tank, and the second settling tank constitute the rear section of the system.
  • the whole system is shared by the two sections of sludge before and after. This design improves the operating efficiency and impact risk factor of the system.
  • TN in the second aerobic tank effluent is total nitrogen, that is, the sum of nitrite nitrogen, nitrate nitrogen, inorganic ammonium salt, dissolved ammonia and most organic nitrogen compounds in water.
  • the detection method is: alkali Ultraviolet spectrophotometry for potassium persulfate digestion, see GB 11894-89.
  • the function of the anaerobic tank in the whole system is to denitrify the effluent of the whole system, and it is effective to denitrify the N0 3 - or N0 2 in the aerobic tank drainage to nitrogen, so that the total nitrogen in the system effluent The content can be stably maintained at a very low concentration.
  • Adding a carbon source delivery pipe to the inlet of the anaerobic tank or from the Anammox pool construction overrunning pipe When the TN of the second aerobic tank is more than 20 mg/L, the carbon source is added, and the COD in the carbon source flow is added.
  • the ratio of TN in the effluent pool is between 3 and 6, so that the denitrification reaction can have more electron donors to ensure denitrification. Going smoothly.
  • the sedimentation tank completes the separation of the muddy water, and most of the sludge is returned to the Anammox pool or the anaerobic tank through the sludge return pipeline as needed, and the surplus sludge is discharged according to the needs and actual operating conditions.
  • the Anammox pool can also be equipped with an air floatation tank.
  • the Anammox pool inlet water is pretreated by the air floatation tank to remove a large amount of petroleum substances and suspended solids.
  • the process flow of the invention is simple, and the Anammox pool is used in the front section, and different operation modes can be adopted according to different water quality, so that it is suitable for different types of incoming water, lowering the construction cost, improving the processing capacity, and also saving energy and reducing consumption. .
  • Two-stage A/0 and anaerobic ammonium oxidative denitrification the effect of total nitrogen removal is significantly better than the existing A/0 process.
  • the ammonia nitrogen of the coking wastewater can be controlled below 15 mg/L
  • the COD can be controlled below 100 m g /L
  • other indexes can also reach the national first-class discharge standard.
  • the method for treating high-concentration nitrogen wastewater by using microorganisms disclosed in the invention is also applicable to refractory production wastewater such as pharmaceutical wastewater, fermentation wastewater, food enterprise wastewater, and can also be used for treatment of municipal wastewater and domestic sewage.
  • the whole process of the present invention uses the HSBEMBM microbial flora, and the treatment cost is significantly lower than the conventional activated sludge method due to the high efficiency of the HSBEMBM microbial flora.
  • FIG. 1 is a schematic diagram of a conventional A/0 water treatment process.
  • FIG. 2 is a schematic diagram of a process flow according to an embodiment of the present invention. Note: In the figure: A: sewage, B: sludge return, C: nitrate reflux. BEST MODE FOR CARRYING OUT THE INVENTION The following examples are operational tests performed by the present invention in a wastewater treatment project, which is a closed test, which is not accessible to a specific population and understands the test process.
  • the Anammox pool, the first aerobic tank, the first sedimentation tank, the anaerobic tank, the second aerobic tank, and the second sedimentation tank spatially constitute six main units, wherein the first sedimentation tank Set the sludge return pipe to the inlet of the Anammox pool.
  • the first aerobic tank outlet is provided with a nitrifying liquid return pipe to the Anammox pool inlet
  • the second settling tank is provided with a sludge return pipe to the oxycarbonate inlet, the second aerobic tank.
  • the water outlet is provided with a nitrifying liquid return pipe to the water inlet of the anaerobic tank.
  • the Anammox pool effluent enters the first aerobic tank for nitrification reaction.
  • the first aerobic tank effluent enters the first sedimentation tank for sludge water separation.
  • the sludge is returned to the Anammox pool.
  • the sludge reflux ratio is 1: 1 ⁇ 1: 2, and the effluent flows to A facultative pool.
  • the organic matter in the influent pool is used as the denitrifying carbon source and energy source, and the nitrate nitrogen in the nitrifying reflux liquid is used as the denitrifying nitrogen source to denitrify under the action of HSBEMBM® microorganism on the activated carbon carrier in the pool.
