CN114804358B - Immersed membrane biological integrated reactor for oilfield produced water reaching standard and reinjecting ultra-low permeability layer and application - Google Patents
Immersed membrane biological integrated reactor for oilfield produced water reaching standard and reinjecting ultra-low permeability layer and application Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
An immersed membrane biological integrated reactor for oilfield produced water reaching the standard and reinjecting an ultra-low permeability layer and application thereof relate to an immersed membrane biological integrated reactor and application thereof. The invention aims to solve the problems that the degradation efficiency of organic matters is low and the quality of treated water does not reach the standard in the existing device for treating the recycled extremely low permeability layer produced water. The immersed membrane biological integrated reactor comprises a box body, wherein the inside of the box body is divided into a plurality of reaction chambers along the water flow direction by baffle plates, and the reaction chambers are a first anaerobic chamber, a second anaerobic chamber, a third anaerobic chamber, an anoxic chamber, a first aerobic chamber, a second aerobic chamber and an immersed membrane reaction chamber which are sequentially connected in series. An immersed membrane biological integrated reactor for oilfield produced water reaching the standard and reinjecting an ultra-low permeability layer is used for treating the reinjected ultra-low permeability layer produced water. The invention can obtain the immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer.
Description
Technical Field
The invention relates to an immersed membrane biological integrated reactor and application thereof.
Background
Very low penetrationThe permeability of the layer oil reservoir is low (average air permeability is less than or equal to 0.01 mu m) 2 ) The pore throat radius is small, and blockage is easy to occur in the water injection process, so that the water injection quality requirement is extremely strict. According to SY/T5329-2012 of the water injection quality recommendation index of clastic rock oil reservoirs, the ultra-low permeability layer is effectively developed, and the water quality of 5.1.1 is required to be ensured, namely the oil content is less than or equal to 5mg/L, the suspended solid content is less than or equal to 1mg/L, and the median value of the suspended solid particle size is less than or equal to 1 mu m after the treatment of the oily sewage.
At present, the domestic and foreign oily sewage treatment process has the advantages that the treated water quality needs to reach the index of '5.1.1' (the oil content is less than or equal to 5mg/L, the suspended solid content is less than or equal to 1mg/L, and the median value of the suspended solid particle size is less than or equal to 1 mu m), the conventional filtration technology cannot meet the requirements, and the membrane component filtration technology is adopted as terminal treatment. For domestic oil fields such as Daqing, the problems of membrane assembly pollution, fast membrane flux attenuation and the like in large-scale popularization and application are still the biggest obstacle for restricting the process operation stability and reaching the standard of '5.1.1' water quality.
"physical and chemical method+film" process: the membrane is difficult to regenerate after being polluted, the membrane flux is fast to drop, the replacement cost is high, the membrane flux is fast to drop, besides the defects of the membrane filtration process, the physical and chemical method mainly cannot degrade or intercept macromolecular organic matters at the front end of the membrane, the fluctuation of the oil content and suspended solid content in the treated water is large, the content is high, the pollution load of a membrane filtration system is too high, and the quality of the effluent cannot reach the standard stably. Meanwhile, in order to ensure the stable operation of the membrane filtration system, the water flux can only be maintained at 30% -60% of the design flux, and the chemical cleaning period is short, the cross-flow circulating water quantity is large, and the pollution discharge quantity is large. Overall, the "5.1.1" process flow is inefficient.
In the treatment of oilfield produced water, a single aerobic biochemical process has low degradation efficiency on organic matters.
Disclosure of Invention
The invention aims to solve the problems that the existing device is low in organic matter degradation efficiency and the quality of treated water is not up to standard in treating the reinjection ultra-low permeability layer produced water, and provides an immersed membrane biological integrated reactor for the oilfield produced water up to standard reinjection ultra-low permeability layer and application.
The invention provides an immersed membrane biological integrated reactor, firstly, organic pollutants of produced water are subjected to multiphase multistage biological gradient degradation according to the selection of anaerobic current and aerobic treatment through a composite microbial reactor, and inorganic matters of the organic pollutants are fully adsorbed and trapped; finally, the water quality of the produced water meets the water quality index of reinjection water with trace oil content, suspended solid content of 0.4mg/L and suspended solid particle diameter median of 0.6 mu m by carrying out terminal advanced treatment on the water through an immersed membrane reaction chamber.
