CN101549907A - Membrane biologic reaction equipment and processing method for processing industrial waste water with high ammoniac nitrogen - Google Patents

Abstract

The invention provides membrane biologic reaction equipment and a processing method for processing industrial waste water with high ammoniac nitrogen. In the processing equipment, an anaerobic water outlet pool (100), an oxygen-poor pool (2), a first-section aerobian pool (3), a second-section aerobian pool (4) and a membrane pool (5) are connected according to the circulation sequence of fluid, wherein immersion type unitization hollow fibre membrane filtration equipment is arranged in the membrane pool for carrying out solid and liquid separation of processing liquid. The equipment adopts a control mode combining manual control and automatic control, and the operation and the maintenance are simple. A biochemical system has a flexible running mode with adjustable oxygen-poor and aerobian time, adjustable dirt return quantity, adjustable return modes, and the like so as to adapt to the change condition of the produced waste water and ensure high processing efficiency.

Description

Membrane bioreaction equipment and treatment method for high ammonia nitrogen industrial wastewater treatment

technical field

The invention relates to a membrane bioreactor and a treatment method, in particular to a membrane bioreactor and a treatment method for high ammonia nitrogen industrial wastewater treatment.

Background technique

Ammonia nitrogen and COD (Chemical oxygen demand, Chemical oxygen demand) are the two most important indicators of sewage discharge, and are also important indicators to measure the effect of sewage treatment and whether it can be reused. In most reuse standards and discharge standards, these two The indicators are strictly regulated. MSG and fermentation industry wastewater is characterized by high ammonia nitrogen and high COD. The current treatment method is mainly based on activated sludge method, including the following processes, (1) A2/O (anaerobic + anoxic + aerobic) method, (2) A+SBR (anaerobic+sequenced batch activated sludge method), (3) A+O+delayed aeration method, the biggest disadvantage of these methods is that they occupy too much area and are easy to Due to the impact of production, the treatment effect is unstable, the energy consumption is high, and it is difficult to directly recycle. Therefore, the monosodium glutamate and starch industry is also one of the most polluting industries, and the industry is under key control and restriction by the state.

With the aggravation of my country's water resource shortage, many companies hope to reuse this kind of wastewater after treatment. The main processes used are advanced treatment processes such as flocculation, sand filtration, membrane filtration, and desalination after biochemical treatment. , a large amount of chemicals are used in the advanced treatment process, the operating cost is high, the process route is complicated, and it is easily affected by the fluctuation of the previous biochemical treatment. Moreover, due to the low removal rate of ammonia nitrogen in biochemical treatment, the high concentration of ammonia nitrogen in RO produced water will affect further reuse, and the concentrated water often contains high concentration of ammonia nitrogen and cannot be discharged directly, which brings hidden troubles to sewage reuse.

Membrane bioreactor technology is a technology that combines biochemistry and membrane technology. Since this process does not require a secondary sedimentation tank to save land, the high-efficiency interception effect of the membrane on nitrifying bacteria makes it have obvious advantages in removing ammonia nitrogen. At present, the membrane bioreactor The combination of (MBR) and the traditional process has the following processes: A+MBR (anoxic + MBR), A+SMBR process, etc. These processes have a better treatment effect on domestic wastewater or industrial wastewater with a low ammonia nitrogen content, but the effect on production wastewater with a high concentration and large fluctuations such as 300-700mg/L ammonia nitrogen content is often not significant, and the energy consumption is high. Nitrate accumulation and other problems.

Contents of the invention

Aiming at the deficiencies of the prior art, the technical problem to be solved by the present invention is to propose a combined process and equipment for anaerobic, anoxic, staged aerobic and membrane separation.

