CN102515345A - Method for reducing running energy consumption of membrane bioreactor (MBR) - Google Patents
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- 239000012528 membrane Substances 0.000 title claims abstract description 39
- 238000005265 energy consumption Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000005273 aeration Methods 0.000 claims abstract description 85
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 238000005276 aerator Methods 0.000 claims abstract description 7
- 230000007774 longterm Effects 0.000 claims description 3
- 239000010802 sludge Substances 0.000 abstract description 24
- 230000000694 effects Effects 0.000 abstract description 9
- 230000004907 flux Effects 0.000 abstract description 8
- 239000003344 environmental pollutant Substances 0.000 abstract description 6
- 231100000719 pollutant Toxicity 0.000 abstract description 6
- 244000005700 microbiome Species 0.000 abstract description 3
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- 238000010008 shearing Methods 0.000 abstract description 2
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000010865 sewage Substances 0.000 description 13
- 230000008569 process Effects 0.000 description 10
- 238000009285 membrane fouling Methods 0.000 description 8
- 238000001914 filtration Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000000813 microbial effect Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
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- 229910052760 oxygen Inorganic materials 0.000 description 3
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- 230000002427 irreversible effect Effects 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000010841 municipal wastewater Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
Description
技术领域 technical field
本发明涉及一种降低膜生物反应器(MBR)运行能耗的方法，尤其涉及一种采用长低－短高循环曝气，以降低总曝气量，达到降低膜生物反应器运行能耗的方法。 The invention relates to a method for reducing the operating energy consumption of a membrane bioreactor (MBR), in particular to a method of using long low-short high cycle aeration to reduce the total aeration volume and reduce the operating energy consumption of the membrane bioreactor method.
背景技术 Background technique
污水处理虽然处理了污染物，但同时自身又是一个耗能过程，能量消耗是污水处理厂运行的主要成本之一。我国污水处理厂电耗约占污水处理总运行费用的60～90%，现阶段市政污水处理厂平均电耗为0.3 kWh/m3污水，而且为满足日益严格的污水排放标准，运行费用还在增大。MBR是一种膜分离与生物技术相结合的污水处理新工艺，具有占地面积小、剩余污泥量少、出水水质稳定等特点，近年来在工业和市政废水处理、污水再生利用中逐步得到认可。但目前MBR工艺运行能耗相对较高，其处理污水能耗约在0.945 kWh/m3，其中曝气能耗占80%以上，远高出一般污水处理工艺。 Although sewage treatment treats pollutants, it is also an energy-consuming process. Energy consumption is one of the main costs of sewage treatment plant operation. The electricity consumption of China's sewage treatment plants accounts for about 60-90 % of the total operating costs of sewage treatment. increase. MBR is a new sewage treatment process combining membrane separation and biotechnology. It has the characteristics of small footprint, less residual sludge, and stable effluent quality. In recent years, it has gradually been used in industrial and municipal wastewater treatment and sewage recycling. recognized. However, at present, the energy consumption of the MBR process is relatively high, and the energy consumption of its sewage treatment is about 0.945 kWh/m 3 , of which the energy consumption of aeration accounts for more than 80%, which is much higher than that of the general sewage treatment process.
