WO2013185350A1

WO2013185350A1 - Internal-circulation aeration anammox-membrane bioreactor

Info

Publication number: WO2013185350A1
Application number: PCT/CN2012/077009
Authority: WO
Inventors: 陈静; 彭培源; 郑园蓁; 王悦超
Original assignee: 乐金电子研发中心(上海)有限公司
Priority date: 2012-06-15
Filing date: 2012-06-15
Publication date: 2013-12-19
Also published as: CN104350012A

Abstract

Disclosed is an internal-circulation aeration Anammox-membrane bioreactor, comprising a continuous stirred-tank anaerobic reactor, a membrane component, and a gas internal circulation device. The anaerobe grows in an even and suspended manner in the continuous stirred-tank anaerobic reactor, and to-be-treated waste water containing high ammonia nitrogen and nitrite enters the continuous stirred-tank anaerobic reactor; the anaerobe is evenly and fully mixed with the pollutants in intake water; the ammonia nitrogen and nitrite in the waste water are removed by the Anammox bacteria and are subject to solid-liquid separation by the membrane component; the anaerobe is held in the reactor, to prevent the anaerobe growing in a suspended manner from flowing out of the continuous stirred-tank anaerobic reactor. In the foregoing treatment process, nitrogen generated during the reaction of the Anammox bacteria is used as an anaerobic gas source; the nitrogen generated in the anaerobic reactor is delivered to a membrane aeration cleaning distributer in a circulating manner; after passing through the membrane component, the gas then return to the anaerobic reactor, hence implementing the recycling of the nitrogen.

Description

Internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor

The present technology relates to a sewage treatment technique, and more particularly to an internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor. Background technique

In recent years, nitrogen pollution in water has become more and more serious, and pollution problems caused by the environment have become increasingly prominent. Compared with physical and chemical denitrification technology, biological denitrification technology has the advantages of simple process, low cost, and promotion of trade, and is widely used.

The traditional biological nitrogen removal process is a three-stage activated sludge system. In this process, the oxidation of carbon-containing organic matter and the ammoniation of nitrogen-containing organic matter, the nitrification of ammonia nitrogen, and the denitrification of nitrate are carried out in three structures, respectively. Maintain separate sludge return systems. As shown in Figure 1, it is a schematic diagram of the structure of the existing nitrification-denitrification denitrification system. The system includes:

a) aeration tank: oxidize organic matter (B0D) by heterotrophic B0D oxidizing bacteria under aerobic conditions; b) biological nitrification reactor: through the action of nitrite bacteria and nitrate bacteria under aerobic conditions, Oxidizing ammonia nitrogen to nitrite nitrogen and nitrate nitrogen;

c) Biological denitrification reactor: Under the condition of anoxic conditions, nitrite nitrogen and nitrate nitrogen are reduced to nitrogen due to the action of facultative denitrifying bacteria (denitrifying bacteria).

Traditional biological nitrogen removal technologies, including nitrification and denitrification processes, are completed by the autotrophic nitrifying bacteria and heterotrophic denitrifying bacteria. Due to the different environmental requirements of the flora (dissolved oxygen, alkalinity) and mutual competition with the matrix, in order to stabilize the denitrification function, two or more reactors are often used in operation (see Figure 1). Therefore, the traditional biological nitrogen removal process has long process, complicated control and high operating cost.

a) Nitrifying bacteria are autotrophic bacteria that grow slowly and cannot compete with heterotrophic bacteria in a mixed culture activated sludge system, making it difficult to obtain advantages;

b) Nitrifying bacteria are susceptible to external influences and are very sensitive to environmental shocks, especially toxic shocks, and it is quite difficult to restart the system;

c) Nitrification and denitrification are difficult to be unified in time, and the effect of nitrogen removal is poor. The multi-step biocatalytic reaction of biological nitrogen removal is limited by factors such as matrix transfer rate, substrate and product inhibition. From the perspective of sustainable development, the traditional biological nitrogen removal method firstly consumes a large amount of energy. The oxygen equivalent of ammonia nitrogen is 4.57g. To supply oxygen, energy is consumed. Similarly, if internal reflux is set, energy consumption is increased. Secondly, In the denitrification process, organic carbon is used as an electron donor. If the carbon source is insufficient, an external carbon source (such as methanol) is required, which significantly increases operating costs.

