WO2017096693A1 - 一种用于氧化法脱硝的废水脱硝处理系统 - Google Patents

一种用于氧化法脱硝的废水脱硝处理系统 Download PDF

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WO2017096693A1
WO2017096693A1 PCT/CN2016/070848 CN2016070848W WO2017096693A1 WO 2017096693 A1 WO2017096693 A1 WO 2017096693A1 CN 2016070848 W CN2016070848 W CN 2016070848W WO 2017096693 A1 WO2017096693 A1 WO 2017096693A1
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membrane
wastewater
filtrate
treatment system
module
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PCT/CN2016/070848
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English (en)
French (fr)
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朱核光
熊靓
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深圳广昌达环境科学有限公司
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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
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • 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
    • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C02F2101/163—Nitrates
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C02F2101/166—Nitrites
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents

Definitions

  • the invention relates to a treatment system, in particular to a wastewater denitration treatment system for oxidizing denitration.
  • SO 2 and NOx are two major gaseous atmospheric pollutants that are produced primarily by combustion or other chemical processes and are emitted to the atmosphere with the flue gases.
  • the denitration of flue gas mainly adopts two types of reduction method and oxidation method.
  • the reduction method uses ammonia or urea as a reducing agent, V 5 O 2 as a catalyst at a temperature of 300-400 C, or does not use a catalyst at a temperature of 1000 C.
  • the NOx in the flue gas is selectively reduced to nitrogen under conditions.
  • the selective catalytic reduction method requires a catalyst containing a transition metal element, and the catalyst is subject to wear by dust in the flue gas and needs to be frequently replaced, and at the same time, there are problems such as ammonia leakage and severe temperature conditions, and the use thereof is limited.
  • the selective non-catalytic reduction method does not meet the stringent NOx emission standards and its use is limited.
  • the oxidation method uses oxidants such as ozone and H 2 O 2 to oxidize NO in NOx (accounting for more than 90% of NOx in the flue gas) to NO 2 or N 2 O 5 (NO2 accounts for more than 90%). It is removed together with SO 2 in the flue gas in a wet scrubber.
  • Oxidation denitration has certain advantages in terms of cost of use and applicability due to its simple process, no need to use a catalyst, and a wide temperature range.
  • the denitrification by oxidation will produce a certain amount of wastewater containing nitrogen to be treated.
  • the wastewater discharged from these desulfurization and denitration devices contains both desulfurization and denitrification products, and the concentration is very high, often containing about 5% of salt content, which is formed by using lime or limestone as an absorbent.
  • Both calcium sulfite and calcium sulphate are compounds which are poorly soluble in water and can be removed as a suspended solid by coagulation precipitation.
  • the sodium sulfite and sodium hydrogen sulfite and sodium sulfate produced by using NaOH as an absorbent are easily soluble in water, and industrially, aerating sodium sulfite and sodium hydrogen sulfite are generally oxidized to sodium sulfate, and then evaporated by crystallization. .
  • the nitrite and nitrate formed by oxidative denitration are either present in wastewater alone or mixed with sulfur-containing salts such as sodium sulfate. Due to their solubility in water, coagulation and sedimentation methods generally have limited removal effects.
  • Evaporative crystallization is used to achieve the purpose of desalting. Evaporative crystallization requires 60-70 kW of electricity to process one ton of water.
  • the Na 2 SO 4 converted into sulfur compounds in the wastewater after sufficient aeration oxidation treatment is stable in the environment and generally not used as a pollutant, and can be directly discharged.
  • the nitrate in the wastewater brought by denitration will cause the total nitrogen in the wastewater to exceed the standard and must be removed before it can be directly discharged.
  • Biological denitrification is the use of microbial denitrification characteristics (also known as anaerobic respiration) to convert NO 2 and NO 3 into harmless nitrogen. NO 2 and NO 3 are used as electron acceptors.
  • Nitrifying microorganisms need to obtain a certain amount of carbon sources and trace elements as a nutrient source in the denitrification process.