MBR反应器内高浓度活性污泥是MBR处理效率高于普通好氧反应器相的主要原因，为确保反应器内高污泥浓度，需要较长污泥停留时间(SRT)，通常在20~40d。Nitrification and mass balance with a membrane for municipal wastewater treatment. Wat. Sci. Tech., 1996, 34(1-2): 129-136）报导，当SRT从5 d延长到20 d时，污泥浓度从3.0 g/L增加到7.5 g/L。然而SRT越长，高的污泥浓度使污泥粘度增加，从而加重膜污染(Treatment of domestic sewage from rural settlements by a membrane bioreactor. Wat. Sci. Tech., 1996, 34(9): 189-196)；其次，SRT延长，还导致混合液中微生物代谢产物－胞外聚合物(EPS)含量增加，同时使得多糖含量相应也增多，导致污泥沉降性能下降(污泥龄对膜生物反应器污泥特性及膜污染的影响. 中国环境科学, 2009, 29(4): 384-390. Surface properties of sludge and the role in bioflocculation and settleability. Wat. Res., 2001, 35(2): 339-350)，一定程度上加剧了膜污染。MBR反应器为缓解膜污染速率，通常采用增大曝气量方式，增大曝气量为膜面创造湍流，产生冲击作用擦洗膜表面，清除污泥颗粒，减少膜面沉积物形成使膜结垢最小化。上述原因使得MBR反应器运行，通常采用连续高强曝气，气水体积比通常在40～60：1，明显高于普通活性污泥处理工艺(气水比通常在10-20：1)。连续高强曝气(40～60：1)，不仅造成运行能耗较高，而且还会产生负面作用，例如曝气量大会破坏絮体结构，减小絮体尺寸并使EPS释放到生物反应器中，使混合液中细小污泥颗粒增多，从而导致膜孔堵塞。 The high concentration of activated sludge in the MBR reactor is the main reason why the treatment efficiency of the MBR is higher than that of the ordinary aerobic reactor phase. In order to ensure the high sludge concentration in the reactor, a longer sludge residence time (SRT) is required, usually between 20~ 40d. Nitrification and mass balance with a membrane for municipal wastewater treatment. Wat. Sci. Tech., 1996, 34(1-2): 129-136) reported that when the SRT was extended from 5 d to 20 d, the sludge concentration increased from 3.0 g/L increased to 7.5 g/L. However, the longer the SRT, the higher the sludge concentration will increase the viscosity of the sludge, which will aggravate the membrane fouling (Treatment of domestic sewage from rural settlements by a membrane bioreactor. Wat. Sci. Tech., 1996, 34(9): 189-196 ); secondly, the prolongation of SRT also leads to the increase of microbial metabolite-extracellular polymer (EPS) content in the mixed solution, and the corresponding increase of polysaccharide content, which leads to the decrease of sludge settling performance (the effect of sludge age on membrane bioreactor sewage Effects of sludge properties and membrane fouling. Chinese Environmental Science, 2009, 29(4): 384-390. Surface properties of sludge and the role in bioflocculation and settleability. Wat. Res., 2001, 35(2): 339-350 ), aggravated the membrane fouling to some extent. In order to alleviate the membrane fouling rate, the MBR reactor usually adopts the method of increasing the aeration rate, which creates turbulence on the membrane surface, produces impact action to scrub the membrane surface, removes sludge particles, and reduces the formation of sediment on the membrane surface to make the membrane clump. Scale is minimized. The above reasons make the operation of the MBR reactor usually adopt continuous high-intensity aeration, and the air-water volume ratio is usually 40-60:1, which is significantly higher than that of ordinary activated sludge treatment process (the air-water ratio is usually 10-20:1). Continuous high-intensity aeration (40-60:1) not only results in higher operating energy consumption, but also has negative effects, such as large aeration volume destroying the floc structure, reducing the floc size and releasing EPS into the bioreactor In the middle, the fine sludge particles in the mixed solution increase, which leads to the clogging of the membrane pores.
其次，通常MBR采用微孔曝气，而微孔曝气主要缺点是曝气器膜片阻力大，心及微孔容易堵塞，此也是MBR工艺曝气能耗高的另一原因。 Secondly, MBR usually uses microporous aeration, and the main disadvantage of microporous aeration is that the diaphragm of the aerator has high resistance, and the core and micropores are easily blocked. This is another reason for the high energy consumption of aeration in the MBR process.
发明内容 Contents of the invention
本发明目的在于克服上述现有技术的不足，提供一种不影响出水水质和膜污染，而使曝气能耗有明显下降，从而节约运行能耗的降低膜生物反应器运行能耗的方法。 The purpose of the present invention is to overcome the deficiencies of the above-mentioned prior art and provide a method for reducing the operating energy consumption of a membrane bioreactor that does not affect the effluent water quality and membrane fouling, but significantly reduces the energy consumption of aeration, thereby saving the energy consumption of the operation.