The present invention provides a kind of membrane bioreaction equipment for the treatment of high ammonia nitrogen industrial wastewater, which is characterized in that it comprises: an anaerobic effluent pool, an anoxic pool, a first-stage aerobic pool, a second-stage aerobic pool, Membrane pool, wherein, the anaerobic effluent pool is used to store anaerobic effluent and play the role of regulation and water supply; an anoxic pool is provided downstream of the anaerobic effluent pool, and the above-mentioned anoxic pool denitrifies organic matter in the water; the anoxic pool A section of aerobic pool is arranged downstream of the first section of aerobic pool, and the above-mentioned section of aerobic pool is used for nitrosation and nitrification of ammonia nitrogen; downstream of the first section of aerobic pool, there is a second section of aerobic pool, which treats part of the unnitrated ammonia nitrogen and part of nitrous oxide in the first section of aerobic pool. The nitrate is fully oxidized; the end of the second-stage aerobic tank is connected to the membrane tank, and the membrane tank is equipped with a submerged unitized hollow fiber membrane filtration device to separate the solid and liquid of the treatment liquid.

In addition, the anaerobic effluent pool is liquid-connected with the anoxic pool through pipelines, and the waste water is lifted to the grid well through the centrifugal pump, and then enters the anoxic pool through the fine grid arranged in the grid well.

In addition, the bottom of the anoxic tank is connected to the bottom of the first-stage aerobic tank and the second-stage aerobic tank. The liquid overflows from the second-stage aerobic tank to the membrane tank, and the sludge passes through the sludge return pump and the second-stage aerobic tank respectively. The sludge return pump installed at the bottom of the membrane pool returns from the aerobic pool and the membrane pool to the anoxic pool.

In addition, a stirring device and microporous aeration tubes are installed in a section of the aerobic pool. The microporous aeration tubes are installed in groups, and the number of microporous aeration tubes can be changed according to the water quality to adjust the anoxic/aerobic time.

In addition, a blower is also provided for oxygen supply. The fan is connected to the first aerobic pool through the air supply valve of the first aerobic pool, connected to the second aerobic pool through the valve of the second aerobic pool, and connected to the second aerobic pool through the air supply valve of the membrane pool. The membrane pools are connected, and when the dissolved oxygen is low, it can be adjusted through the above-mentioned first-stage aerobic pool air supply valve, second-stage aerobic pool valve, and membrane pool air supply valve.

The present invention also provides a membrane bioreaction method for treating high-ammonia-nitrogen industrial wastewater, which is characterized in that: high-ammonia-nitrogen industrial wastewater first undergoes anaerobic treatment, anaerobically decomposes macromolecular refractory organic matter into small molecular organic matter, and then enters the pool Supply water for the subsequent process; then enter the anoxic stage of the anoxic pool, denitrify the nitrate nitrogen and nitrite nitrogen produced in the aerobic process into nitrogen to achieve denitrification; then enter the aerobic pool for a section Aerobic, control the dissolved oxygen in a lower range, convert ammonia nitrogen into nitrite nitrogen and then carry out a reflux to realize the short-range nitrification process of nitrosation-denitrification, and the remaining nitrite and ammonia nitrogen will then enter the second-stage aerobic pool for secondary aerobic and converted into nitrate nitrogen; finally, the second-stage sludge reflux is carried out in the membrane separation tank at the end of the system, and the mixed solution containing nitrate nitrogen is returned to the anoxic tank for further denitrification into nitrogen.

In addition, the membrane filtration adopts the method of opening for 8-12 minutes and stopping for 1-3 minutes, that is, the membrane system produces water for 8-12 minutes and stops water production for 1-3 minutes; the membrane tank is equipped with perforated aeration for membrane filament shaking The aeration tube and the aeration tube are in the normal open state. When the membrane module does not produce water, it is in an empty aeration state, so that the activated sludge deposited on the membrane surface is blown off, the membrane surface pollution is slowed down, and the membrane flux is relatively stable.