The immersed membrane biological integrated reactor comprises a box body, wherein the inside of the box body is divided into a plurality of reaction chambers along the water flow direction by baffle plates, the reaction chambers are sequentially connected in series, namely a first anaerobic chamber, a second anaerobic chamber, a third anaerobic chamber, an anoxic chamber, a first aerobic chamber and a second aerobic chamber, a water inlet is formed in the upper part of one side of the box body, which is close to the first anaerobic chamber, a return port is formed in the bottoms of the anoxic chamber and the first aerobic chamber, and air inlets are formed in the bottoms of the first aerobic chamber and the second aerobic chamber; the bottoms of all the reaction chambers are provided with mud phase outlets communicated with a mud discharge pipe, and the upper parts of all the reaction chambers are provided with oil phase outlets communicated with an oil discharge pipe; the inside of the box body is also provided with an immersed membrane reaction chamber which is communicated with the second aerobic chamber;
a partition board is arranged in the immersed membrane reaction chamber, and a first microporous membrane component and a second microporous membrane component are respectively arranged on two sides of the partition board; the first aeration system is arranged outside the first microporous membrane component, and the second aeration system is arranged outside the second microporous membrane component; the bottom of the first microporous membrane component is provided with a first solid-liquid separation system, and the bottom of the second microporous membrane component is provided with a second solid-liquid separation system;
the reflux pump, the sludge pump, the suction pump, the first fan, the vacuum pressure gauge, the liquid flowmeter and the gas flowmeter are arranged outside the immersed membrane reaction chamber, one end of the gas flowmeter is communicated with an air outlet of the first fan, and the other end of the gas flowmeter is respectively communicated with one ends of the third electric valve and the fourth electric valve; the other end of the third electric valve is communicated with the first aeration system, and the other end of the fourth electric valve is communicated with the second aeration system;
the water outlet end of the first microporous membrane component is communicated with one end of a first electric valve, the water outlet end of the second microporous membrane component is communicated with one end of a second electric valve, the other ends of the first electric valve and the second electric valve are connected in parallel, the second electric valve is communicated with a vacuum pressure gauge and a suction pump, and the other end of the suction pump is connected with a liquid flowmeter.
The immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer is used for treating the reinjected ultra-low permeability layer produced water, and specifically comprises the following steps of:
1. adding nutrition to the first nutrition factor adding device and the second nutrition factor adding device, opening a valve of a water inlet pipe, and sequentially treating the water extracted from the reinjection ultra-low permeability layer through a first anaerobic chamber, a second anaerobic chamber, a third anaerobic chamber, an anoxic chamber, a first aerobic chamber and a second aerobic chamber, and then entering an immersed membrane reaction chamber;
2. the reinjection ultra-low permeability layer produced water entering the immersed membrane reaction chamber is alternately treated through two periods, in the previous period, a first electric valve and a third electric valve in the immersed membrane reaction chamber are opened, a second electric valve and a fourth electric valve are closed, the reinjection ultra-low permeability layer produced water treated by the second aerobic chamber is filtered through a first microporous membrane component, and negative pressure generated by communication of a suction pump forms a driving force, so that a transmembrane pressure difference is obtained, and the produced water is externally conveyed after passing through the first microporous membrane component and the suction pump; in the stage, compressed air provided by a first fan is aerated into a first microporous membrane component through a first aeration system, active sludge mixed liquor in a reaction zone is forced to circulate, and an ascending flow is formed at the left side of a partition plate, and a descending flow is formed at the right side of the partition plate; the liquid on the right side of the partition plate passes through a second solid-liquid separation system in the descending process, and at the moment, the second solid-liquid separation system plays a role in drainage and mud sliding;
under the action of the first aeration system and the second solid-liquid separation system, introducing the mixed solution on the right side of the partition board to the left side of the partition board, and then blocking most of activated sludge in the activated sludge mixed solution when passing through the first solid-liquid separation system, retaining the activated sludge at the bottom of the reaction zone, and continuously rising clear liquid, and continuously carrying out forced circulation flow under the action of the first aeration system; in the previous period, the first solid-liquid separation system plays a role in solid-liquid separation from bottom to top, and the second solid-liquid separation system plays a role in drainage and slip, so that liquid is discharged from top to bottom; in the latter period, the first electric valve and the third electric valve are closed, the second electric valve and the fourth electric valve are opened, the liquid coming from the reaction zone is filtered by the second microporous membrane component, the negative pressure generated by the suction pump forms a driving force, thus a transmembrane pressure difference is obtained, the liquid coming from the reaction zone is conveyed outwards after passing through the second microporous membrane component and the suction pump, in this stage, the compressed air provided by the first fan is aerated into the right side of the partition board of the reaction zone through the second aeration system, the active sludge mixed liquid in the reaction zone is forced to circulate, an upward flow is formed on the right side of the partition board, a downward flow is formed on the left side of the partition board, and forced circulation flow is realized; in the latter period, the second solid-liquid separation system plays a role in solid-liquid separation, liquid is discharged from bottom to top, the first solid-liquid separation system plays a role in drainage and mud sliding, the liquid is discharged from top to bottom, the immersed membrane reaction chamber is in an aerobic state at any running time, water can be continuously discharged, and mud at the bottom of the immersed membrane reaction chamber is periodically discharged into the bottom of the first aerobic chamber through a perforated mud discharge pipe or directly discharged into established station mud.