  • the denitrification reaction causes most of the pollutants such as NH 3 -N and COD in the wastewater to be removed and degraded.
  • the Anammox pool effluent flows into the first aerobic pond to degrade the organic matter in the wastewater by microorganisms.
  • the dissolved oxygen in the first aerobic tank wastewater is increased by the provision of a microporous aerator, oxygen is supplied to the microorganisms, and the mixture is stirred.
  • soda ash (N3 ⁇ 4C0 3 ) and phosphorus salts may be added as needed.
  • the soda ash is fed in stages according to the flow of the first aerobic pool, and the effluent of the first aerobic tank is returned to the Anammox pool through the nitrifying liquid return pipe.
  • the first aerobic tank can be operated according to the following parameters during normal operation:
  • the alkalinity is calculated by (CaC0 3 ): ⁇ 200mg/l MLSS: 3g/l or so
  • the dilution water is added to the inlet tank of the first aerobic tank, and the first aerobic tank is provided with a defoaming water pipeline.
  • the defoaming water pipe valve should be opened for defoaming.
  • the first aerobic tank effluent enters the first settling tank. 5 ⁇ 5L/ ⁇
  • the concentration of methanol in the inlet of the effluent pool is controlled to 2. 5 ⁇ 5L / h methanol (concentration > 99%).
  • the operating parameters of the facultative tank and the second aerobic tank were operated according to the Anammox pool and the first aerobic tank, respectively.
  • the sedimentation tank completes the separation of the muddy water, and most of the sludge is returned to the Anammox pool or the anaerobic tank through the sludge return pipeline as needed, and the surplus sludge is discharged according to the needs and actual operating conditions.
  • the effluent water quality treated by this example as shown in Table 1 is: C0D ⁇ 150m g /L, TN ⁇ 20m g /L, NH 3 -N ⁇ 3m g /l, and the sewage treatment effect is obviously better than the conventional A/0 Process.
  • Embodiment 2 is a diagrammatic representation of Embodiment 1:
  • High concentration coking wastewater COD about 4500m g / L, ammonia nitrogen about 350m g / L, volatile phenol about 1800m g / L, total cyanide about 70m g / L, before entering the system through the air floatation tank, through the air floater pre After removing oil and suspended solids and slag, it enters the Anammox pool.
  • the Anammox pool activates the aeration device. Under the aeration operation mode, the wastewater reacts with the anaerobic ammonium oxidizing bacteria in the pool with activated carbon as the carrier.
  • the temperature is controlled at 15 ⁇ 40°C, pH 6. 5 ⁇ 9. 0, dissolved oxygen 0. 6 ⁇ 3.
  • the effluent quality treated by this example as shown in Table 2 is: C0D ⁇ 150m g /L, T_N ⁇ 15m g /L, NH 3 -N ⁇ 3m g /L, the effect is obviously better than the traditional A/0 process .