  • Biological denitrification has been applied in the treatment of municipal wastewater.
  • biological denitrification devices that have been used in the field of wastewater treatment are generally integrated with biological nitrification devices. This is because the nitrogenous substances contained in common urban wastewater are mainly ammonia, and ammonia is firstly nitrated by microorganisms. It becomes nitrous acid and nitric acid and is then converted to nitrogen by denitrification. This system generally has a low concentration of ammonia nitrogen, only a few hundred ppm.
  • urban wastewater generally contains the carbon source required for biological denitrification, and no additional carbon source is needed.
  • the nitrifying bacteria and the denitrifying bacteria and other wastewater-treated heterotrophic bacteria are symbiotic together, and a stable bacterial micelle floc structure can be formed, so that the microorganisms can be separated in the subsequent sedimentation tank and partially returned to the biological treatment.
  • the system is to ensure that it is in the wastewater treatment system.
  • such a system is not suitable for the treatment of nitrogen-containing wastewater generated by a flue gas denitration system. The reasons are as follows: 1. Flue gas denitration nitrogen-containing wastewater does not contain ammonia nitrogen, only nitrate and nitrite; 2.
  • Flue gas denitration nitrogenous wastewater contains high concentration of salt, the concentration of salt can reach 5-10%; 4.
  • the concentration of nitrate contained is also several times or even hundreds of times higher than that in urban wastewater.
  • the flue gas oxidation denitration technology will produce a certain amount of high-concentration nitric acid wastewater to be treated, and the evaporation crystallization method has high power consumption and high running cost.
  • the suitable nitrogen load is low and cannot be used in the flue gas treatment system. Therefore, there is an urgent need for a device that can be specifically treated for the treatment of nitrate-containing wastewater produced by oxidation after denitrification.
  • the invention mainly provides an effective biological denitrification and denitrification treatment system for the oxidation method flue gas denitration system, which utilizes denitrification of microorganisms to reduce nitrogen-containing compounds in the wastewater to N2, thereby being removed from the wastewater.
  • a wastewater denitration treatment system for oxidizing denitration comprising: a membrane bioreactor, a degassing device and a filtrate tank; the membrane bioreactor is provided with a wastewater inlet, a carbon source injection port, and a trace element injection port a lye injection port and an excess sludge discharge outlet; the membrane bioreactor is provided with a stirrer, a pH probe and a membrane filter assembly, and the excess sludge discharge outlet is disposed behind the membrane filter assembly,
  • the membrane filter assembly and the deaeration device are connected by a pipeline, a control valve is arranged on the pipeline between the membrane filtration assembly and the deaeration device, and an upper portion of the degassing device is provided with an exhaust valve, and the deaeration device and
  • the filtrate pool is connected by a pipeline, and a filtrate pump is arranged on the pipeline between the deaerator and the filtrate tank.
  • the membrane bioreactor is further provided with a flushing pump for flushing the membrane filtration module.
  • an excess sludge discharge pump is disposed on the pipeline between the excess sludge discharge outlet and the membrane bioreactor.
  • the membrane filtration module is a flat membrane module or a hollow fiber membrane module.
  • the flat membrane module is a group of flat membranes placed in parallel as a basic membrane module unit, each unit having a set of fixed parallel membranes and a gasket and a clamp for clamping them together and an integrated filtrate outlet.
  • the hollow fiber membrane module is composed of a bundle of hollow fiber membranes, and each unit has a set of clamps for fixing the hollow fiber membranes, a separator separating the mixed liquid and the filtrate, and a liquid collection zone for the filtrate.
  • An application of the above treatment system is characterized in that the concentration of NO 2 and NO 3 in the wastewater is in the range of 1-20 g/L, and the molar ratio of NO 2 and NO 3 is in the range of 0-2, salt concentration Below 30g/L, pH is 7-9.
  • the wastewater has a residence time of 7-9 hours in the membrane bioreactor.