本发明目的实现，主要改进：一是将现有连续高强度曝气改为长时低－短时超高波动循环曝气，以在保证不增加膜污染提前下，降低总曝气量；二是将现有微孔曝气改为穿孔曝气，以降低曝气阻力，二者共同作用降低运行曝气能耗，从而克服现有技术的不足，实现本发明目的。具体说，本发明降低膜生物反应器运行能耗的方法，其特征在于MBR运行曝气采用穿孔曝气器，对膜组件曝气分为8-12 min长时间低强度曝气，和1-2 min短时间超高强度曝气，低强度曝气气水比20-30：1，超高强度曝气气水比60-80：1。 The purpose of the present invention is achieved, and the main improvements are as follows: first, the existing continuous high-intensity aeration is changed to long-time low-short-time ultra-high fluctuation cycle aeration, so as to reduce the total aeration volume without increasing membrane fouling; The method is to change the existing microporous aeration into perforated aeration to reduce aeration resistance, and the two work together to reduce the energy consumption of aeration during operation, so as to overcome the deficiencies of the prior art and achieve the purpose of the present invention. Specifically, the method for reducing the energy consumption of a membrane bioreactor in the present invention is characterized in that the aeration of the MBR operation adopts a perforated aerator, and the aeration of the membrane module is divided into 8-12 min long-term low-intensity aeration, and 1- 2 minutes short-term ultra-high-intensity aeration, low-intensity aeration air-water ratio 20-30:1, ultra-high-intensity aeration air-water ratio 60-80:1.
在详细说明前，先通过对发明能够达到的基本功能及效果作一介绍，以使本领域技术人员对本专利总体构思技术方案及达到的基本技术效果有一个明确了解。 Before explaining in detail, an introduction to the basic functions and effects that can be achieved by the invention is given first, so that those skilled in the art can have a clear understanding of the general technical scheme of the patent and the basic technical effects achieved.
申请人对现有MBR运行经大量测试、试验表明：MBR工艺中曝气量增加，并不会正比提高膜通量，在通常曝气量下适当降低曝气量(气水比)并不会影响出水水质和膜通量。现有持续高强度曝气，有相当一部分是消耗在膜表面形成较大错流速度，达到减少污染物在膜表面积累，以及加快污染物在膜表面的脱落，用于生物反应部分曝气量略高于普通活性污泥法即可，例如气水比20-30：1。即持续高气水比主要目的是用于对膜的冲刷，降低膜污染，这是造成MBR曝气能耗高的主要原因。本发明采用MBR运行时曝气里较常规MBR降低，正常曝气时曝气气水比设定为20-30：1，已经能够满足生物反应所需要氧量，不会影响微生物正常生长对氧需求，间歇提高曝气量，超高强度曝气时曝气气水比为60-80：1，造成短时间较常规MBR更高的曝气强度，通过间隙短时高强曝气对膜表面冲刷，同样可以缓解膜面污染。即膜生物反应器运行中，连续曝气量较常规降低，间歇采用提高曝气强度运行，较现有技术全部采用中高强持续曝气(40～60：1)，减少了运行总曝气量，从而使得运行能耗有相对降低。其次，穿孔曝气阻力相对较小，相同曝气量风压可降低3-5kPa。两者相加，在不增加膜污染程度情况下，可以节约运行能耗约5－8%。 The applicant has performed a large number of tests on the existing MBR operation, and the experiments show that the increase of the aeration rate in the MBR process will not increase the membrane flux in direct proportion, and the appropriate reduction of the aeration rate (air-water ratio) under the usual aeration rate will not cause the Affect effluent water quality and membrane flux. In the existing continuous high-intensity aeration, a considerable part of it is consumed on the surface of the membrane to form a large cross-flow velocity, so as to reduce the accumulation of pollutants on the surface of the membrane and accelerate the shedding of pollutants on the surface of the membrane, which is used for part of the aeration volume of the biological reaction Slightly higher than the ordinary activated sludge method, for example, the air-water ratio is 20-30:1. That is to say, the main purpose of continuously high air-water ratio is to scour the membrane and reduce membrane fouling, which is the main reason for the high energy consumption of MBR aeration. In the present invention, when the MBR is used, the aeration