  • Influent water quality (m g /L) effluent quality (m g /L) Conventional A/0 C0D ⁇ 250, T-N ⁇ 120, N -N ⁇ 25
  • the invention has C0D ⁇ 150, TN ⁇ 15, NH 3 -N ⁇ 3

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Description

一种利用微生物处理煤化工废水总氮的方法
技术领域
本发明涉及生化环保领域， 尤其是涉及一种利用微生物处理煤化工废水总氮的方法。 背景技术
目前氮元素是造成湖泊内海等封闭性水域富营养化的主要元素之一。 它会引起藻类的过 渡增殖， 造成水体的富营养化现象， 大量藻类死亡会耗去水中的氧， 而一些藻类蛋白质毒素 可富集在生物体内， 并通过食物链使人中毒。 各国对废水中含氮物质的排放都有较严格的限 制。 并且随着工农业生产的不断发展， 氮所产生的水体污染越来越严重。 污水排放标准的不 断收紧是目前世界各国普遍的发展趋势， 以控制富营养化为目的的氮、 磷脱除已成为各国主 要的奋斗目标。 目前发达国家如美国、 法国、 日本等， 均对处理出水中总氮有排放要求， 而 我国目前还只是对氨氮有排放要求。
《城镇污水处理厂污染物排放标准》 （GB18918-2002 )是目前最新的标准， 较《污水综合 排放标准》 的系统性、 完整性、 可操作性均有较大程度的提高。 该标准分四级标准， 在实际 工作中主要执行一级 B标准，提出了总氮的要求，对氨氮和磷的要求作了调整。 2010年 2月， 环境保护部发布 《炼焦工业污染物排放标准》 （征求意见稿）， 对炼焦企业废水排放增加了总 氮考核指标， 直接排放废水要求： 总氮 15mg/L; 间接排放废水要求： 总氮 30mg/L。 可以 预见的是今后对总氮排放的要求会逐渐得到国家的重视，其排放标准会同发达国家趋于近似。
如图 1所示， 经典的 A/0脱氮工艺在布局上按先后顺序设置了缺氧池、好氧池和沉淀池， 缺氧池进行缺氧反硝化反应， 好氧池进行好氧硝化反应， 其中好氧池出水通过硝化液回流管 道回流到缺氧池中为反硝化提供 N03—或 N02—。但是作为布局上设置在后的好氧池， 其出水中的 N03—或 N02—是不可能完全彻底的回流到前端缺氧池的， 这样整个系统的出水在正常情况下肯 定含有一定浓度的 N03—或 N02—； 而当系统前端的缺氧池中反硝化不正常时， 出水中的 N03—或 M 将肯定是相当高的。另外不管在上述的哪一种情况下， 在布局上紧随好氧池其后的沉淀池 中的沉泥也必然带有大量的 N03—或 N02—， 当排泥时也会间接的造成 N03—或 N02—对环境的污染。
无疑， 由于本身的工艺布局设置局限和反硝化运行时控制不利等非正常情况将导致经典 的 A/0脱氮工艺应付日趋严格的排放标准显得力不从心。 发明内容
本发明要解决的技术问题是处理高浓度氮废水或其他废水采用 A/0工艺时， 其出水总氮 无法得到有效控制的技术问题。
为解决上述技术问题， 本发明所采用的技术方案是： 一种利用微生物处理煤化工废水总 氮方法， 废水依次经过第一好氧池、 第一沉淀池、 兼氧池、 第二好氧池和第二沉淀池进行二 段生化处理， 第一好氧池、 兼氧池、 第二好氧池中添加有微生物菌群和微生物载体， 其特征 在于： 废水在进入第一好氧池前先经过 Anammox池， 该 Anammox池中添加有厌氧氨氧化菌 及载体活性炭， 池内同时设置有曝气装置和搅拌装置。
进一步地， 所述 Anammox池的水温控制在 25〜35°C， pH控制在 6~9， DO (溶解氧） < 0. 5mg/l , MLVSS (有效污泥浓度） 在 3_6g/l。
第一沉淀池的污泥回流至 Anammox池， 第二沉淀池的污泥回流至兼氧池， 回流比为 1 : 1-2； 第一好氧池的硝化液回流至 Anammox池， 第二好氧池的硝化液回流至兼氧池， 回流比 为 1 : 2~8。
更进一步地： 当所处理废水的 B/C<0. 3时， Anammox池采用搅拌方式运行； 所处理废 水的 B/O0. 3时， Anammox池采用曝气方式运行。 其中， B为 B0D (生物耗氧量）， C为 COD
(化学耗氧量）。
本发明所述的技术方案为半开放式， 可以在工艺流程中增加不发生生化反应的工艺步骤 和设备， 如沉淀池、 气浮池等。