  • the invention has the beneficial effects that: according to the invention, the waste water generated when the flue gas treatment is performed by the oxidation denitration can be treated by the biological denitrification method, and the energy consumption and the treatment cost are large compared with the evaporation crystallization method. reduce.
  • Figure 1 is a schematic view of the structure of the present invention
  • 1 wastewater inlet 1 membrane bioreactor, 3 agitator, 4 membrane filtration module, 5 degassing device, 6 filtrate pump, 7 filtrate pool, 8 filtrate outlet, 9 excess sludge discharge pump, 10 residual pollution Mud discharge outlet, 11 flushing pump, 12 carbon source injection port, 13 trace element injection port, 14 lye injection port, 15 control valve, 16 exhaust valve.
  • a wastewater denitration treatment system for oxidative denitration comprising a membrane bioreactor 2, a degassing device 5 and a filtrate tank 7;
  • the device 2 is provided with a waste water inlet 1, a carbon source injection port 12, a trace element injection port 13, an alkali liquid injection port 14 and an excess sludge discharge outlet 10;
  • the membrane bioreactor 2 is provided with a stirrer 3, a pH probe And a membrane filter assembly 4, further provided with a flushing pump 11 for flushing the membrane filter assembly, the excess sludge discharge outlet 10 being disposed behind the membrane filtration module 4, the membrane filtration assembly 4 and the degasser 5 passing
  • the pipe connection, the pipe between the membrane filter assembly 4 and the deaeration device 5 is provided with a control valve 15, an upper portion of the degassing device 5 is provided with an exhaust valve 16, and the degassing device 5 and the filtrate pool 7 pass through the pipeline a pipeline pump 6 is
  • the wastewater treated by the system is required.
  • the concentration of NO 2 and NO 3 in the wastewater is in the range of 1-20 g/L, and the molar ratio of NO 2 and NO 3 is in the range of 0-2, and the salt concentration is low.
  • the pH is between 7 and 9.
  • the residence time of the wastewater in the membrane bioreactor is 7-9 hours.
  • the second embodiment is different from the first embodiment in that the membrane filtration module is a hollow fiber membrane module, and the hollow fiber membrane module has a bundle of hollow fiber membranes as a basic unit, and each unit has a set of fixed hollow fiber membranes.
  • the jig is composed of a separator separating the mixture and the filtrate and a liquid collection zone of the filtrate.
  • the oxidizing flue gas denitration process uses an oxidant to oxidize NOx (usually 90% or more of NO) in the exhaust gas to a higher valence NOx (mainly NO 2 ), and will be expensive in the subsequent desulfurization scrubber. The NOx of the state is washed into the liquid washing liquid to remove them from the gas phase.
  • the discharged wastewater discharged from the washing liquid also contains these nitrogen-containing compounds. Due to the total nitrogen control of the discharged wastewater, wastewater containing these nitrogenous compounds must be disposed of prior to discharge.
  • the invention utilizes the principle of denitrification of microorganisms, and treats the wastewater by using denitrification membrane bioreactor technology, so that the nitrate and nitrite contained in the wastewater are reduced to N 2 under the action of microorganisms, thereby making the wastewater The nitrate-containing compound is removed by harmlessness.
  • the membrane bioreactor of the present invention refers to a membrane filtration system placed in a bioreactor such that water and small molecule compounds can exit the reactor through the membrane while microorganisms and other suspended solids can remain in the reactor. Since the membrane bioreactor does not use subsequent precipitation separation, the concentration of microorganisms in the reaction tank can be made much higher than that of the general bioreactor, and the load can be much higher than that of the conventional reaction tank, and the reaction efficiency is much higher. In the ordinary reaction device. The concentration of NO 2 and NO 3 in the wastewater to which the present invention is applied is in the range of 1-20 g/L.
  • the molar ratio of NO 2 and NO 3 is between 0 and 2
  • the total salt concentration in the wastewater is less than 30 g/L
  • the pH is 7-9
  • the sludge concentration in the reaction tank is 20- 38 (g/L).
