CN101234817A - Membrane carrier bubble-free oxygen supply biomembrane reactor and method for treating organic wastewater - Google Patents
Membrane carrier bubble-free oxygen supply biomembrane reactor and method for treating organic wastewater Download PDFInfo
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- 239000012528 membrane Substances 0.000 title claims abstract description 101
- 239000002351 wastewater Substances 0.000 title claims abstract description 52
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 239000001301 oxygen Substances 0.000 title claims abstract description 30
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000012510 hollow fiber Substances 0.000 claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 244000005700 microbiome Species 0.000 claims abstract description 6
- 239000005416 organic matter Substances 0.000 claims description 10
- 239000010410 layer Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 claims description 2
- 230000001054 cortical effect Effects 0.000 claims description 2
- 230000007423 decrease Effects 0.000 claims description 2
- 239000000835 fiber Substances 0.000 claims description 2
- 239000012466 permeate Substances 0.000 claims description 2
- 239000002356 single layer Substances 0.000 claims description 2
- 210000003437 trachea Anatomy 0.000 claims 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims 1
- QRSFFHRCBYCWBS-UHFFFAOYSA-N [O].[O] Chemical compound [O].[O] QRSFFHRCBYCWBS-UHFFFAOYSA-N 0.000 claims 1
- 229910017604 nitric acid Inorganic materials 0.000 claims 1
- 238000001556 precipitation Methods 0.000 claims 1
- 150000003839 salts Chemical class 0.000 claims 1
- 238000005273 aeration Methods 0.000 abstract description 7
- 238000004065 wastewater treatment Methods 0.000 abstract description 6
- 238000012546 transfer Methods 0.000 abstract description 4
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000007787 solid Substances 0.000 description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- WSSSPWUEQFSQQG-UHFFFAOYSA-N 4-methyl-1-pentene Chemical compound CC(C)CC=C WSSSPWUEQFSQQG-UHFFFAOYSA-N 0.000 description 5
- 239000010840 domestic wastewater Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000002209 hydrophobic effect Effects 0.000 description 4
- 239000010815 organic waste Substances 0.000 description 4
- 229920002379 silicone rubber Polymers 0.000 description 4
- 239000004945 silicone rubber Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012982 microporous membrane Substances 0.000 description 3
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- 239000004952 Polyamide Substances 0.000 description 2
- 239000004695 Polyether sulfone Substances 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229920001778 nylon Polymers 0.000 description 2
- 229920002647 polyamide Polymers 0.000 description 2
- 229920006393 polyether sulfone Polymers 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000012855 volatile organic compound Substances 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
Description
技术领域：Technical field:
本发明涉及一种膜载体无泡供氧生物膜反应器及处理有机废水方法，属于废水处理技术。The invention relates to a membrane carrier bubble-free oxygen supply biofilm reactor and a method for treating organic waste water, belonging to waste water treatment technology.
背景技术：Background technique:
膜技术和生物水处理技术的结合产生了三类膜生物反应器，即截留微生物和悬浮固体膜生物反应器(MBR)、无气泡膜曝气生物反应器(MABR)和萃取膜生物反应器(EMBR)。在有机废水处理方面，MBR已经实现商业化，但由于采用的是有泡曝气形式，氧气利用率低，MBR能耗高，使其运行成本高，应用范围受到限制。MABR污水处理技术是针对当前MBR的不足而研发的一种新工艺，该工艺理论上具有氧的传递效率高、所需曝气量少、能同时实现硝化与反硝化、占地面积小、能处理挥发性有机物、能处理难降解有机物以及运行管理方便等特点。The combination of membrane technology and biological water treatment technology has produced three types of membrane bioreactors, namely, the membrane bioreactor (MBR) for retaining microorganisms and suspended solids, the bubble-free membrane aerated bioreactor (MABR) and the extraction membrane bioreactor ( EMBR). In terms of organic wastewater treatment, MBR has been commercialized, but due to the use of bubble aeration, the oxygen utilization rate is low, and the energy consumption of MBR is high, which makes its operation cost high and its application range is limited. MABR sewage treatment technology is a new process developed to address the shortcomings of the current MBR. The process theoretically has high oxygen transfer efficiency, requires less aeration, can realize nitrification and denitrification at the same time, occupies a small area, and can It has the characteristics of processing volatile organic compounds, refractory organic compounds and convenient operation and management.