Based on the defects of the above-mentioned biological nitrogen removal technology, some existing technical solutions for combining membrane separation technology with anaerobic ammonium oxidation technology to enrich anaerobic ammonium oxidizing bacteria, such as anaerobic ammonium oxidation-free aerated membrane organisms. A reactor, which typically includes an anaerobic reactor, a membrane module, an influent, a effluent, and a sludge reflux system. The patent application No. 20101C523416. 3 discloses an external anaerobic ammonium oxide membrane bioreactor, as shown in FIG. 2; the patent application No. 200620104478. X discloses a membrane-anaerobic ammonia oxidation organism. The reactor is shown in Figure 3.

The biggest problem with the above anaerobic ammonium oxide membrane bioreactor is that there is no aeration scrub system. Aeration scrubbing is the most effective means of preventing and controlling membrane fouling. The absence of an aeration scrub system will result in:

a) Severe membrane fouling problem: The absence of an aeration scrub system will rapidly deposit membrane contaminants such as microorganisms, particulate matter, inorganic precipitates, and organic macromolecules onto the membrane surface and block the pores of the membrane. The membrane flux is rapidly reduced, and the transmembrane pressure difference rises rapidly.

b) Significantly increase the on-line and off-line chemical cleaning frequency of the membrane: This will significantly increase the operating cost of the membrane bioreactor, and frequent chemical cleaning will poison the microbial flora in the system and reduce the nitrogen removal efficiency of the system.

c) Frequent replacement of membrane modules: Due to the high deposition rate of contaminants and low cleaning efficiency, membrane modules can quickly become irreversible membrane fouling, so frequent replacement of new membrane modules is required, and reactor replacement membrane modules are frequently turned on. It will increase the dissolved oxygen concentration of the system, destroy the living environment of anammox bacteria, and significantly increase the operating cost of the system.

d) Low concentration of anaerobic ammonium oxidation sludge in the system: In order to control membrane fouling, frequent sludge discharge is required to control the concentration of anaerobic ammonium oxide sludge in the system, and the sludge concentration is controlled to a relatively low concentration range (5- 15g/L), this will extend the system startup time. And because of the low sludge concentration, it will reduce the operating load of the system and reduce the impact resistance and stability of the system. Summary of the invention

The technical problem addressed by the present invention is to provide an internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor to improve or overcome one or more of the deficiencies of the prior art.

The technical solution of the present invention is: an internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor, the membrane bioreactor comprising: In an anaerobic reactor, anaerobic organisms are uniformly suspended in the anaerobic reactor, and the sewage to be treated containing high ammonia nitrogen and nitrite is introduced into the anaerobic reactor, and the pollutants in the anaerobic organism and the influent water are evenly distributed. Fully mixed

Membrane module, ammonia nitrogen and nitrite in the sewage are removed by the anaerobic ammonium oxidizing bacteria in the full-mix anaerobic reactor, and then the solid-liquid separation is performed by the membrane module, and the anaerobic organism is trapped in the reactor. Anaerobic organisms that avoid suspended growth are lost from the fully mixed anaerobic reactor to increase sludge concentration;

The gas internal circulation device uses nitrogen generated by the anammox reaction as a source of anaerobic gas, and circulates the nitrogen generated in the anaerobic reactor to the membrane aeration cleaning distributor under the membrane module, through the membrane The gas after the assembly is returned to the anaerobic reactor, thus achieving the recycling of nitrogen.