  • the carbon source required for the reaction may be carried out by commercially available low molecular organic substances such as sodium acetate, ethanol or methanol, or by introduction of an organic waste water, or any waste liquid or waste containing a volatile organic acid component. Trace elements can also be used by waste water from wastewater plants.
  • the waste water membrane bioreactor mixes with carbon source and trace elements discharged from the carbon source inlet and the trace element discharge inlet to provide sufficient energy and nutrient components of the denitrifying bacteria in the bioreactor, and the hydraulic power of the wastewater in the reactor
  • the retention time is 8 hours, and the nitrate and nitrite contained in the wastewater are used as electron donors for the energy metabolism of denitrifying bacteria, and finally converted into harmless nitrogen.
  • Denitrifying bacteria use a part of the carbon source as a nutrient to grow.
  • the treated wastewater enters the membrane filtration module for filtration, and the filtrate is pumped into the filtration liquid pool by the filtrate through the degassing device, and discharged into the drainage pipe of the plant through the discharge port.
  • the membrane surface of the membrane module is hydraulically flushed using a flushing pump.
  • the mixed liquid refers to a mixture of waste water which enters at an initial state and a mixture of a carbon source and a trace element which are discharged from a carbon source discharge port and a trace element discharge port, and a pH-adjusting alkali solution
  • the filtrate refers to a membrane which passes through the membrane. Filter the filtered liquid.

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  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