本发明在 Anammox池后设置第一好氧池，第一好氧池将废水中氨氮转化为硝基氮，第一 好氧池后设置第一沉淀池， 第一沉淀池的污泥回流至 Anammox池首部，同时第一好氧池出口 设置硝化回流管至 Anammox池首部， 将第一好氧池中产生的硝基氮带至 Anammox池， 硝基 氮在 Anammox池中完成反硝化反应。 同时带回的硝基氮与废水中的氨氮发生厌氧氨氧化反 应， 使硝基氮和氨氮直接反应完成脱氮。
在厌氧或缺氧的条件下,以 NH4+-N为电子供体, N02— -N为电子受体,把 NH4+-N、 N02— -N同时 转化为 N2 ,称之为厌氧氨氧化，厌氧氨氧化反应的特点是微生物在厌氧条件下， 以 NH4 +为电子 供体， 以 N02—或 N03—为电子受体， 将氨氮和硝态氮变成氮气排入大气中， 其主要反应如下： NH4++ N02—→N2+2 H20 AG= -358kJ/mol NH4+
5NH4++3 N03—→4 N2+9H20+2H+ AG = -297kJ/mol NH4+
上述两种厌氧氨氧化 (Anammox)过程的 AG<0 ( G为能量）， 说明反应可自发进行， 厌氧 氨氧化过程的是一个产能的反应， 可以提供能量供微生物生长。 而且 NH4+与 N02—反应比 NH4+ 与 N03—更容易进行。在缺氧条件下，氨氧化菌可以利用 NH4 +作电子供体将 N02—还原， NH2OH、 NH2 NH2、 NO和 N20等是重要的中间产物。 厌氧氨氧化的途径目前推测有三种： （1 ) 羟氨 ( NH2OH) 和 N02—生成 N20的反应， 而 N20可以进一步转化为氮气， 氨被氧化为羟氨； （2) 氨和羟氨反应生成联氨 （NH2 NH2)， 联氨被转化为氮气并生成 4个还原性 [H]。
在本发明这种 Anammox/C -A/02工艺中， ANAMMOX单元处于最前端， 进水中将有大量 NH4 +存在， 而另一种反应底物 N02—将从第一好氧池通过硝化回流获得。
如下的一些措施有利于使第一好氧池单元实现 N02—的积累：
1) 第一好氧池中投加活性炭， 能固定细胞， 使亚硝化菌富集。
2) H: 8.2-9.1
3) DO: 0.8-2.5mg/L。
兼氧池、 第二好氧池即为经典的 A/0脱氮工艺组合， 兼氧池完成反硝化； 第二好氧池完 成硝化作用， 并为兼氧池中的反硝化反应提供相应的 N03—或 N02—， 其中第二好氧池出水口设置 硝化液回流管道至兼氧池进水口。 Anammox池、第一好氧池和第一沉淀池构成系统的前段部 分， 后面的兼氧池、 第二好氧池、 和第二沉淀池构成系统的后段部分。 整个系统由前后两段 污泥共同承担负荷，这样的设计提高了系统的运行效率和抗冲击风险系数。
第二好氧池出水中 T-N的含义是总氮， 即水中亚硝酸盐氮、 硝酸盐氮、 无机铵盐、 溶解 态氨及大部分有机含氮化合物中氮的总和， 其检测方法是： 碱性过硫酸钾消解紫外分光光度 法， 见 GB 11894-89。兼氧池在整个系统中起到的作用就是对整个系统出水进行反硝化，确实 有效的将由好氧池排水中的 N03—或 N02—反硝化为氮气，从而使得系统出水中的总氮含量能够稳 定地保持非常低浓度。 在兼氧池的进水处设置外加碳源投放管或是从 Anammox池建超越管 道至此，当第二好氧池出水 T-N超过 20mg/L， 投放外加碳源， 外加碳源流量中的 COD与兼氧 池进水的 T-N的比例在 3— 6之间，使得反硝化反应能够有恰当多的电子供体保证反硝化反应 顺利进行。 沉淀池完成泥水分离，通过污泥回流管道根据需要将大部分污泥回流至 Anammox池或兼 氧池， 根据需要和实际运行状况将富余污泥排放。
Anammox池前还可以设置有气浮池， Anammox池进水根据需要先经过气浮池预处理去 除大量的石油类物质和悬浮物。 本发明工艺流程简洁， 前段采用 Anammox池， 能够根据不同水质采用不同运行方式， 这 样就适用于不同性质的来水， 降低了建造成本， 提高了处理能力， 同时也能起到节能降耗的 作用。 两级 A/0与厌氧氨氧化脱总氮， 脱总氮效果明显优于现有的 A/0工艺。
经本发明处理后，焦化废水氨氮可以控制在 15mg/L以下, COD可以控制在 100mg/L以下， 其他指标也可以达到国家一级排放标准。除焦化废水外，本发明所公开的利用微生物处理高浓 度氮废水的方法，也适用于制药废水、 发酵废水、 食品企业废水等难降解的生产废水，还可以 用于市政废水、 生活污水的处理。 本发明整个过程使用 HSBEMBM微生物菌群， 由于 HSBEMBM 微生物菌群的高效力使得处理成本明显低于传统活性污泥方法。