The invention has the following advantages:
1. the first microporous membrane components and the second microporous membrane components on two sides of the partition board in the immersed membrane reaction chamber can alternately operate through the PLC control system, water flow is forced to circulate under the action of the first aeration system and the second aeration system, and the chemical cleaning period of the membrane components and the service life of the membrane components are greatly prolonged; the integral membrane filtration system can continuously feed and discharge water, so that the management of an industrial production station is facilitated; the intermittent operation mode adopted by the suction pump of the traditional immersed membrane bioreactor for prolonging the operation period and slowing down the membrane pollution is overcome;
2. the first and second aeration systems are arranged outside the first and second microporous membrane components, and compared with the traditional aeration systems, the invention has the advantages that: firstly, the deposition of pollutants on the surface of a membrane component is slowed down by direct scouring and blowing-off of bubbles; secondly, the concentration of solute tends to be more uniform through disturbance generated by the aeration belly membrane component, so that the resistance generated by concentration polarization in the areas near the two sides of the membrane component is greatly weakened; by arranging aeration systems at two sides of the membrane component, the rising of the transmembrane pressure difference is slowed down under constant flux, and the chemical cleaning period and the running time of the membrane component are prolonged;
3. the first solid-liquid separation system and the second solid-liquid separation system of the solid-liquid separation system are arranged at the lower parts of the membrane component and the aeration system, the structure is simple, and the functions of drainage and mud sliding can be achieved according to different hydraulic flow states in the forced circulation process; but also has the function of solid-liquid separation; in the forced circulation process, the concentrated activated sludge mixed liquid intercepted by the membrane component can be fully subjected to solid-liquid separation, and most of activated sludge is blocked and deposited at the bottom of the reaction zone; the solid-liquid separation system greatly slows down the deposition of organic pollutants, inorganic matters and biological flocs on a mud cake layer and a gel layer on the surface of the membrane component and the blockage of membrane holes; and the rise of the transmembrane pressure difference is slowed down under the constant flux, and the chemical cleaning period and the running time of the membrane component are prolonged.
4. The immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer is used for treating the reinjected produced water of the ultra-low permeability layer, and the quality of the treated produced water meets the water quality index of the reinjected water with trace oil content, 0.4mg/L suspended solid content and 0.6 mu m suspended solid particle diameter median.
The invention can obtain the immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer.
Drawings
FIG. 1 is a schematic diagram of an immersed membrane bio-integrated reactor for the standard-reaching reinjection of oilfield produced water into an ultra-low permeability layer;
FIG. 2 is a flow pattern change diagram of an immersed membrane biological integrated reactor for achieving standard reinjection of oilfield produced water into an ultra-low permeability layer in accordance with the present invention;
FIG. 3 is a schematic structural view of an immersed membrane reactor;
fig. 4 is a schematic diagram of a solid-liquid separation system.
Detailed Description
The following examples further illustrate the invention but are not to be construed as limiting the invention. Modifications and substitutions to methods, procedures, or conditions of the present invention without departing from the spirit of the invention are intended to be within the scope of the present invention.