The equipment provided by the present invention includes biochemical equipment and hollow fiber membrane filtration equipment. The system adopts a manual and automatic control mode, and the operation and maintenance are simple. The biochemical system has flexible operation modes such as adjustable anoxic and aerobic time, adjustable sludge return flow rate and return mode, so as to adapt to the fluctuation of production wastewater and ensure high treatment efficiency.

Compared with existing wastewater treatment equipment and treatment methods, the present invention has the following advantages:

(1), the present invention is provided with two-stage aerobic and two-stage sludge reflux, realizes the organic combination of short-range nitrification and denitrification, nitrification and denitrification, and this technique is very applicable to high ammonia nitrogen wastewater and high COD wastewater, and this technique produces Water can greatly reduce COD and ammonia nitrogen and has a high denitrification effect.

(2) The aerobic residence time and anoxic residence time can be adjusted to adapt to the change of influent water quality.

(3) The interception effect of the membrane can make the suspended solids in the effluent close to zero, and the effluent of the system can meet the first-level discharge standard, and can also be directly reused or desalinated by reverse osmosis to produce high-quality process reuse water.

(3) The system saves alkalinity and reduces energy consumption.

The equipment and method proposed by the present invention can be applied to the advanced treatment and reuse of production wastewater in monosodium glutamate and fermentation industries. The production wastewater in these industries is characterized by high COD (organic matter) and high ammonia nitrogen. This method can reduce COD to 80mg/L Below, the ammonia nitrogen is reduced to below 15mg/L, and the removal efficiency reaches more than 95%, and the treatment effect is very remarkable.

The invention overcomes the deficiencies of the prior art, and has good effluent quality and strong impact resistance. Under the background of increasingly strict national discharge standards and widespread promotion of sewage reuse, the process described in the invention can meet the requirements of enterprises for advanced sewage treatment.

Description of drawings

Fig. 1 is a schematic diagram of the structure of the membrane reactor proposed by the present invention.

Detailed ways

In general, the technical solution of the present invention is to design a biochemical and membrane separation multi-stage combined integrated system equipment, the combined treatment process includes anaerobic + anoxic + one-stage aerobic + two-stage aerobic + submerged membrane filtration, etc. In a multi-stage process, the sludge return flows from the aerobic and membrane tanks to the anoxic tank respectively. The effects of each process on the biochemical degradation of organic matter and ammonia nitrogen are as follows: anaerobic decomposition of macromolecular refractory organic matter into small molecular organic matter, and most of the products are methane, which can be separated from the bulk solution, and COD can be reduced from 4000-5000mg/L to 2000mg/L Below L, then enters the anoxic stage, where the nitrate nitrogen and nitrite nitrogen produced in the subsequent aerobic process can be denitrified into nitrogen to achieve denitrification. Aerobic is divided into two stages, one aerobic control of dissolved oxygen in a lower range, so that ammonia nitrogen is converted into nitrite nitrogen, and then a reflux is carried out to realize the short-range nitrification process of nitrosation-denitrification, and the remaining nitrite and ammonia nitrogen are subsequently In the second-stage aerobic process, it is transformed into nitrate nitrogen, so as to avoid the accumulation of a large amount of nitrite and affect the quality of effluent water. In the membrane separation tank at the end of the system, the second-stage sludge return is carried out, and the mixed solution containing nitrate nitrogen is returned to the anoxic tank for further denitrification into nitrogen. A part of the alkalinity can be produced in the process to supplement the alkalinity consumed in the subsequent nitrification process, and a part of the carbon source (COD) is also consumed in the denitrification process, which reduces the burden of degrading COD for the subsequent aerobic process. The above-mentioned membrane filtration process adopts immersion type, unit grouping control mode, continuous water production, and intermittent membrane operation. To prevent membrane fouling, aeration, backwashing, chemical backwashing, off-line cleaning and other cleaning methods can be selected to adapt to different pollution levels.