rate is lower than that of the conventional MBR, and the aeration gas-water ratio is set to 20-30:1 during normal aeration, which can already meet the oxygen required by the biological reaction and will not affect the normal growth of microorganisms on oxygen. Demand, increase the aeration volume intermittently, the aeration air-water ratio is 60-80:1 during ultra-high-intensity aeration, resulting in a higher aeration intensity than conventional MBR in a short period of time, and the membrane surface is washed by short-term high-intensity aeration through the gap , can also alleviate membrane surface fouling. That is to say, during the operation of the membrane bioreactor, the continuous aeration rate is lower than the conventional one, and the aeration intensity is increased intermittently. Compared with the existing technology, medium and high-intensity continuous aeration (40-60:1) is used to reduce the total operating aeration rate , so that the operating energy consumption is relatively reduced. Secondly, the perforated aeration resistance is relatively small, and the wind pressure can be reduced by 3-5kPa for the same aeration volume. The addition of the two can save about 5-8% of the operating energy consumption without increasing the degree of membrane pollution.
本发明中：对膜组件曝气，采用长时低强度－短时超高强度循环，区别于现有技术采用持续高强度曝气，低强度曝气满足微生物生长所需空气量，维持微生物生长；超高强度曝气对膜面进行冲刷，以缓解膜污染。 In the present invention: the aeration of the membrane module adopts a long-time low-intensity-short-time ultra-high-intensity cycle, which is different from the prior art in which continuous high-intensity aeration is used, and low-intensity aeration meets the air volume required for microbial growth and maintains microbial growth ; Ultra-high-intensity aeration scours the membrane surface to alleviate membrane fouling.
本发明较现有MBR工艺，除曝气方式及曝气气水比，以及曝气器形式与现有MBR工艺不同外，其余均同现有技术，例如MBR工艺控制等等，就不一一另行叙述，此对本领域技术人员是清楚的。 Compared with the existing MBR process, the present invention is different from the existing MBR process except that the aeration mode, the aeration gas-water ratio, and the form of the aerator are different from the existing MBR process. It will be clear to those skilled in the art that it will be described separately.
本发明降低膜生物反应器运行能耗的方法，相对于现有技术，由于降低MBR反应器正常运行的气水比，使正常气水比由现有的40～60：1降低到20-30：1，满足MBR正常运行微生物对氧气的需要；间歇短时加大曝气强度，采用超高强度曝气(60-80：1)，形成对膜生物反应器膜面的间歇短时高强冲刷，在不影响出水水质和膜通量的前提下降低了曝气总能耗；同时采用穿孔曝气，也使得曝气阻力得以下降，从而降低了运行成本，综合运行能耗可以降低约5－8%。其次，由于长时间正常曝气气量有所降低，也减轻了对污泥剪切作用，提了高微生物活性，改善污泥沉降性能，提高污染物去除效率。在进水COD 250-350 mg/L，NH3-N 25-30 mg/L试验水质，污泥停留时间10~40 d，pH值为6.8~7.2，温度为24~28℃，采用恒通量操作模式，膜通量为18 L/（m2·h）运行条件下，8-12 min20-30：1气水比，1-2 min60-80：1气水比循环，COD去除率为94%~96%，跨膜压差(TMP)增速为0.69~2.20 kPa/d。 Compared with the prior art, the method for reducing the energy consumption of membrane bioreactor operation in the present invention reduces the normal gas-water ratio from the existing 40-60:1 to 20-30 due to the reduction of the gas-water ratio in the normal operation of the MBR reactor. : 1, to meet the needs of microorganisms for oxygen in the normal operation of the MBR; intermittently increase the aeration intensity for a short time, and use ultra-high-intensity aeration (60-80: 1) to form intermittent short-term high-intensity scouring of the membrane surface of the membrane bioreactor , without affecting the effluent