附图说明
图 1为常规 A/0水处理工艺示意图。 图 2为本发明实施例工艺流程示意图。 注： 图中： A :污水， B :污泥回流， C :硝化液回流。 具体实施方式 以下实施例是本发明在某废水处理工程中所做的运行试验， 该试验为封闭试验， 非特定 人群不能接触、 了解试验过程。
如图 2所示， 以 Anammox池、 第一好氧池、 第一沉淀池、 厌氧池、 第二好氧池、 第二沉 淀池在空间上构成了六个主体单元， 其中第一沉淀池设置污泥回流管道至 Anammox池进水 口， 第一好氧池出水口设置硝化液回流管道至 Anammox池进水口， 第二沉淀池设置污泥回 流管道至兼氧池进水口， 第二好氧池出水口设置硝化液回流管道至兼氧池进水口。 实施例一：
高浓度硝基苯工业废水，流量为 100 m Vh,其 COD > 5500 m g /L,氨氮 > 350 m g /L， B/C=0. 27， 进入系统前先经过气浮池， 经气浮池预处理除去油和悬浮物及渣后进入 Anammox 池中， 在微量搅拌的情况下废水与 Anammox池中以活性炭为载体的厌氧氨氧化菌进行生化 反应， 降解污水中一部分有害物质， 提高了污水的可生化性， 同时进行反硝化反应和厌氧氨 氧化反应脱氮。 为了满足 Anammox 池生化反应的需要， 为微生物提供营养物磷源， 在 Anammox池内设置了磷盐投加管道。 Anammox池运行中：
P: 4mg/l PH: 7. 5 水温： 30 °C
Anammox池出水进入第一好氧池进行硝化反应， 第一好氧池出水进入第一沉淀池进行泥 水分离，污泥回流到 Anammox池，污泥回流比例 1： 1〜 1： 2, 出水流到兼氧池。 兼氧池中以进 水中的有机物作为反硝化的碳源和能源， 以硝化回流液中的硝态氮作为反硝化的氮源， 在池 中活性炭载体上的 HSBEMBM®微生物作用下进行反硝化脱氮反应， 使废水中的 NH3—N、 COD等 污染物质得以大部分去除和降解。
为了满足 Anammox池和第一好氧池生化反应的需要， 为微生物提供磷和适宜的水温， 在 Anammox池和第一好氧池考虑了蒸汽加热设施，运行中应根据实际情况进行操作， Anammox 池正常运行时可按以下参数进行操作：
溶解氧： <0. 5mg/l P: 3-4mg/l
水温： 30°C PH: 7〜8
Anammox池出水流入第一好氧池由微生物降解废水中的有机物。 为了满足生化要求， 通 过设置的微孔曝气器来增加第一好氧池废水中的溶解氧， 为微生物提供氧和对混合液进行搅 拌。另外还可根据情况需要投加纯碱 (N¾C03)及磷盐。纯碱按第一好氧池混合液流向分段投加， 第一好氧池出水通过硝化液回流管回流至 Anammox池， 正常运转时第一好氧池可按以下参 数进行操作：
溶解氧 （DO): 2-4mg/l P: 〜3mg/l以上 PH: 〜7. 5
碱度以 （CaC03) 计： 〉200mg/l MLSS: 3g/l左右
适宜水温： 25〜30°C
为了保证生化处理的有害物质浓度控制在允许范围内， 在第一好氧池的进水槽中加入稀 释水， 第一好氧池上设有消泡水管道， 当第一好氧池中泡沫多时， 应打开消泡水管道阀门进 行消泡。 第一好氧池出水进入第一沉淀池。 在兼氧池进水处设置甲醇投放管道控制流量为 2. 5〜5L/h 甲醇 (浓度〉99%)。 兼氧池和 第二好氧池运行参数分别按 Anammox池和第一好氧池操作。
沉淀池完成泥水分离， 通过污泥回流管道根据需要将大部分污泥回流至 Anammox池或 兼氧池， 根据需要和实际运行状况将富余污泥排放。
如表 1所示经本实施例处理后的出水水质为： C0D〈150m g /L, T-N<20m g /L, NH3-N<3m g /l,污水处理效果明显好于常规 A/0工艺。
表 1
Figure imgf000008_0001
实施例二:
高浓度焦化废水， 其 COD约 4500m g /L,氨氮约 350m g /L， 挥发酚约 1800m g /L， 总 氰约 70m g /L， 进入系统前先经过气浮池， 经过气浮器的预处理除去油和悬浮物及渣后， 进 入 Anammox池中， Anammox池启用曝气装置， 在曝气运行方式下废水与池中以活性炭为载 体的厌氧氨氧化菌进行生化反应，控制温度在 15〜40°C , pH值 6. 5〜9. 0,溶解氧 0. 6〜3. 2mg/L, 污泥沉降比 SV3。为 10%〜25%,停留时间 12〜28小时，进水 C0D指标 1500〜3500 mg/L,出水 C0D 指标 400〜650mg/L, COD降解效率 40%〜75%,出水时各种对硝化和反硝化有影响的各种指标不 超过 50mg/L; 从 Anammox池出来的废水进入第一好氧池。 其他的实施方式同实施例一。