The features and advantages of the present invention are as follows:

1 Compared with the traditional biological nitrogen removal process, the floor space and energy consumption level of the invention will be significantly reduced by more than 50%, and the operating cost can be saved by more than 80%;

2 Due to the anaerobic internal circulation gas membrane scrubbing technology, the anaerobic environment of the system is ensured, and the membrane module can be effectively scrubbed to significantly reduce the membrane fouling rate. Therefore,

2. 1 Relative to the existing anaerobic ammonium oxidation process:

The increase of the ammonia nitrogen removal rate from 80% to more than 90%, the total nitrogen load can be increased from 0. 5~0. 8 kg/m3/day to >=2. 0 kg/m3/day„ 2. 2 Relative to the existing anaerobic ammonium oxidation-non-aeration membrane bioreactor (see Figure 2, Figure 3)

a) The anaerobic ammonium oxidation sludge concentration of the system can be increased from 5-15 _g /L to 20-40 _g / L, which significantly increases the stability and impact resistance of the system;

b) The membrane cleaning service life can be increased from 30-40 days to more than 3 years;

c) The frequency of membrane cleaning can be reduced by daily cleaning to 1 week or once a month, or lower (depending on the specific operation);

2. 3 Relative to reactors using exogenous anaerobic gas as the source of aeration system gas:

The system of the present invention does not require external anaerobic gas at all during operation, and the gas storage tank can also be removed, which significantly reduces system construction cost and operating cost. DRAWINGS

Figure 1 is a schematic view showing the structure of a conventional nitrification-denitrification denitrification system.

Figure 2 is a drawing of Figure 2 of the Chinese patent CN10196225A (external anaerobic ammonium oxide membrane bioreactor).

Figure 3 is a drawing of Chinese patent CN2900509A (membrane-anaerobic ammonia oxidation bioreactor). 4a to 4d are schematic structural views of four specific embodiments of the present invention. this

Based on the defects described in the above background art, if the air aeration scrub system commonly used in current aerobic membrane bioreactors is selected, the anaerobic environment of the system will be seriously damaged, resulting in the failure of anaerobic ammonium oxidizing bacteria to grow, and the system is completely瘫痪; If an external anaerobic gas (such as industrial nitrogen, carbon dioxide, etc.) is used as the gas source for the aeration scrub system, because of the large gas flow required, it is first necessary to design a bulky gas tank for storage of the external source. Anaerobic gas, which will significantly increase the footprint and construction cost of the system; Secondly, it will consume a large amount of external anaerobic gas during operation, which will significantly increase the operating cost of the system.

In order to solve the above problems, the present invention provides an internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor comprising a full-mix anaerobic reactor, a membrane module, and a gas internal circulation device, wherein the anaerobic organism is The mixed anaerobic reactor is uniformly suspended and grows. The sewage to be treated containing high ammonia nitrogen and nitrite enters the fully mixed anaerobic reactor, and the anaerobic organisms are uniformly mixed with the pollutants in the influent water. The ammonia nitrogen and nitrite are removed by the anaerobic ammonium oxidizing bacteria in the fully mixed anaerobic reactor, and then the solid-liquid separation is carried out by the membrane module, and the anaerobic organisms are all trapped in the reactor to avoid suspension growth. Anaerobic organisms are lost from the fully mixed anaerobic reactor, and the sludge concentration is increased. In the foregoing reaction process, nitrogen generated by the anammox reaction is used as a source of anaerobic gas, and is circulated through the gas inner circulation passage. Means the nitrogen gas generated in the anaerobic reactor is sent to the membrane aeration cleaning distributor below the membrane module, and the gas is returned to the anaerobic reactor after passing through the membrane module, Now using nitrogen circulation.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor combines the anaerobic internal circulation aeration membrane separation technology with the anaerobic ammonium oxidation technology, and utilizes the anaerobic gas generated by the system anaerobic ammonium oxidizing bacteria reaction as an annoyance Oxygen gas source, aeration or external (pressure) membrane module is aerated and cleaned by internal circulation gas flow or gas-liquid jet method, thereby overcoming high energy consumption in existing nitrification/denitrification biological nitrogen removal process High investment, high operating costs, etc., as well as serious membrane fouling problems and low sludge concentration defects in aeration-free anaerobic ammonium oxidation-membrane bioreactors.

The above and other objects, features and advantages of the present invention will become more apparent from the aspects of the invention. The figure is described in detail below.