Below, the specific implementation process route of the present invention is described in detail as follows:

For example, waste liquid (high ammonia nitrogen, high COD) such as monosodium glutamate production comprehensive wastewater is treated as follows:

The wastewater goes through the anaerobic stage, the anoxic stage, the first aerobic stage, the second aerobic stage, the membrane tank treatment stage, and finally produces water.

Among them, the anaerobic section is a conventional UASB process, which can reduce the COD of wastewater from 4000-5000mg/L to less than 2000mg/L, but when the production is impacted, the COD of the effluent can also reach more than 2000mg/L, and the ammonia nitrogen is 200-700mg /L, the concentration of ammonia nitrogen in the effluent at this stage is slightly higher than that in the influent.

Anoxic section: two channels (that is, two water channels in series separated by a partition wall), each equipped with 2 submersible mixers, used to mix the influent and return sludge mixture, and the second channel is installed There are microporous aeration devices and submersible mixers, which can be adjusted according to the quality of incoming water. It can be used as both an aerobic section and an anoxic section. When the COD of the incoming water is lower than 1000mg/L and the ammonia nitrogen content is higher than 400mg/L The microporous aeration can be closed, and the submersible mixer can be turned on. At this time, the two grids are all used as anoxic sections. When the influent COD is higher than 1000mg/L and the ammonia nitrogen is low at 400mg/L, microporous aeration can be turned on as an aerobic stage. In this way, the hypoxia and aerobic time can be changed more flexibly. The hypoxic time can be adjusted between 7 and 14 hours.

A period of aerobic, control the dissolved oxygen to make it in the aerobic stage of low dissolved oxygen, the dissolved oxygen can be in the range of 0.5-1.5mg/L, most of the ammonia nitrogen is converted into nitrite at this stage, and a small part is converted into nitrate, At the aerobic end, there is a sludge return pump to return the nitrite solution to the anoxic tank to realize short-range nitrification-denitrification nitrogen removal. This process not only saves aeration and reduces energy consumption, but also generates part of alkalinity to supplement aerobic Alkalinity consumption of the process. An aerobic period can be controlled within 10 to 20 hours. The sludge return ratio can be adjusted between 50% and 100%.

The second stage is aerobic. At this stage, the remaining ammonia nitrogen and part of the nitrite nitrogen are fully oxidized to avoid excessive nitrite in the effluent from affecting the COD value of the effluent. At this stage, the remaining dissolved oxygen should be controlled at 1.5-2.5mg/L. Too low will affect the nitrification reaction, too high will lead to large gas volume and high energy consumption. Adjust the residence time between 15 and 20 hours, and monitor the pH of the solution at this stage. When the pH is lower than 7.0, add alkali to adjust the pH so that the nitration reaction can proceed normally.

After the second aerobic stage, a submerged membrane filtration device is installed to achieve solid-liquid separation. There is a sludge return device at the end of the membrane pool to transport the high-concentration mud-water mixture to the anoxic section. The effect of this treatment is to balance the entire biochemical pool. Second, because the mixed solution contains nitrate after complete nitrification of ammonia nitrogen, denitrification and nitrogen removal can be realized in the anoxic tank after reflux, and the alkalinity generated at the same time supplements the alkalinity consumed by the aerobic nitrification reaction. The sludge reflux ratio can be adjusted between 100% and 200%.

The membrane separation system of the present invention adopts a submerged hollow fiber membrane filtration method, and the system includes a membrane module, a water production system, a backwashing dosing system, a control system, and the like. The membrane module is suitable for the applicant's prior patent application technology (application number: 200510133640.0).

The membrane filtration system of the present invention adopts a submerged external pressure hollow fiber membrane module. The membrane module is applicable to the applicant's prior patent application technology (application number: 200510133640.0).

For a membrane device or system, according to the size of the treated water, it can be composed of multiple membrane modules connected in series or in parallel. When the treatment capacity is large enough, multiple separation tanks can also be set, each separation tank is filled with enough membrane modules, and each separation tank is equipped with a dedicated low-pressure suction pump. The suction pump can also be used as a backwash pump, or can be specially configured with a backwash pump; the cleaning pump can be shared by multiple pools in the entire membrane device system.