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Abstract

一种用于氧化法脱硝的废水脱硝处理系统，包括膜生物反应器（2）、脱气装置（5）和滤液池（7）；膜生物反应器（2）设有废水入口（1）、碳源注入口（12）、微量元素注入口（13）、碱液注入口（14）和剩余污泥排放出口（10）；膜生物反应器（2）内设有搅拌器（3）、PH探头和膜过滤组件（4），剩余污泥排放出口（10）设置在膜过滤组件（4）的后方，膜过滤组件（4）与脱气装置（5）通过管道连接，膜过滤组件（4）与脱气装置（5）之间的管道上设有控制阀门（15），脱气装置（5）的上部设有排气阀门（16），脱气装置（5）和滤液池（7）通过管道连接，脱气装置（5）和滤液池（7）之间管道上设有滤液泵（6）。

Description

一种用于氧化法脱硝的废水脱硝处理系统 技术领域
本发明涉及一种处理系统，具体涉及一种用于氧化法脱硝的废水脱硝处理系统。
背景技术
SO2和NOx是两种主要的气体性大气污染物，它们主要由燃烧或其它化工过程产生并随烟气排放到大气中。目前，烟气的脱硝主要采用还原法和氧化法两类，还原法使用氨或尿素作为还原剂，使用V5O2作为催化剂在300-400C的温度条件下，或不使用催化剂在1000C的温度条件下将烟气中的NOx选择性地还原成氮气。选择性催化还原法由于需要使用含过渡金属元素的催化剂，催化剂会受到烟气中尘埃的磨损而需要经常更换，同时有氨泄漏及温度条件苛刻等问题，其使用受到一定的限制。选择性非催化还原法则脱硝效果无法满足严格的NOx排放标准，因而其使用也受到限制。而氧化法则使用臭氧和H2O2等氧化剂将NOx中的NO(占烟气中NOx的90％以上)氧化成更容易洗脱的NO2或N2O5(NO2占90％以上)，并和烟气中的SO2一起在湿式洗涤塔中去除。氧化法脱硝由于工艺简单，无需使用催化剂，适用温度范围广，因此在使用成本和适用性上有一定优势。但是氧化法脱硝会产生一定量的含硝废水需要处理。由于脱硫和脱硝往往同时进行，这些脱硫脱硝装置所排的废水，同时含有脱硫和脱硝产物，而且浓度很高，往往含有5％左右的含盐量，采用石灰或石灰石做吸收剂时所形成的亚硫酸钙和硫酸钙都是难溶与水的化合物，可以作为悬浮固体通过混凝沉淀去除。而使用NaOH作为吸收剂时所产生的亚硫酸钠和亚硫酸氢钠以及硫酸钠都易溶于水，在工业上一般采用曝气将亚硫酸钠和亚硫酸氢钠氧化成硫酸钠，然后蒸发结晶的方法除去。氧化法脱硝所形成的亚硝酸盐和硝酸盐，要么单独存在于废水中，要么和硫酸钠等含硫盐分混在一起，由于它们易溶于水的特性，混凝沉淀法一般去除效果有限，一般需使用蒸发结晶法来达到除盐的目的。蒸发结晶的方法处理一吨水需要消耗60-70度电。这样高的电耗及由此带来的高成本，很大程度上限制了蒸发结晶法的使用。废水中的含硫化合物经充分曝气氧化处理后转化成的Na2SO4，在环境中很稳定，一般不作为污染物，可以直接进行排放。脱硝所带来的废水中的硝酸盐，由于会引起废水总氮超标，必须进行脱除后才能直接排放。 生物反硝化是利用微生物在缺氧条件下的反硝化特性(也成为厌氧呼吸机制)将NO2和NO3转化成无害的氮气，NO2和NO3是作为电子受体获得利用，反硝化微生物在反硝化过程中需要获得一定量的碳源和微量元素作为营养来源。生物反硝化已经在城市污水的处理中得到应用。但是，已经在废水处理领域使用的生物反硝化装置，一般都是和生物硝化装置组成一个整体的，这是因为常见城市废水中所含的含氮物质主要是氨，氨首先通过微生物的硝化作用变成亚硝酸和硝酸，然后才通过反硝化作用转化成氮气。这种系统一般氨氮的浓度很低，只有几百个ppm。同时城市废水中一般含有生物反硝化所需要的碳源，不需要另外添加碳源。而且，硝化菌和反硝化菌和其它废水处理的异养菌共生在一起，可以形成稳定的菌胶团絮体结构，使得这些微生物可以在后续的沉淀池中得以分离，并部分回流到生物处理系统中，以确保废水处理系统中的。但是这样的系统对于烟气的脱硝系统所产生的含氮废水的处理就不适合。原因有如下几点：1.烟气脱硝含氮废水不含氨氮，只有硝酸盐和亚硝酸盐；2.废水中没有碳源和其他微量元素可以利用，必须添加碳源和微量元素；3.烟气脱硝含氮废水中含有高浓度的盐，盐的浓度可以达到5-10％；4.所含硝酸根的浓度也比城市废水中的高几十倍甚至上百倍。正如上面所描述，烟气氧化法脱硝技术，会产生一定量的高浓度含硝废水需要处理，而采用蒸发结晶的方法，电耗很高，运行成本大。而现有生物脱氮系统硝化和反硝化联合使用，适合的氮负荷低，不能使用到烟气处理系统中来。因此，急需一种能专门针对氧化法脱硝后产生的含硝废水进行处理且经济适用的装置。