Example 1 External internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor

As shown in Fig. 4a, it is a schematic structural view of a preferred embodiment of the internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor of the present invention. This embodiment is an external internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor, which includes water inlet Pool 1, feed pump 2, anaerobic reactor 3, membrane module 4 and its associated equipment (such as closed membrane tank 4-1), water pump 5, distributor 6, gas storage tank 7, pressure ceramic 8, transmembrane The differential pressure probe 9, the sensor 10, the circulation pump 11, the gas flow meter 13, the agitator 14, the gas circulation pump 15, and the absorption tower 16. The sewage in the water inlet tank 1 is pumped into the anaerobic reactor 3 by the feed water pump 2, and the upper gas collecting space of the anaerobic reactor 3 and the distributor 6 disposed under the membrane module 4 are connected through a gas supply line. A gas circulation pump 15 and a gas flow meter 13 are disposed on the air supply line, and an air outlet of the upper portion of the sealed membrane tank 4-1 and an upper gas collection space of the anaerobic reactor 3 are communicated through a return gas pipeline, and the gas return pipeline is connected An absorption tower 16 is provided.

In this embodiment, a fully mixed anaerobic reactor is preferably used, and anaerobic organisms are uniformly suspended and grown in the anaerobic reactor. The anaerobic ammonium oxidizing bacteria in the anaerobic reactor utilize nitrite as an electron acceptor, and ammonia nitrogen is used. Oxidation to nitrogen.

In this embodiment, an external microfiltration membrane or an ultrafiltration membrane membrane module is used, and the assembly structure of the membrane module 4 can be selected by a hollow fiber membrane or a flat membrane, and the material thereof can be an organic membrane or an inorganic membrane. The separation membrane retains most of the anaerobic ammonia oxidizing bacteria and other suspended particulate matter in the reactor, and the filtrate is pumped from the system by a suction pump 5. Since the filtrate water quality meets or exceeds national emission or reuse standards, it can be discharged directly or further into the water reuse system.

In this embodiment, the gas inner circulation passage includes a gas supply line connecting the anaerobic reactor and the distributor below the membrane module, and an outlet port connecting the closed membrane tank 4-1 and a return gas line of the anaerobic reactor 3. .

The gas supply line is provided with a gas circulation pump 15 and a gas flow meter 13. The nitrogen in the anaerobic reactor 3 is taken out from the head space of the anaerobic reactor 3 by the gas circulation pump 15 and sent to the membrane. The gas is cleaned to the dispenser 6.

Preferably, the return line is provided with an absorption tower 16 for absorbing the substance to be blown off to reduce the inhibitory effect of harmful substances on anaerobic organisms in the anaerobic reactor 3.

In addition, the gas internal circulation device further includes a gas storage tank 7 disposed on another branch of the return air line, and the gas volume for internal circulation can be controlled by the gas flow meter, so that more gas than the required gas amount in the reactor can flow automatically A gas storage tank for storing excess gas as a backup gas, the gas storage tank 7 is provided with a pressure valve 8 which automatically opens the exhaust gas when the pressure in the gas storage tank 7 reaches a certain limit.

In this embodiment, a liquid internal circulation passage is formed between the anaerobic reactor 3 and the closed membrane tank 4-1, and the liquid internal circulation passage includes a connection between the upper portion of the anaerobic reactor and the upper portion of the closed membrane tank 4-1. a liquid line and a liquid return line connecting the lower portion of the closed membrane tank 4-1 and the lower portion of the anaerobic reactor 3. A circulation pump 1 1 is provided on the liquid supply line.

In order to monitor the change in the reaction environment in the anaerobic reactor 3, it is preferred to provide a sensor 10 for monitoring values such as temperature, 0 RP, pH, etc. in the anaerobic reactor 3.

In order to facilitate a more accurate understanding of the technical solution corresponding to this embodiment, the main working process is described as follows: a. The sewage to be treated containing high ammonia nitrogen and nitrite is pumped from the inlet tank 1 into the anaerobic reactor 3 by the feed water pump 2; b. The ammonia nitrogen in the sewage, the nitrite and the anaerobic in the anaerobic reactor 3 The ammonia oxidizing bacteria are in contact with each other, and the nitrite is used as an electron acceptor to oxidize the ammonia nitrogen to nitrogen. The total reaction formula is as follows - 1V + 1..32Ν(3⁄4-' +· 0.066H(X> + 0A3W— *