The cleaning system described in the membrane device of the present invention can realize online cleaning, including water backwashing, chemical cleaning and the like. Obviously, membrane fouling will inevitably occur during the use of the membrane. Membrane fouling will directly lead to the decrease of membrane flux and function, so the membrane needs to be cleaned. The membrane cleaning device of the invention can make the membrane system run stably for a long time.

The control system described in the membrane device of the present invention is mainly a PLC controller, including corresponding software and a touch screen.

The operating method or operating mode of the submerged hollow fiber membrane separation device of the present invention is as follows: the membrane filtration adopts the mode of opening for 8-12 minutes and stopping for 1-3 minutes, that is, the membrane system produces water for 8-12 minutes, and stops producing water For 1-3 minutes, the membrane unit is equipped with a perforated aeration tube for the shaking of the membrane filament. The aeration tube is in a normally open state. When the membrane module does not produce water, it is in an empty aeration state. The purpose is to reduce the activity deposited on the membrane surface. Sludge is blown off to slow down membrane surface fouling and maintain relatively stable membrane flux.

Membrane fouling is judged by the positive and negative pressure gauge readings on the water production pipe. When the pressure gauge reading drops to a certain set value, the system needs to be cleaned online. If the cleaning effect is not satisfactory, high-concentration liquid medicine should be used for off-line cleaning outside the system.

Through this process, the COD of fermentation liquid wastewater can be reduced from 4000-5000 mg/L to below 80 mg/L, and the ammonia nitrogen can be reduced from 300-600 mg/L to below 15 mg/L. The denitrification rate reaches over 80%. The solid content (SS) of the product water is less than 3mg/L. This process is an energy-saving and efficient waste water treatment and reuse process for monosodium glutamate and fermentation industry.

Example

Below according to Fig. 1, process flow and system equipment of the present invention are described with the monosodium glutamate wastewater treatment example.

As shown in Figure 1, the main parts of wastewater treatment in the present invention include anaerobic outlet pool 100, anoxic pool 2, one-stage aerobic pool 3, two-stage aerobic pool 4, and membrane pool 5 in liquid communication in sequence, wherein anaerobic The effluent pool 100 is liquid-communicated with the anoxic pool 2 through the pipeline 80, the bottom of the anoxic pool 2 is connected with the bottom of the pool 3 and the pool 4, and the mixed solution of the pool 4 overflows to the pool 5, so the sludge and the treated liquid can flow to the next processing equipment.

The COD value of monosodium glutamate wastewater is reduced from 4000-5000mg/L to 300-1000mg/L through the ordinary anaerobic (UASB) process. After anaerobic treatment, it increases slightly, and the concentration is 300-600mg/L, and sometimes reaches more than 700mg/L when the production fluctuates. The anaerobic waste water flows into the storage tank 100, and then is lifted to the grid well 21 on the top of the anoxic tank 2 through the centrifugal pump 101, and enters the anoxic tank 2 through the fine grid 1 set in the grid well 21. . The bottom of the anoxic pool 2 communicates with the first-stage oxygen pool 3 and the second-stage oxygen pool 4, and then overflows to the pool 5, so the sludge flows back from the aerobic pool 3 and the membrane pool 5 through the sludge return pumps 102 and 103 respectively. In the anoxic pool 2, the return flow is regulated by valves 139 and 138 respectively. The reflux pump 102 is set at the bottom of the aerobic tank 4 , and the reflux pump 103 is set at the bottom of the membrane tank 5 .

In the anoxic tank 2, nitrite and nitrate react with the organic matter (COD) in the influent to generate nitrogen to achieve denitrification, and at the same time generate carbonate alkalinity to supplement the alkalinity consumption of the subsequent nitrification reaction. An agitation device 161 is installed in the anoxic tank 2, which plays the role of agitation and mixing, and avoids insufficient biochemical reactions of sludge settling. The mixture enters an aerobic zone by gravity flow.