如表 2 所示经本实施例处理后的出水水质为： C0D〈150m g /L, T_N〈15m g /L, NH3-N<3m g /L, 效果明显好于用传统 A/0工艺。
表 2
进水水质（m g /L) 出水水质（m g /L) 常规 A/0 C0D<250, T-N< 120, N -N<25
C0D〜4500，氨氮〜 350， 挥发酚〜
1800， 氰化物〜 70
本发明 C0D< 150， T-N< 15, NH3-N<3

Claims

1. 一种利用微玍物处埋煤化丄 j发水^風的万法， j发水侬次 a弟一好 ¾池、 弟一沉浞池、 m 氧池、 第二好氧池和第二沉淀池进行二段生化处理， 第一好氧池、 兼氧池、 第二好氧池中添 加有微生物菌群和微生物载体， 其特征在于： 废水在进入第一好氧池前先经过 Anammox池， 该 Anammox池中添加有厌氧氨氧化菌及载体活性炭， 池内同时设置有曝气装置和搅拌装置。
2. 如权利要求 1 所述的一种利用微生物处理煤化工废水总氮的方法， 其特征在于： 所述 Anammox池的水温控制在 25〜35°C， pH控制在 6~9， DO (溶解氧） <0.5mg/l， MLVSS (有 效污泥浓度） 在 3-6g/l。
3. 如权利要求 2所述的一种利用微生物处理煤化工废水总氮的方法， 其特征在于： 第一沉淀 池的污泥回流至 Anammox池， 第二沉淀池的污泥回流至兼氧池， 回流比为 1 : 1-2； 第一好 氧池的硝化液回流至 Anammox池， 第二好氧池的硝化液回流至兼氧池， 回流比为 1 : 2~8。
4. 如权利要求 3所述的一种利用微生物处理煤化工废水总氮的方法， 其特征在于： 当所处理 废水的 B/C<0.3时， Anammox池采用搅拌方式运行； 所处理废水的 B/O0.3时， Anammox 池采用曝气方式运行。
1
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110240276A (zh) * 2019-07-24 2019-09-17 太仓新瑞节能设备有限公司 生态污水处理设备及其排污装置

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102249481A (zh) * 2011-05-16 2011-11-23 浙江汉蓝环境科技有限公司 一种利用微生物处理煤化工废水总氮的方法
CN103193357A (zh) * 2012-01-04 2013-07-10 上海巴安水务股份有限公司 木薯酒精废水好氧处理系统
CN102757127B (zh) * 2012-07-13 2013-10-23 浙江汉蓝环境科技有限公司 一种利用微生物处理水煤浆气化废水的方法
CN102718370A (zh) * 2012-07-13 2012-10-10 浙江汉蓝环境科技有限公司 一种利用微生物处理焦化废水总氮的方法
CN102795748A (zh) * 2012-09-06 2012-11-28 浙江汉蓝环境科技有限公司 一种利用好氧与两级缺氧好氧处理废水的方法
CN103408138B (zh) * 2013-07-16 2016-01-13 中石化宁波工程有限公司 含高cod、高氨氮煤化工污水的两段式生物处理设备
CN103466905A (zh) * 2013-10-10 2013-12-25 浙江汉蓝环境科技有限公司 利用微生物处理废水中硝基苯及苯胺的方法
CN105906057A (zh) * 2016-06-16 2016-08-31 徐州工程学院 一种高浓度氨氮化工废水的生物处理方法
US11427489B2 (en) * 2017-12-13 2022-08-30 Toyo University Carrier for retaining anammox bacteria for use in wastewater treatment, anammox bacteria-adhered particle, and wastewater treatment apparatus using the carrier