0.26 (3⁄4~ +! .02fi ₂ + 0.066CH ₂ (3⁄4,s ₀ , _i3 ÷ 2.03H ₂ O

c. The ammonia nitrogen and nitrite in the sewage are removed by the anaerobic ammonium oxidizing bacteria in the anaerobic reactor 3, and further transported by the circulation pump 11 to the membrane module 4 outside the anaerobic reactor 3 and its supporting equipment (sealed In the membrane tank 4-1), the filtrate of the membrane module 4 is pumped from the system by a suction pump 5. Because the filtrate water quality meets or exceeds national emission or reuse standards, it can be discharged directly or further into the water reuse system.

d. Anaerobic ammonium oxidizing bacteria or other particulate matter trapped outside the membrane module 4 will return directly to the anaerobic reactor 3 .

e. Using nitrogen produced by the anammox reaction in the anaerobic reactor 3 as a source of anaerobic gas, it is withdrawn from the head space of the anaerobic reactor 3 by the gas circulation pump 15 in a cyclic manner, and the gas passes through the membrane module 4 The membrane aeration cleaning distributor 6 below effectively scrubs the membrane module 4, and then the gas is returned from the closed membrane tank 4-1 to the anaerobic reactor 3 by the circulation line; the excess gas is stored in the specific gas storage tank 7 as The backup gas or direct discharge, when the pressure in the gas storage tank 7 reaches a certain limit, the pressure valve 8 is opened to automatically discharge the gas.

In this embodiment, a full-mix anaerobic reactor is used, and anaerobic organisms are uniformly suspended and grown in the full-mix anaerobic reactor, and anaerobic organisms and influent pollutants can be uniformly and uniformly mixed, so the anaerobic biological growth state Good, there will be no local concentration too high or too low, and all parts of the reactor can efficiently generate anaerobic reactions, thus effectively removing pollutants. The membrane module acts as a high-efficiency solid-liquid separation. The liquid internal circulation pathway can completely trap the slow-growing anaerobic organisms in the reactor, avoiding the loss of suspended growth anaerobic organisms from the reactor, thereby significantly increasing the sludge concentration. Internal circulation aeration can effectively scrub the membrane module, significantly reducing the number of chemical cleaning of the components and the number of membrane module replacements, thereby minimizing chemical cleaning agents (especially oxidative cleaning agents) and frequent replacement of components. The effects of factors such as elevated dissolved oxygen concentration in the system on anaerobic organisms.

In this embodiment, an absorption tower 16 (such as a hydrogen sulfide absorption tower, an ammonia absorption tower, etc.) for discharging the substance is placed on the gas inner circulation passage, and the internal circulation aeration process may be harmful to the anaerobic reactor 3. The substance is blown off, effectively reducing the inhibitory effect of harmful substances on the anaerobic organisms in the anaerobic reactor 3, and significantly improving the efficiency, impact resistance and stability of the anaerobic reactor 3.

In order to monitor the trend of membrane fouling, the transmembrane pressure difference probe 9 can be used to monitor the transmembrane pressure difference, and the temperature, 0RP, pH and other sensors 10 are used to monitor the reaction environment change of the anaerobic reactor. Example 2 Built-in internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor

As shown in Fig. 4b, it is a schematic view of the structure of Example 2 of the internal circulation aeration anammox-membrane bioreactor of the present invention. This embodiment is a built-in internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor comprising a water inlet tank 1, a feed water pump 2, an anaerobic reactor 3, a membrane module 4, an outlet pump 5, a distributor 6, and a gas reservoir. The tank 7, the pressure valve 8, the transmembrane differential pressure probe 9, the sensor 10, the gas flow meter 13, the agitator 14, the gas circulation pump 15, and the absorption tower 16.

In the same manner as in the first embodiment, the present embodiment employs a fully mixed anaerobic reactor in which the anaerobic organism is uniformly suspended and grown, and the anaerobic ammonia oxidizing bacteria in the anaerobic reactor utilize nitrous acid. The salt is an electron acceptor that oxidizes ammonia nitrogen to nitrogen.

The main difference from Embodiment 1 is that the present embodiment is such that the membrane module 4 is disposed inside the anaerobic reactor 3, that is, a built-in membrane module is employed. Corresponding to this feature, in this embodiment, it is not necessary to provide the liquid inner circulation passage in the first embodiment, and the gas inner circulation passage only needs to provide a gas supply line connecting the anaerobic reactor and the distributor below the membrane module. Yes, it is not necessary to provide the return air line in Embodiment 1.