目前，MABR还处于实验研究阶段，在膜的选择和使用方面，主要以硅橡胶等对称致密中空纤维和疏水微孔中空纤维膜为主。虽然硅橡胶具有良好的透氧能力，但用硅橡胶类材质所制成的对称致密中空纤维壁厚、气体阻力大、比表面积小，机械强度差，且硅橡胶价格昂贵，同样以PMP(聚4-甲基-1-戊烯)制成的对称致密中空纤维的氧气的透过性能并没有提高；疏水微孔膜虽然具有价格便宜和比表面积大的优点，但其物理孔道使其不具备O2/N2选择性，其外表附着的微生物膜极易被空气穿透破坏，另一方面微孔膜的疏水性会因细胞残骸和蛋白质的沉积变成亲水微孔膜，所以疏水微孔膜并不适用于长期的使用。因此，有效避免对称致密膜和疏水微孔膜的主要缺点，提高中空纤维膜的氧气透过能力是未来MABR膜的发展方向。另外，MABR在应用方面还没有形成成熟的工艺模式。本发明就是针对当前MABR的不足而研发的一种新型膜生物膜反应器及处理有机废水的方法。At present, MABR is still in the stage of experimental research. In terms of membrane selection and use, it is mainly based on symmetrical dense hollow fibers such as silicone rubber and hydrophobic microporous hollow fiber membranes. Although silicone rubber has good oxygen permeability, the symmetrical and dense hollow fiber made of silicone rubber has thick wall, large gas resistance, small specific surface area, poor mechanical strength, and expensive silicone rubber. 4-Methyl-1-pentene) The oxygen permeability of the symmetrical dense hollow fiber made of 4-methyl-1-pentene) has not improved; Although the hydrophobic microporous membrane has the advantages of cheap price and large specific surface area, its physical pores make it not available. O 2 /N 2 selectivity, the microbial membrane attached to the surface is easily destroyed by air penetration, on the other hand, the hydrophobicity of the microporous membrane will become hydrophilic due to the deposition of cell debris and protein, so the hydrophobic microporous membrane Porous films are not suitable for long-term use. Therefore, effectively avoiding the main disadvantages of symmetrical dense membranes and hydrophobic microporous membranes, and improving the oxygen permeability of hollow fiber membranes is the development direction of MABR membranes in the future. In addition, MABR has not yet formed a mature process model in terms of application. The present invention is a novel membrane biofilm reactor and a method for treating organic waste water developed for the deficiency of the current MABR.
发明内容：Invention content:
本发明的目的是提供一种膜载体无泡供氧生物膜反应器及其处理有机废水的方法。所述的膜载体无泡供氧生物膜反应器具有氧利用率高，节能的特点，适合于大规模的推广和应用。The purpose of the present invention is to provide a membrane carrier bubble-free oxygen-supplying biofilm reactor and a method for treating organic waste water. The membrane carrier bubble-free oxygen supply biofilm reactor has the characteristics of high oxygen utilization rate and energy saving, and is suitable for large-scale popularization and application.
本发明是通过下述技术方案加以实现的，一种膜载体无泡供氧生物膜反应器，该反应器包括：帘式中空纤维膜组件，所述的帘式中空纤维膜组件由两根连接杆分别连接平行的气体进气管和出气管所构成的矩形框架，其特征在于：在两根平行的气体分配管之间连通帘式布置的透氧中空纤维膜，透氧中空纤维膜膜表面附着着处理废水的生物膜。The present invention is achieved through the following technical scheme, a membrane carrier bubble-free oxygen supply biofilm reactor, the reactor includes: a curtain hollow fiber membrane module, the curtain hollow fiber membrane module is connected by two The rods are respectively connected to the parallel gas inlet pipe and the gas outlet pipe to form a rectangular frame, which is characterized in that: the oxygen-permeable hollow fiber membrane arranged in a curtain is connected between the two parallel gas distribution pipes, and the surface of the oxygen-permeable hollow fiber membrane is attached biofilms in wastewater treatment.
所述的透氧中空纤维膜是指多孔材料支撑的超薄致密皮层中空纤维膜；中空纤维膜的外径在20～5000微米之间，壁厚在1～1000微米之间。The oxygen-permeable hollow fiber membrane refers to an ultra-thin dense cortical hollow fiber membrane supported by a porous material; the outer diameter of the hollow fiber membrane is between 20 and 5000 microns, and the wall thickness is between 1 and 1000 microns.