发明内容
本发明主要为氧化法烟气脱硝系统提供一种有效的生物反硝化脱氮处理系统，该系统利用微生物的反硝化作用，将废水中的含氮化合物被还原成N2,从而从废水中除去，一种用于氧化法脱硝的废水脱硝处理系统，其特征在于：包括膜生物反应器、脱气装置和滤液池；所述膜生物反应器设有废水入口、碳源注入口、微量元素注入口、碱液注入口和剩余污泥排放出口；所述膜生物反应器内设有搅拌器、PH探头和膜过滤组件，所述剩余污泥排放出口设置在所述膜过滤组件的后方，所述膜过滤组件与脱气装置通过管道连接，膜过滤组件与脱气装置之间的管道上设有控制阀门，所述脱气装置的上部设有排气阀门，所述脱气装置和 滤液池通过管道连接，脱气装置和滤液池之间管道上设有滤液泵。
进一步的，所述膜生物反应器还设有用于冲刷膜过滤组件的冲洗泵。
进一步的，所述剩余污泥排放出口与膜生物反应器之间的管道上设有剩余污泥排放泵。
进一步的，所述膜过滤组件为平板膜组件或者中空纤维膜组件。
进一步的，所述平板膜组件以平行放置的一组平板膜为基本膜组件单元，每个单元有一套固定平行膜和将它们夹固在一起的衬垫和夹具以及集成的滤液出口组成。
进一步的，所述中空纤维膜组件以一束中空纤维膜为基本单元，每个单元有一套固定中空纤维膜的夹具和将混合液和过滤液分隔的隔板及滤液集液区组成。
一种上述处理系统的应用，其特征在于：所述废水中的NO2和NO3浓度适用范围为1-20g/L，NO2和NO3的摩尔比例范围为0-2之间，盐浓度低于30g/L，pH在7-9。
进一步的，所述废水在膜生物反应器中的定留时间为7-9小时。
本发明的有益效果为：采用本发明，在使用氧化法脱硝进行烟气处理时所产生的废水可以用生物反硝化法来处理，相比采用蒸发结晶法来说，能耗及处理成本大幅度降低。
附图说明
图1是本发明的结构示意图；
其中，1废水入口，2膜生物反应器，3搅拌器，4膜过滤组件，5脱气装置，6滤液泵，7滤液池，8滤清液出口，9剩余污泥排放泵，10剩余污泥排放出口，11冲洗泵，12碳源注入口，13微量元素注入口，14碱液注入口，15控制阀门，16排气阀门。
具体实施方式
以下结合附图对本发明作进一步地说明：第一实施例，一种用于氧化法脱硝的废水脱硝处理系统，包括膜生物反应器2、脱气装置5和滤液池7；所述膜生物反应器2设有废水入口1、碳源注入口12、微量元素注入口13、碱液注入口14和剩余污泥排放出口10；所述膜生物反应器2内设有搅拌器3、PH探头 和膜过滤组件4，还设有用于冲刷膜过滤组件的冲洗泵11，所述剩余污泥排放出口10设置在所述膜过滤组件4的后方，所述膜过滤组件4与脱气装置5通过管道连接，膜过滤组件4与脱气装置5之间的管道上设有控制阀门15，所述脱气装置5的上部设有排气阀门16，所述脱气装置5和滤液池7通过管道连接，脱气装置5和滤液池7之间管道上设有滤液泵6，所述剩余污泥排放出口10与膜生物反应器2之间的管道上设有剩余污泥排放泵9，所述膜过滤组件为平板膜组件，所述平板膜组件以平行放置的一组平板膜为基本膜组件单元，每个单元有一套固定平行膜和将它们夹固在一起的衬垫和夹具以及集成的滤液出口组成。
实际中，本系统处理的废水是有要求的，废水中的NO2和NO3浓度适用范围为1-20g/L，NO2和NO3的摩尔比例范围为0-2之间，盐浓度低于30g/L，pH在7-9，在具体处理废水时，废水在膜生物反应器中的定留时间为7-9小时。