Corresponding to the above structure, the main working principle of this embodiment is similar to the embodiment, mainly the steps c, d, e are slightly different: In the above step c, the ammonia nitrogen and nitrite in the sewage pass through the anaerobic reactor 3 After the anaerobic ammonium oxidizing bacteria is removed, the membrane module 4 is further contacted, and the separation membrane module 4 retains most of the anammox bacteria and other suspended particulate matter in the anaerobic reactor 3, and the filtrate is suctioned. The pump 5 is pumped out of the system; in this embodiment, since the built-in membrane module is employed, the step in the first embodiment is not required, and in the step e, the anaerobic ammonium oxidizing bacteria reaction in the anaerobic reactor 3 is utilized. Nitrogen is used as a source of anaerobic gas, which is withdrawn from the head space of the anaerobic reactor 3 by a gas circulation pump 15 in a circulating manner, and the gas is effectively scrubbed by the membrane aeration cleaning distributor 6 below the membrane module 4, and finally Return to the gas gathering space in the upper part of the anaerobic reactor 3 and enter the subsequent cycle. The excess gas in the upper gas collecting space of the anaerobic reactor 3 is stored in the gas storage tank 7 as a backup gas or directly discharged. When the pressure in the gas storage tank reaches a certain limit, the pressure valve 8 is opened to automatically discharge the gas.

In addition to the advantages described in the embodiment 1, the embodiment has the design form of the built-in membrane module, so that the inner circulation aeration can simultaneously achieve effective membrane cleaning, water inlet, and full mixing of the solid-liquid mixture in the reactor. And greatly simplify the system design, significantly reduce the investment cost, and the operation control is more convenient and stable. Example 3 External internal circulation jet aeration anaerobic ammonium oxidation-membrane bioreactor

As shown in Fig. 4c, it is a schematic structural view of Example 3 of the internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor of the present invention. This embodiment is an external internal circulation jet aeration anaerobic ammonium oxidation-membrane bioreactor comprising a water inlet tank 1, a feed water pump 2, an anaerobic reactor 3, a membrane module 4 and its supporting equipment (closed membrane tank 4 -1 ) , water pump 5, The gas-liquid mixed flow distributor 6, the gas storage tank 7, the pressure W8, the transmembrane differential pressure probe 9, the sensor 10, the circulation pump 11, the jet 12, the gas flow meter 13, the agitator 14, and the absorption tower 16.

Wherein, the sewage in the water inlet tank 1 is pumped into the anaerobic reactor 3 by the feed water pump 2, and the upper gas collecting space of the anaerobic reactor 3 and the gas-liquid mixed flow distributor 6 disposed under the membrane module 4 are exposed by the jet. The gas pipeline is connected. In this embodiment, the nitrogen gas is transported by means of a jet. The gas outlet of the upper portion of the closed membrane tank 4-1 and the upper gas gathering space of the anaerobic reactor 3 are connected through the gas return pipeline. An absorption tower 16 is disposed on the return line.

As in the first and second embodiments, the present embodiment preferably employs a fully mixed anaerobic reactor in which the anaerobic organism is uniformly suspended and grown, and the anaerobic ammonia in the anaerobic reactor. Oxidizing bacteria use nitrite as an electron acceptor to oxidize ammonia nitrogen to nitrogen.