CN109368928A (zh) * 2018-11-21 2019-02-22 杭州宸祥环境工程有限公司 一种基于短程反硝化反应的除磷脱氮装置及其方法
CN109485155B (zh) * 2019-01-09 2022-07-12 广东嘉园生物技术有限公司 同步厌氧氨氧化和产甲烷的膜生物反应器及废水处理方法
CN112592003B (zh) * 2020-12-28 2023-04-18 四川省生态环境科学研究院 一种酿酒废水处理方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003053387A (ja) * 2001-08-10 2003-02-25 Kurita Water Ind Ltd 生物学的窒素除去方法
CN1562820A (zh) * 2004-02-10 2005-01-12 凌亮 一种利用微生物处理焦化废水的方法
CN1778725A (zh) * 2005-10-14 2006-05-31 单明军 节能型焦化废水脱氮工艺
CN101054236A (zh) * 2007-05-28 2007-10-17 北京市环境保护科学研究院 亚硝化－厌氧氨氧化单级生物脱氮方法
CN101254980A (zh) * 2008-03-25 2008-09-03 浙江大学 低碳氮比高氨氮化工综合废水的生物脱氮系统及方法
CN102249481A (zh) * 2011-05-16 2011-11-23 浙江汉蓝环境科技有限公司 一种利用微生物处理煤化工废水总氮的方法

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101259977B (zh) * 2007-12-28 2011-06-22 凌亮 利用微生物脱总氮的方法
CN101792243B (zh) * 2010-04-12 2011-07-20 哈尔滨工业大学 两级生物选择反硝化除磷脱氮污水处理装置及方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2003053387A (ja) * 2001-08-10 2003-02-25 Kurita Water Ind Ltd 生物学的窒素除去方法
CN1562820A (zh) * 2004-02-10 2005-01-12 凌亮 一种利用微生物处理焦化废水的方法
CN1778725A (zh) * 2005-10-14 2006-05-31 单明军 节能型焦化废水脱氮工艺
CN101054236A (zh) * 2007-05-28 2007-10-17 北京市环境保护科学研究院 亚硝化－厌氧氨氧化单级生物脱氮方法
CN101254980A (zh) * 2008-03-25 2008-09-03 浙江大学 低碳氮比高氨氮化工综合废水的生物脱氮系统及方法
CN102249481A (zh) * 2011-05-16 2011-11-23 浙江汉蓝环境科技有限公司 一种利用微生物处理煤化工废水总氮的方法

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
ZHAO, FENG ET AL.: "Feasibility of ANAMMOX Enhancement in A2/O Process", CHINA WATER & WASTEWATER, vol. 25, no. 3, February 2009 (2009-02-01), pages 7 - 10 *
ZHAO, ZONGSHENG ET AL.: "A Study on ANAMMOX A2/O Process for Ammonium-rich Leachates", ENVIRONMENTAL SCIENCE, vol. 24, no. 6, November 2003 (2003-11-01), pages 121 - 124 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110240276A (zh) * 2019-07-24 2019-09-17 太仓新瑞节能设备有限公司 生态污水处理设备及其排污装置

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