第二实施例，与第一实施例不同之处在于，所述的膜过滤组件为中空纤维膜组件，中空纤维膜组件以一束中空纤维膜为基本单元，每个单元有一套固定中空纤维膜的夹具和将混合液和过滤液分隔的隔板及滤液集液区组成。现有技术中，氧化法烟气脱硝工艺使用氧化剂将废气中的NOx(通常90％或以上为NO)氧化成更高价态的NOx(主要是NO2)，并在后续脱硫洗涤塔中将高价态的NOx洗涤到液态洗涤液中使它们从气相中脱除。这样在洗涤液中就存在高浓度的亚硝酸盐和硝酸盐，因而从洗涤液所分流出去的排放废水也含有这些含氮化合物。由于排放废水的总氮控制，含有这些含氮化合物的废水在排放前必须进行处理。本发明利用微生物的反硝化原理，采用反硝化膜生物反应器技术对该废水进行处理，使得废水中所含的硝酸盐和亚硝酸盐在微生物的作用下被还原成N2，从而使得废水中的含硝化合物被无害化而除去。本发明的膜生物反应器是指在生物反应装置中放置膜过滤系统，使得水和小分子的化合物能透过膜而离开反应器，而微生物及其它悬浮固体能保留在反应器内。由于膜生物反应器不用后续的沉淀分离，这样，可以使得反应池中的微生物浓度远远高于一般的生物反应装置，并且，其负荷也可以比常规的反应池高出很多，反应效率远高于普通反应装置。本发明所应用的废水中的NO2和NO3浓度适用范围为：1-20g/L。其中NO2和NO3的摩尔比例在0-2之间的任何值，废水中所含的总的盐浓度低于30g/L，pH在7-9，反应池中的污泥 浓度为20-38(g/L)。反应所需要的碳源可以由市售乙酸钠，乙醇或甲醇等低分子有机物，或引入一股有机废水，或任何含有挥发性有机酸成分的废液或废料来充当。微量元素也可以由污水厂的废液来充当。废水膜生物反应器内和从碳源排入口及微量元素排入口排入的碳源和微量元素混合，提供生物反应器内的反硝化菌足够的能量及营养成分，废水在反应器中的水力定留时间为8小时，废水中所含的硝酸盐及亚硝酸盐作为反硝化菌能量代谢的电子供体，最终被转化成无害的氮气。反硝化菌利用部分碳源作为营养得到生长。处理后的废水进入膜过滤组件进行过滤，滤液则经过脱气装置被滤液泵抽入滤清液池，并且经排出口排入厂区排水管道。生物膜反应器内增长的微生物菌体必须作为剩余污泥通过剩余污泥排放泵排走，进入脱水装置进行脱水处理。为了使得膜过滤组件的表面获得足够的冲洗，并保持膜表面的清洁，使用冲洗泵对膜组件的膜表面进行水力冲刷。本发明中混合液指的是初始状态进入的废水和从碳源排入口及微量元素排入口排入的碳源和微量元素混合以及调节PH的碱液的混合体，过滤液指的是通过膜过滤组件过滤后的液体。

Claims (8)

  1. 一种用于氧化法脱硝的废水脱硝处理系统，其特征在于：包括膜生物反应器、脱气装置和滤液池；所述膜生物反应器设有废水入口、碳源注入口、微量元素注入口、碱液注入口和剩余污泥排放出口；所述膜生物反应器内设有搅拌器、PH探头和膜过滤组件，所述剩余污泥排放出口设置在所述膜过滤组件的后方，所述膜过滤组件与脱气装置通过管道连接，膜过滤组件与脱气装置之间的管道上设有控制阀门，所述脱气装置的上部设有排气阀门，所述脱气装置和滤液池通过管道连接，脱气装置和滤液池之间管道上设有滤液泵。
  2. 根据权利要求1所述的处理系统，其特征在于：所述膜生物反应器还设有用于冲刷膜过滤组件的冲洗泵。
  3. 根据权利要求1所述的处理系统，其特征在于：所述剩余污泥排放出口与膜生物反应器之间的管道上设有剩余污泥排放泵。
  4. 根据权利要求1所述的处理系统，其特征在于：所述膜过滤组件为平板膜组件或者中空纤维膜组件。
  5. 根据权利要求4所述的处理系统，其特征在于：所述平板膜组件以平行放置的一组平板膜为基本膜组件单元，每个单元有一套固定平行膜和将它们夹固在一起的衬垫和夹具以及集成的滤液出口组成。
  6. 根据权利要求4所述的处理系统，其特征在于：所述中空纤维膜组件以一束中空纤维膜为基本单元，每个单元有一套固定中空纤维膜的夹具和将混合液和过滤液分隔的隔板及滤液集液区组成。
  7. 根据权利要求1-6任一项所述的处理系统的应用，其特征在于：废水中的NO2和NO3浓度适用范围为1-20g/L，NO2和NO3的摩尔比例范围为0-2之间，盐浓度低于30g/L，pH在7-9。
  8. 根据权利要求7所述的处理系统的应用，其特征在于：所述废水在膜生物反应器中的定留时间为7-9小时。
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