As described above, the main difference between this embodiment and the embodiment 1 is that the present embodiment is a method in which the nitrogen in the upper gas collecting space of the anaerobic reactor 3 is sent to the distributor 6 below the membrane module by means of a jet. Specifically, the solid-liquid mixture in the anaerobic reactor 3 is pumped by the circulation pump 11 and then connected to the inlet end of the jet; the nitrogen line in the upper gas collecting space of the anaerobic reactor 3 is connected to the jet inlet. The gas-liquid mixture flows through the jet at a high speed by the circulation pump 11, and a negative pressure is formed at the inlet end in the jet, thereby sucking the nitrogen in the upper gas collecting space of the anaerobic reactor 3 into the jet. Inside (in order to increase the gas flow, a gas circulation pump may be added to the gas pump into the flow device), the gas flow rate is controlled by the gas flow meter 13, and then a gas-solid liquid high-speed mixed flow is formed inside the jet; the jet is formed in the jet The gas-solid liquid high-speed mixed flow forms a high-speed cross flow on the surface of the membrane via the distributor 6 below the membrane module, thereby effectively preventing membrane fouling. The lower portion of the closed membrane tank 4-1 communicates with the lower portion of the anaerobic reactor 3 through the liquid return line, so that the anaerobic ammonium oxidizing bacteria or other particulate matter trapped outside the membrane module can be directly returned to the anaerobic reactor 3 to form Liquid internal circulation system.

Correspondingly, the working work of this embodiment is substantially the same as that of the first embodiment, the difference mainly lies in the step e, the nitrogen generated by the anammox reaction is sucked from the head space of the anaerobic reactor by the jet 12 in a circulating manner, the gas and liquid The mixed stream is effectively scrubbed via the membrane aeration purge dispenser 6 below the membrane module 4, and then the gas is returned from the membrane module to the anaerobic reactor 3 by the recycle line: excess gas is stored in a particular gas storage tank 7 As a backup gas or direct discharge, when the pressure in the gas storage tank 7 reaches a certain limit, the pressure valve 8 is opened to automatically discharge the gas.

In addition to the advantages of the embodiment 1, the embodiment has a high flow velocity of the gas-solid liquid mixed flow due to the design of the inner circulation of the jet flow mode, the distributor 6 is not easily clogged, and the cross-flow velocity formed on the surface of the membrane is high, so it is particularly suitable for use. Treatment of high solid waste water. Example 4 Built-in internal circulation jet aeration anaerobic ammonium oxidation-membrane bioreactor As shown in Fig. 4d, it is a schematic structural view of Example 4 of the internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor of the present invention. This embodiment is a built-in internal circulation jet aeration anaerobic ammonia oxidation-membrane bioreactor, which includes a water inlet tank 1, a feed water pump 2, an anaerobic reactor 3, a membrane module 4 and its supporting equipment, a water pump 5, and distribution. The gas tank 7, the gas storage tank 7, the pressure valve 8, the transmembrane differential pressure probe 9, the sensor 10, the circulation pump 11, the fluidizer 12, the gas flow meter 13, the agitator 14, and the absorption tower 16.

Similar to Examples 1, 2, and 3, this embodiment adopts a fully mixed anaerobic reactor in which anaerobic organisms are uniformly suspended and grown in the anaerobic reactor, and anaerobic ammonium oxidation in the anaerobic reactor The bacterium uses nitrite as an electron acceptor to oxidize ammonia nitrogen to nitrogen.

The main differences between this embodiment and Embodiment 1 include:

Similar to the second embodiment, the membrane module of the present embodiment adopts a built-in membrane module, that is, the membrane module 4 is disposed inside the anaerobic reactor 3, and correspondingly, the relevant connecting pipeline also changes accordingly, for details, please refer to Example 2.

Further, similarly to the embodiment 3, in the present embodiment, the nitrogen in the upper gas collecting space of the anaerobic reactor 3 is sent to the distributor 6 below the membrane module by means of a jet. A gas jet is provided in the gas supply line of the gas inner circulation passage, and the nitrogen gas in the anaerobic reactor 3 is sucked by the liquid jet 12 and sent to the membrane aeration cleaning distributor 6.

In addition to the advantages of the embodiment 2, the embodiment has a high flow velocity of the gas-solid liquid mixing flow due to the design of the inner circulation of the jet flow mode, the distributor 6 is not easily clogged, and the cross-flow velocity formed on the surface of the membrane is high, so it is particularly suitable for use. Treatment of high solid waste water. The result composition and working principle of various embodiments of the present invention have been described above. After many experiments, the effects of the internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor include: The service life of the membrane module can be obtained from existing ones. Increased from 30-40 days to more than 3 years, the concentration of anaerobic ammonium oxidation sludge in the system can be increased from the existing 5-15g/L to 20-40g/L, and the membrane flux can be increased from the existing 3-5L to 10LMH. The floor space and energy consumption level will be significantly reduced by more than 50% compared with the traditional nitrification/denitrification biological nitrogen removal process, the operating cost can be saved by more than 8C%, and the system startup time will be shortened from one year to three months. the following.