water quality and membrane flux, the total energy consumption of aeration is reduced; at the same time, the use of perforated aeration also reduces the aeration resistance, thereby reducing the operating cost, and the comprehensive operating energy consumption can be reduced by about 5- 8%. Secondly, due to the long-term normal aeration air volume has been reduced, it also reduces the shearing effect on sludge, improves microbial activity, improves sludge settling performance, and improves pollutant removal efficiency. In the influent COD 250-350 mg/L, NH3-N 25-30 mg/L test water quality, sludge residence time 10-40 days, pH value 6.8-7.2, temperature 24-28 ℃, constant flux operation Mode, under the operating condition of membrane flux of 18 L/(m2 h), 8-12 min20-30:1 air-water ratio, 1-2 min60-80:1 air-water ratio cycle, COD removal rate is 94%~ 96%, and the growth rate of transmembrane pressure (TMP) was 0.69~2.20 kPa/d.
以下结合若干个具体实施例，示例性说明及帮助进一步理解本发明实质，但实施例具体细节仅是为了说明本发明，并不代表本发明构思下全部技术方案，因此不应理解为对本发明总的技术方案限定，一些在技术人员看来，不偏离本发明构思的非实质性增加和/或改动，例如以具有相同或相似技术效果的技术特征简单改变或替换，均属本发明保护范围。 Below in conjunction with several specific embodiments, illustrate and help to further understand the essence of the present invention, but the specific details of the embodiments are only to illustrate the present invention, and do not represent all technical solutions under the concept of the present invention, so it should not be interpreted as a summary of the present invention. In the eyes of a skilled person, some non-essential additions and/or changes that do not deviate from the concept of the present invention, such as simple changes or replacements with technical features having the same or similar technical effects, all fall within the protection scope of the present invention.
具体实施方式 Detailed ways
实施例1：试验某污水处理厂原水，COD 260mg/L，NH3-N 27 mg/L。膜生物反应器的SRT为15 d，pH值为6.8，温度为24℃。反应器采用穿孔管曝气器，恒通量操作模式，膜通量为18 L/(m2·h)，出水泵的抽停比为10 min：2 min。正常低强度曝气时间和超高强度曝气时间分别为10 min和2 min，正常低强度曝气气水比为30:1，超高强度曝气气水比为60：1。运行10 d后，COD去除率为97.2%，NH3-N去除率为96.3%；污泥浓度为6.02 g/L，污泥颗粒体积平均粒径为158 μm，LB- EPS含量为2.26mg/(g·VSS)；过滤总阻力为5.33×1012 1/m，可逆滤阻为1.16×1012 1/m，不可逆滤阻为0.87×1012 1/m；TMP平均增长速率为1.69kPa/d，运行平均能耗0.892 kWh/m3。 Example 1: Test the raw water of a sewage treatment plant, COD 260mg/L, NH 3 -N 27 mg/L. The SRT of the membrane bioreactor is 15 days, the pH value is 6.8, and the temperature is 24 °C. The reactor adopts perforated tube aerator, constant flux operation mode, the membrane flux is 18 L/(m 2 ·h), and the pump-stop ratio of the outlet pump is 10 min:2 min. The normal low-intensity aeration time and ultra-high-intensity aeration time were 10 min and 2 min, respectively, the air-water ratio of normal low-intensity aeration was 30:1, and the air-water ratio of ultra-high-intensity aeration was 60:1. After running for 10 days, the removal rate of COD was 97.2%, and the removal rate of NH 3 -N was 96.3%; the sludge concentration was 6.02 g/L, the average particle size of sludge particles was 158 μm, and the content of LB-EPS was 2.26mg/ (g·VSS); the total filtration resistance is 5.33×10 12 1/m, the reversible filtration resistance is 1.16×10 12 1/m, and the irreversible filtration resistance is 0.87×10 12 1/m; the average growth rate of TMP is 1.69kPa/ d, the average running energy consumption is 0.892 kWh/m 3 .