所述的附着在透氧中空纤维膜膜表面的生物膜的厚度从5到1000微米。The thickness of the biofilm attached to the surface of the oxygen-permeable hollow fiber membrane ranges from 5 to 1000 microns.
所述的帘式中空纤维膜组件的宽度为0.05～10米，高度为0.1～5米，帘式中空纤维膜组件内的纤维可以是单层排列或多层帘式排列。The curtain-type hollow fiber membrane module has a width of 0.05-10 meters and a height of 0.1-5 meters. The fibers in the curtain-type hollow fiber membrane module can be arranged in a single layer or in a multi-layer curtain arrangement.
利用本发明的膜载体无泡供氧生物膜反应器处理有机废水的方法，其特征在于包括以下过程：Utilize the method for the treatment of organic waste water by the membrane carrier of the present invention without bubble oxygen supply biofilm reactor, it is characterized in that comprising following process:
将膜载体无泡供氧生物膜反应器置于废水池中，由进气管端连续通入空气，空气进入透氧中空纤维膜的内腔，在一定的压力下，空气中的氧气透过透氧中空纤维膜的膜壁，剩余的空气由出气管端排出。透过的氧进入透氧中空纤维膜膜外壁的生物膜，靠近透氧中空纤维膜膜外壁的生物层由于能到得到充足的氧气，会形成好氧区，该好氧区能够进行去除含碳有机物和氨氮的反应，远离透氧中空纤维膜膜外壁的生物层，会形成缺氧区，该缺氧区能够进行去除硝酸盐及亚硝酸盐氮的反应。与此同时，经过沉淀后的有机废水以一定流速流经透氧中空纤维膜上附着的生物膜表面，经过透氧中空纤维膜上微生物对有机物的分解，水中有机物含量逐渐降低，当有机物指标达到废水排放要求后，废水通过出水口被排放。Place the membrane carrier bubble-free oxygen-supplying biofilm reactor in the waste water pool, continuously feed air from the inlet pipe end, and the air enters the inner cavity of the oxygen-permeable hollow fiber membrane. Under a certain pressure, the oxygen in the air permeates through the membrane. The membrane wall of the oxygen hollow fiber membrane, and the remaining air is discharged from the end of the air outlet pipe. The permeated oxygen enters the biofilm on the outer wall of the oxygen-permeable hollow fiber membrane, and the biolayer close to the outer wall of the oxygen-permeable hollow fiber membrane will form an aerobic zone because it can get enough oxygen, and the aerobic zone can remove carbon. The reaction of organic matter and ammonia nitrogen, away from the biological layer on the outer wall of the oxygen-permeable hollow fiber membrane, will form an anoxic zone, which can carry out the reaction of removing nitrate and nitrite nitrogen. At the same time, the organic wastewater after sedimentation flows through the surface of the biofilm attached to the oxygen-permeable hollow fiber membrane at a certain flow rate. After the microorganisms on the oxygen-permeable hollow fiber membrane decompose the organic matter, the content of organic matter in the water gradually decreases. When the organic matter index reaches After the waste water discharge is required, the waste water is discharged through the water outlet.
本发明与现有工业膜生物反应器相比，具有如下优点：Compared with existing industrial membrane bioreactors, the present invention has the following advantages:
由于该膜载体无泡供氧生物膜反应器使用的是无泡曝气，氧气直接被附着在透氧中空纤维膜膜表面的微生物所消耗，氧利用率高，所需曝气量少，节能，此外还可以根据调节空气进气压力来调节氧气的传递速度，传递效率易于控制，运行管理方便；由于膜载体无泡供氧生物膜反应器可以在单一处理单元内实现同时含碳有机物和含氮化合物的去除，所以它所需的占地面积小；由于膜载体无泡供氧生物膜反应器采用的是无泡曝气，而且它的供氧能力要比传统的曝气方式强很多，所以它能够处理含挥发性有机物、难降解有机物和高浓度有机物的废水。Since the membrane carrier bubble-free oxygen supply biofilm reactor uses bubble-free aeration, the oxygen is directly consumed by the microorganisms attached to the surface of the oxygen-permeable hollow fiber membrane, the oxygen utilization rate is high, the required aeration is small, and energy saving , in addition, the oxygen transfer rate can be adjusted according to the air intake pressure, the transfer efficiency is easy to control, and the operation and management are convenient; because the membrane carrier has no bubbles, the oxygen-supplying biofilm reactor can realize simultaneous carbon-containing organic matter and carbon-containing biofilm reactor in a single processing unit. The removal of nitrogen compounds, so it requires a small footprint; because the membrane carrier bubble-free oxygen supply biofilm reactor uses bubble-free aeration, and its oxygen supply capacity is much stronger than the traditional aeration method, Therefore, it can treat wastewater containing volatile organic compounds, refractory organic compounds and high-concentration organic compounds.