One section of aerobic pool 3 is equipped with stirring device 162 and microporous aeration tube. The microporous aeration pipes are installed in groups and have valves respectively. The number of switch groups of the aeration pipes can be adjusted according to the change of the influent water quality, and the valve opening can be controlled through the valve 1310 to realize the time change of anoxic and aerobic and the control of dissolved oxygen. Before entering the second-stage aerobic pool 4, the dissolved oxygen is controlled below 1.0 mg/L, so that ammonia nitrogen can undergo semi-nitration reaction as much as possible to generate nitrite, which can realize short-range nitrification and save energy. At this stage, more than 80% of ammonia nitrogen forms nitrite or nitrate.

After nitrosation, part of the unnitrated ammonia nitrogen and part of nitrite enter the subsequent second-stage aerobic pool 4 and membrane pool 5 . Among them, in the aerobic pool, the dissolved oxygen should be controlled at about 2.0 mg/L, so that the nitrification reaction can be completed, and the ammonia nitrogen and nitrite nitrogen can be reduced from flowing out of the system through the membrane system.

A solution oxygen meter 121 and a pH meter 122 are installed in the membrane pool 5 to monitor dissolved oxygen and the pH of the mixed solution.

Oxygen supply to the system is realized by blower 91 . The fan 91 is connected to the first aerobic tank through the first aerobic tank air supply valve 1310, connected to the second aerobic tank through the second aerobic tank valve 1311, and connected to the membrane tank 5 through the membrane tank air supply valve 1312. In this way, when the dissolved oxygen is low, it can be adjusted by valves 1310, 1311, 1312.

The fan 92 is used for supplying the air volume of the membrane filament shaking of the membrane unit 15 . Due to the high concentration of ammonia nitrogen in the influent, a large amount of alkalinity will be consumed in the biochemical process to gradually reduce the pH. When the pH is lower than 7.0, it will affect the progress of the nitrification reaction. According to the pH measurement, the system should be properly supplemented with alkalinity to supplement the alkalinity. The method can automatically control the frequency of the alkali-adding pump according to the online pH, and can also use the manual valve to adjust the amount of alkali-adding. The alkali used is preferably sodium carbonate.

The instrument air for the pneumatic regulating valve in the system comes from the air storage tank 8 and is supplied through the decompression filter valve 137 .

The membrane module in the membrane system of the present invention is a hollow fiber submerged type, and the system operation mode is as follows: the membrane module is a membrane unit 15 composed of 40 curtain membranes, and the number of membrane units can vary according to the amount of water to be treated. The number of membrane units can also be changed according to specific conditions. In this embodiment, there are 10 membrane units, each of which is a group of two, and each group is equipped with a flow meter 14, a pneumatic control valve 133 and a manual valve. Regulate valve 134 . The water outlet mode of the system is negative pressure water outlet, and the water outlet suction pump 104 is a frequency conversion pump. According to the water outlet requirements of the system, it is realized by frequency conversion, and the water output is realized by controlling the opening of the pneumatic regulating valve 133 according to the set value of the flow meter 14 . Membrane work is to open for 8 minutes and stop for 2 minutes, which is also realized by valve 133 start and stop. That is, the valve 133 is opened for 8 minutes to produce water, and closed for 2 minutes to produce no water and air to aerate. When the membrane system is opened for the first time, because there is air in the pipeline, it needs to be vacuumed to pump out the system gas, and the water will be produced through the membrane. The vacuum system is composed of a vacuum pump 107 and a solenoid valve 131. Close, vacuuming stops. When the system has multiple sets of membrane units, it can be vacuumized in groups until all the water is discharged.