In summary, the invention combines the anaerobic internal circulation aeration membrane separation technology with the anaerobic ammonia oxidation technology, and utilizes the anaerobic gas generated by the system itself to expose the immersed or external membrane module by means of internal circulation. Air cleaning, anaerobic organisms are uniformly suspended in the reactor, and the anaerobic organisms and the influent pollutants can be uniformly mixed uniformly, so the anaerobic biological growth state is good, and the local concentration is too high or too low; The membrane module acts as a high-efficiency solid-liquid separation to avoid the loss of suspended growth anaerobic organisms from the reactor, so that all the slow-growing anaerobic organisms can be trapped in the reactor, significantly increasing the sludge concentration; The membrane module can be effectively scrubbed, Significantly reduce the number of chemical cleaning of the components and the number of membrane module replacements, thereby minimizing the chemical cleaning agents (especially oxidative cleaning agents), as well as the frequent replacement of components resulting in increased concentrations of dissolved oxygen in the system. influences.

The above description is only a preferred embodiment of the invention and is not intended to limit the invention in any way. The present invention has been disclosed in the above preferred embodiments, but is not intended to limit the present invention. Any one skilled in the art can make some modifications or use the above disclosed technical contents without departing from the technical scope of the present invention. Equivalent embodiments modified to equivalent changes, such as the type of anaerobic reactor, the type or position of the membrane module, the type or amount of the accessory equipment included in the present invention, are not limited to the embodiments, but are not deviated from the technical solution of the present invention. Any simple modifications, equivalent changes and modifications of the above embodiments in accordance with the technical spirit of the present invention are still within the scope of the technical solutions of the present invention.

Claims

Claim

An internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor, characterized in that the membrane bioreactor comprises: an anaerobic reactor in which the anaerobic organism is uniformly suspended and grown, and contains high The sewage to be treated of ammonia nitrogen and nitrite enters the anaerobic reactor, and the anaerobic organism is uniformly mixed with the pollutants in the influent water;

2. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the gas internal circulation device comprises a gas circulation pump, and the nitrogen in the anaerobic reactor is annoying The oxygen reactor headspace is withdrawn by the gas circulation pump and delivered to the membrane aeration purge dispenser.

3. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the gas internal circulation device comprises a jet, and the nitrogen in the anaerobic reactor is via a jet The jet is sprayed at a high speed and sent to the membrane aeration cleaning dispenser.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the gas internal circulation device further comprises a gas storage tank for storing excess gas as a backup gas.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 4, wherein the gas storage tank is provided with a pressure 闽, and the pressure is reached when the pressure in the gas storage tank reaches a certain limit. The valve opens the exhaust gas.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein an absorption tower for absorbing the substance to be blown off is disposed on the passage of the gas inner circulation device to reduce The inhibitory effect of harmful substances on anaerobic organisms in the reactor.

7. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein a cross-membrane differential pressure probe for monitoring a transmembrane pressure difference is provided on a system outlet pipe of the membrane module. .

8. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the anaerobic reactor is provided with a temperature, 0 RP and/or pH sensor to monitor the anaerobic The reaction environment of the reactor changes.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the membrane module is disposed outside the anaerobic reactor.

10. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 9, wherein Forming a liquid inner circulation passage between the anaerobic reactor and the membrane module, the liquid inner circulation passage including a liquid supply line connecting the upper portion of the anaerobic reactor and the upper portion of the membrane module, and the membrane a lower portion of the assembly and a liquid return line at a lower portion of the anaerobic reactor, wherein the liquid supply line is provided with a circulation pump, and the return liquid line is capable of anaerobic ammonium oxidizing bacteria or other substances trapped outside the membrane module The particulate matter is returned to the anaerobic reactor.

The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the membrane module is disposed in the anaerobic reactor.

12. The internal circulation aeration anaerobic ammonium oxidation-membrane bioreactor according to claim 1, wherein the anaerobic reactor is a fully mixed anaerobic reactor.