附图说明Description of drawings
图1为帘式中空纤维膜组件结构示意图；图中：1为挂钩，2为进气管，3为透氧中空纤维膜，4为连接杆，5为出气管。Figure 1 is a schematic diagram of the structure of a curtain-type hollow fiber membrane module; in the figure: 1 is a hook, 2 is an air inlet pipe, 3 is an oxygen-permeable hollow fiber membrane, 4 is a connecting rod, and 5 is an air outlet pipe.
图2为并联的帘式中空纤维膜组件结构示意图Figure 2 is a schematic diagram of the parallel curtain hollow fiber membrane module
图3为串联的帘式中空纤维膜组件结构示意图Figure 3 is a schematic diagram of the structure of the curtain hollow fiber membrane module in series
具体实施方式Detailed ways
实施例1Example 1
对尼龙合成工业废水的处理Treatment of Wastewater from Nylon Synthetic Industry
该废水组成：CODCr为2200mg/L，pH 7.8，悬浮固体为160mg/L，水温30℃。The composition of the wastewater: COD Cr 2200mg/L, pH 7.8, suspended solids 160mg/L, water temperature 30°C.
以本发明膜载体无泡供氧生物膜反应器处理该废水的过程如下：将用聚酰胺致密表层复合聚醚砜多孔中空纤维膜制成的帘式中空纤维膜组件置于废水池中，帘式中空纤维膜组件宽度3米、高度1.5米、每组件上有两层透氧中空纤维膜，如图2，有5个帘式中空纤维膜组件并联排列。将废水引入废水池，然后将能够处理尼龙的活性污泥接种到废水池中，进行生物膜的培养，培养条件为：将空气压缩机压缩的空气引入进气管，调节空气进气压力为0.2MPa，废水以0.2m/h的速度在废水池内流动，经过10天的培养，透氧中空纤维膜的外表面附着上了一层厚度为80微米厚的生物膜。将废水引入废水池中，空气进气压力0.1MPa，废水停留时间5天，经处理后的废水，出水指标为：CODCr为45mg/L，悬浮固体为12mg/L.The process of treating the waste water with the membrane carrier of the present invention is as follows: the curtain-type hollow fiber membrane module made of polyamide dense surface composite polyethersulfone porous hollow fiber membrane is placed in the waste water pool, and the curtain The hollow fiber membrane module has a width of 3 meters and a height of 1.5 meters. Each module has two layers of hollow fiber membranes permeable to oxygen. As shown in Figure 2, there are 5 curtain hollow fiber membrane modules arranged in parallel. The wastewater is introduced into the wastewater tank, and then the activated sludge capable of treating nylon is inoculated into the wastewater tank to cultivate the biofilm. The cultivation conditions are as follows: the air compressed by the air compressor is introduced into the intake pipe, and the air intake pressure is adjusted to 0.2MPa , The waste water flows in the waste water tank at a speed of 0.2m/h. After 10 days of cultivation, a biofilm with a thickness of 80 microns is attached to the outer surface of the oxygen-permeable hollow fiber membrane. The waste water is introduced into the waste water tank, the air intake pressure is 0.1MPa, and the waste water residence time is 5 days. The effluent indicators of the treated waste water are: COD Cr is 45 mg/L, and suspended solids are 12 mg/L.