Liquid level gauges 111 and 112 are respectively installed in the membrane pool 5 and the water production pool 6 to be connected to the PLC. The liquid level gauge 111 controls the liquid level of the entire biochemical pool. When the liquid level is high, the electric valve 1313 is automatically opened; 1313 Shut down the system to stop water intake. The liquid level gauge 112 is a protective liquid level gauge for the membrane unit 15 and the sludge return pump 103. When the liquid level is at a low level, the system stops producing water and the sludge return pump stops running, indicating that the water inlet system is faulty. At this time, the system Call the police.

The membrane cleaning system is divided into online cleaning and offline cleaning. Off-line cleaning is to put the membrane unit 15 detachment system into the membrane cleaning tank for chemical soaking. The cleaning agent can be cleaned with sodium hypochlorite or citric acid with a concentration of 1000-2000mg/L. The specific soaking time And the concentration of liquid medicine depends on the type and degree of pollution of pollutants. The specific method is applicable to the applicant's prior patent application technology (application number: 200510133640.0).

Online cleaning is mainly realized by backwashing. The backwashing system includes a backwashing pump 105, a backwashing dosing pump 106, a liquid medicine storage tank 7, a solenoid valve 132, and a regulating valve 135. The cleaning liquid is stored in the medicine tank 7. Open the solenoid valve 132 during cleaning, pump the concentrated liquid medicine into the backwash pipeline, the backwash pump 105 is connected to the membrane water production tank 6, and use the membrane water production for backwash water, start the PLC backwash program during backwash, and open the valve 136 , 135, the backwash water and the chemical solution are mixed in the pipeline and then enter the hollow fiber membrane filament in the membrane unit 15, reversely clean the contaminated sludge on the membrane surface to make it fall off, and at the same time sterilize the water production system to restore the membrane flow quantity. Membrane cleaning is judged by the reading of the pressure gauge in the water production pipeline. When the reading of the pressure gauge drops by 20-30KPa, the membrane system needs to start the cleaning program. The cleaning can be done in groups. Only one group of membrane units is cleaned each time, and the other membrane groups are still working. , to ensure the continuity of water production in the system.

After the biochemical reaction and membrane filtration of monosodium glutamate wastewater or fermentation liquid production wastewater, the COD, ammonia nitrogen, and suspended solids in the produced water are greatly reduced, COD can be reduced to below 80mg/L, ammonia nitrogen can be reduced to below 15mg/L, and the removal rate is over 95%. , Suspended solids are below 3mg/L, membrane produced water reaches the first-class discharge standard, and can be further desalted through reverse osmosis and reused in the process or circulating cooling water system or directly reused. The fermentation and monosodium glutamate industry is also one of the industries that generate the most wastewater. The MBR integrated process and equipment described in the present invention provide a new water recycling method for the sustainable development of enterprises, which can realize energy saving, emission reduction and sewage recycling.

Claims (6)

1, a kind of membrane biologic reaction equipment that is used for the industrial waste water with high ammoniac nitrogen processing is characterized in that, comprising:

The anaerobism outlet sump (100), anoxic pond (2), one section Aerobic Pond (3), two sections Aerobic Ponds (4), the membrane cisterna (5) that are linked in sequence according to fluid flow, wherein,

Anaerobism outlet sump (100) is used to store the anaerobism water outlet, plays the effect of regulating and supplying water;

The downstream of anaerobism outlet sump (100) is provided with anoxic pond (2), and above-mentioned anoxic pond (2) is carried out denitrogenation to organism in the water;

The downstream of anoxic pond (2) is provided with one section Aerobic Pond (3), and above-mentioned one section Aerobic Pond (3) carries out nitrosification and nitrated to ammonia nitrogen;

One section Aerobic Pond (3) downstream is provided with two sections Aerobic Ponds (4), and it carries out abundant oxidation to not nitrated ammonia nitrogen and the part nitrite of part in one section Aerobic Pond (3);

Two sections Aerobic Ponds (4) end connects membrane cisterna (5), and the tubular fibre membrane filter plant of immersion blocking wherein is set in the membrane cisterna, and treatment solution is carried out solid-liquid separation.