实施例2：例1污水及运行条件，其中不同为正常低强度曝气气水比为20:1，超高强度曝气气水比为70：1。运行10 d后，COD去除率为97%，NH3-N去除率为96%；污泥浓度为6.36 g/L，污泥颗粒体积平均粒径为162 μm，LB- EPS含量为2.28mg/(g·VSS)；过滤总阻力为5.36×1012 1/m，可逆滤阻为1.18×1012 1/m，不可逆滤阻为0.93×1012 1/m；TMP平均增长速率为1.76kPa/d，运行平均能耗0.885 kWh/m3。 Example 2: Example 1 sewage and operating conditions, where the difference is that the ratio of air to water for normal low-intensity aeration is 20:1, and the ratio of air to water for ultra-high-intensity aeration is 70:1. After 10 days of operation, the removal rate of COD was 97%, and the removal rate of NH 3 -N was 96%; the sludge concentration was 6.36 g/L, the average particle size of sludge particles was 162 μm, and the content of LB-EPS was 2.28mg/ (g·VSS); the total filtration resistance is 5.36×10 12 1/m, the reversible filtration resistance is 1.18×10 12 1/m, and the irreversible filtration resistance is 0.93×10 12 1/m; the average growth rate of TMP is 1.76kPa/ d, the average energy consumption in operation is 0.885 kWh/m 3 .
比较例：例1污水，处理条件基本相同，不同为采用膜片式微孔曝气器，连续高强度曝气方式，曝气气水比为50：1，运行10 d后，COD去除率97.3%，NH3-N去除率96.5%；TMP平均增长速率1.56kPa/d，运行平均能耗0.950kWh/m3。同时也表明采用本发明方式曝气，对污染物去除率没有太大影响。 Comparative example: Example 1 sewage, the treatment conditions are basically the same, the difference is that the diaphragm microporous aerator is used, the continuous high-intensity aeration method, the aeration gas water ratio is 50:1, and the COD removal rate is 97.3 after 10 days of operation. %, NH 3 -N removal rate is 96.5%; the average growth rate of TMP is 1.56kPa/d, and the average operating energy consumption is 0.950kWh/m 3 . Simultaneously, it also shows that the aeration by the method of the present invention has no great influence on the removal rate of pollutants.
对于本领域技术人员来说，在本专利构思及具体实施例启示下，能够从本专利公开内容及常识直接导出或联想到的一些变形，本领域普通技术人员将意识到也可采用其他方法，或现有技术中常用公知技术的替代，以及特征的等效变化或修饰，特征间的相互不同组合，例如曝气气水比在本发明给出的范围内波动，等等的非实质性改动，同样可以被应用，都能实现本专利描述功能和效果，不再一一举例展开细说，均属于本专利保护范围。 For those skilled in the art, under the inspiration of the patent concept and specific embodiments, some deformations that can be directly derived or associated from the patent disclosure and common sense, those of ordinary skill in the art will realize that other methods can also be used, Or the replacement of commonly known technologies in the prior art, as well as equivalent changes or modifications of features, different combinations of features, such as fluctuations in the ratio of aeration gas to water within the range given by the present invention, etc. Insubstantial changes , can also be applied, and can all realize the functions and effects described in this patent, and will not give examples one by one to elaborate, all of which belong to the protection scope of this patent.
本发明所说低、高，超高强度曝气，在本发明中分别指曝气气水比为20-30：1，40～60：1(现有工艺采用)和60-80：1。 The low, high, and ultra-high intensity aeration mentioned in the present invention refer to the aeration gas-water ratios of 20-30:1, 40-60:1 (used in existing technology) and 60-80:1 respectively in the present invention.
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