实施例2Example 2
对生活废水的处理Treatment of Domestic Wastewater
生活废水的组成：CODCr为400-500mg/L，总氮为80mg/L左右，pH为7.2左右，悬浮固体为120mg/L，水温20℃；Composition of domestic wastewater: COD Cr is 400-500mg/L, total nitrogen is about 80mg/L, pH is about 7.2, suspended solids is 120mg/L, water temperature is 20°C;
以图3所示的由聚4-甲基-1-戊烯致密皮层非对称多孔中空纤维膜制成的帘式中空纤维膜组件置于废水池中，该帘式中空纤维膜组件宽度2米、高度1米，每组件上有3层透氧中空纤维膜，对上述废水进行处理，过程如下：The curtain-type hollow fiber membrane module made of poly-4-methyl-1-pentene dense cortex asymmetric porous hollow fiber membrane shown in Figure 3 is placed in the waste water tank, and the width of the curtain-type hollow fiber membrane module is 2 meters , a height of 1 meter, each module has 3 layers of oxygen-permeable hollow fiber membranes, to treat the above wastewater, the process is as follows:
生物膜的培养过程：将该生活废水引入废水池中，将能够处理该生活废水的活性污泥直接接种到废水池中，空气进气压力调整为0.2MPa，废水以0.1m/h的流速在废水池中缓慢流动，经过25天的培养，透氧中空纤维膜的外表面附着上了一层300微米厚的生物膜，此生物膜已经有了明显的分区，靠近透氧中空纤维膜的那部分由于能够得到充足的氧，形成了能够进行含碳有机物和氨氮氧化的好氧区，而相应的生物膜的外层及有机废水本体由于相对缺氧，则形成了能够进行反硝化的缺氧区。Biofilm cultivation process: introduce the domestic wastewater into the wastewater tank, inoculate the activated sludge capable of treating the domestic wastewater directly into the wastewater tank, adjust the air inlet pressure to 0.2MPa, and the wastewater flows at a flow rate of 0.1m/h After 25 days of cultivation, a 300 micron thick biofilm was attached to the outer surface of the oxygen-permeable hollow fiber membrane. Partly due to the availability of sufficient oxygen, an aerobic zone capable of oxidizing carbon-containing organic matter and ammonia nitrogen is formed, while the outer layer of the corresponding biofilm and the organic wastewater body are relatively anoxic, forming an anoxic zone capable of denitrification. district.
废水处理过程：将废水引入反应池中，废水停留时间为2天，根据需要处理的生活废水的浓度变化，来调节空气进入透氧中空纤维膜的压力，进气压力在0.08-0.12MPa之间，出水指标为：CODCr为30mg/L，悬浮固体为8mg/L，总氮为6mg/L。Wastewater treatment process: introduce the wastewater into the reaction tank, the residence time of the wastewater is 2 days, adjust the pressure of the air entering the oxygen-permeable hollow fiber membrane according to the concentration change of the domestic wastewater to be treated, and the inlet pressure is between 0.08-0.12MPa , The effluent indicators are: COD Cr is 30mg/L, suspended solids is 8mg/L, and total nitrogen is 6mg/L.
实施例3Example 3
对含甲苯废水的处理Treatment of wastewater containing toluene
该废水组成：CODCr为4000mg/L，pH为8.1，悬浮固体为230mg/L，水温18℃The wastewater composition: COD Cr 4000mg/L, pH 8.1, suspended solids 230mg/L, water temperature 18°C
以图2所示的用聚酰胺致密表层复合聚醚砜多孔中空纤维膜制成的帘式中空纤维膜组件置于废水反应池中，帘式中空纤维膜组件宽度3米、长度1.5米，每组件上有5层透氧中空纤维膜，对上述废水进行处理，过程如下：The curtain-type hollow fiber membrane module made of polyamide dense surface composite polyethersulfone porous hollow fiber membrane shown in Figure 2 is placed in the wastewater reaction tank. The curtain-type hollow fiber membrane module has a width of 3 meters and a length of 1.5 meters. There are 5 layers of oxygen-permeable hollow fiber membranes on the module to treat the above wastewater, the process is as follows:
生物膜的培养过程：将废水引入废水池，将能够处理该含甲苯废水的特种微生物接种到废水反应池中，调节空气进气压力为0.2MPa，废水以0.2m/h的速度在废水池内流动，经过13天的培养，透氧中空纤维膜的外表面附着上了一层100微米厚的生物膜。Biofilm cultivation process: introduce wastewater into the wastewater tank, inoculate special microorganisms capable of treating the toluene-containing wastewater into the wastewater reaction tank, adjust the air inlet pressure to 0.2MPa, and the wastewater flows in the wastewater tank at a speed of 0.2m/h , after 13 days of cultivation, a 100-micron-thick biofilm was attached to the outer surface of the oxygen-permeable hollow fiber membrane.
废水处理过程：将废水引入废水池中，空气进气压力调节为0.15MPa，废水停留时间4天，经处理后的出水指标为：CODCr为40mg/L，悬浮固体为15mg/L。Wastewater treatment process: Introduce the wastewater into the wastewater tank, adjust the air intake pressure to 0.15MPa, and the residence time of the wastewater is 4 days. The effluent index after treatment is: COD Cr is 40mg/L, and the suspended solid is 15mg/L.
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