2, the membrane biologic reaction equipment that is used for the industrial waste water with high ammoniac nitrogen processing according to claim 1 is characterized in that,

Anaerobism outlet sump (100) is by pipeline (80) and anoxic pond (2) fluid connection, and waste water rises to grille well (21) through impeller pump (101), enters anoxic pond (2) through the fine fack (1) that is arranged in the grille well (21).

The membrane biologic reaction equipment that is used for the industrial waste water with high ammoniac nitrogen processing according to claim 1 and 2 is characterized in that,

The bottom of anoxic pond (2) links to each other with one section Aerobic Pond (3), two sections Aerobic Ponds (4) bottom, liquid overflows to membrane cisterna (5) from two sections Aerobic Ponds (4), mud by sludge reflux pump (102) that is arranged on Aerobic Pond (3) bottom and the sludge reflux pump (103) that is arranged on membrane cisterna (5) bottom, is back to anoxic pond (2) from Aerobic Pond (3) and membrane cisterna (5) respectively.

3, the membrane biologic reaction equipment that is used for the industrial waste water with high ammoniac nitrogen processing according to claim 1 is characterized in that,

Be provided with whipping appts (162) and micropore aeration pipe in one section Aerobic Pond (3), the micropore aeration pipe grouping is installed, and can change the micropore aeration pipe working quantity according to the water quality situation, regulates anoxic/aerobic time.

4, the membrane biologic reaction equipment that is used for the industrial waste water with high ammoniac nitrogen processing according to claim 1 is characterized in that,

Also be provided with gas blower (91), carrying out oxygen supplies with, above-mentioned blower fan (91) is connected with one section Aerobic Pond by one section Aerobic Pond air-supply valve (1310), be connected with two sections Aerobic Ponds by two sections Aerobic Pond valves (1311), link to each other with membrane cisterna (5) by membrane cisterna air-supply valve (1312), when dissolved oxygen is low, can regulate by one section Aerobic Pond air-supply of above-mentioned valve valve (1310), two sections Aerobic Pond valves (1311), membrane cisterna air-supply valve (1312).

5, a kind of membrane bioreaction induction method that is used for the industrial waste water with high ammoniac nitrogen processing is characterized in that:

Industrial waste water with high ammoniac nitrogen at first passes through anaerobic treatment, and anaerobism is decomposed into small organic molecule with the macromole hardly degraded organic substance, and entering the pond then is that subsequent technique supplies water;

Next enter the anoxic stage of anoxic pond, the nitrate nitrogen that produces in the aerobic processes and nitrite nitrogen denitrification are become nitrogen reach denitrogenation;

Next enter one section Aerobic Pond carry out one section aerobic, the control dissolved oxygen is in low scope, carries out one section backflow after making ammonia nitrogen be converted into nitrite nitrogen, realizes nitrosification-denitrifying short distance nitration process,

Residue nitrite and ammonia nitrogen enter subsequently two sections Aerobic Ponds carry out two sections aerobic, change nitrate nitrogen into;

Carry out two sections mud at last in the membrane sepn pond of system terminal and reflux, the mixed-liquor return that will contain nitrate nitrogen is to anoxic pond, and further denitrification is a nitrogen.

6, the membrane bioreaction induction method that is used for the industrial waste water with high ammoniac nitrogen processing according to claim 5 is characterized in that:

Membrane filtration adopts and opened 8-12 minute, stops 1-3 minute mode, and promptly the film system produced water 8-12 minute, stopped to produce water 1-3 minute;

Be provided with the boring aeration pipe that is used for film silk shake in the membrane cisterna, aeration tube is in normally open, when membrane module does not produce water, is in sky aeration state, thereby with the active sludge stripping of film surface deposition, slows down the film surface contamination, and it is relatively stable to keep membrane flux.

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