The first embodiment is as follows: the immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer comprises a box body, wherein the inside of the box body is divided into a plurality of reaction chambers along the water flow direction by baffle plates, the reaction chambers are a first anaerobic chamber 4, a second anaerobic chamber 5, a third anaerobic chamber 6, an anoxic chamber 7, a first aerobic chamber 8 and a second aerobic chamber 9 which are sequentially connected in series, a water inlet is arranged at the upper part of one side of the box body, which is close to the first anaerobic chamber 4, return ports are arranged at the bottoms of the anoxic chamber 7 and the first aerobic chamber 8, and air inlets are arranged at the bottoms of the first aerobic chamber 8 and the second aerobic chamber 9; the bottoms of all the reaction chambers are provided with mud phase outlets communicated with a mud discharge pipe, and the upper parts of all the reaction chambers are provided with oil phase outlets communicated with an oil discharge pipe; the inside of the box body is also provided with an immersed membrane reaction chamber 10, and the immersed membrane reaction chamber 10 is communicated with a second aerobic chamber 9;
a partition board 10-9 is arranged in the immersed membrane reaction chamber 10, and two sides of the partition board 10-9 are respectively provided with a first microporous membrane component M 1 And a second microporous membrane module M 2 The method comprises the steps of carrying out a first treatment on the surface of the First microporous membrane module M 1 The outside is provided with a first aeration system P1 and a second microporous membrane component M 2 The outside is provided with a second aeration system P2; first microporous membrane module M 1 A first solid-liquid separation system G1 and a second microporous membrane component M are arranged at the bottom part of the reactor 2 The bottom of the reactor is provided with a second solid-liquid separation system G2;
the reflux pump 10-1, the sludge pump 10-2, the suction pump 10-3, the first fan 10-4, the vacuum pressure gauge 10-5, the liquid flowmeter 10-6 and the gas flowmeter 10-7 are arranged outside the immersed membrane reaction chamber 10, one end of the gas flowmeter 10-7 is communicated with an air outlet of the first fan 10-4, and the other end is respectively communicated with one ends of the third electric valve D3 and the fourth electric valve D4; the other end of the third electric valve D3 is communicated with the first aeration system P1, and the other end of the fourth electric valve D4 is communicated with the second aeration system P2;
first microporous membrane module M 1 The water outlet end of the second microporous membrane component M is communicated with one end of the first electric valve D1 2 The water outlet end of the vacuum pump is communicated with one end of a second electric valve D2, the other ends of the first electric valve D1 and the second electric valve D2 are connected in parallel and are communicated with a vacuum pressure gauge 10-5 and a suction pump 10-3, and the other end of the suction pump 10-3 is connected with a liquid flowmeter 10-6.
The second embodiment is as follows: the present embodiment differs from the specific embodiment in that: the first solid-liquid separation system G1 and the second solid-liquid separation system G2 have the same structure; the structure of the first solid-liquid separation system G1 and the second solid-liquid separation system G2 consists of two layers of a plurality of angle steels which are staggered and uniformly distributed up and down, a gap is reserved between two adjacent angle steels, and the flow velocity of the gap is less than or equal to 2m/h; the included angle of the angle steel is 90-120 degrees, and both ends of the angle steel are connected with the inner wall of the immersed membrane reaction chamber 10. The other steps are the same as in the first embodiment.
And a third specific embodiment: this embodiment differs from the first or second embodiment in that: the second fan 3 arranged outside the box body is communicated with aeration pipes at the bottoms of the first aerobic chamber 8 and the second aerobic chamber 9. The other steps are the same as those of the first or second embodiment.
The specific embodiment IV is as follows: one difference between this embodiment and the first to third embodiments is that: the first nutrition factor adding device 1 and the second nutrition factor adding device 2 are arranged outside the box body, and the first nutrition factor adding device 1 is communicated with the anoxic chamber 7 through a return port at the bottom of the anoxic chamber 7; the second nutrient factor adding device 2 is communicated with the water inlet pipe, and then is communicated with the second nutrient factor adding device 2 through a water inlet at the upper part of the first anaerobic chamber 4. The other steps are the same as those of the first to third embodiments.
Fifth embodiment: one to four differences between the present embodiment and the specific embodiment are: the reflux horn mouth 10-8 at the upper part of the immersed membrane reaction chamber 10 is communicated with the anoxic chamber 7 through a reflux mouth at the bottom of the reflux pump 10-1 and the anoxic chamber 7. Other steps are the same as those of the first to fourth embodiments.
Specific embodiment six: the present embodiment differs from the first to fifth embodiments in that: the bottom of the immersed membrane reaction chamber 10 is provided with a perforated mud discharging pipe 10-10, and the perforated mud discharging pipe 10-10 is communicated with the first aerobic chamber 8 through a mud discharging pump 10-2 and a return port at the bottom of the first aerobic chamber 8. Other steps are the same as those of the first to fifth embodiments.
Seventh embodiment: the embodiment is an immersed membrane biological integrated reactor for reaching the standard and reinjecting the oilfield produced water into an extremely low permeability layer, which is used for treating the reinjected the produced water into the extremely low permeability layer, and specifically comprises the following steps:
1. adding nutrition to the first nutrition factor adding device 1 and the second nutrition factor adding device 2, opening a valve of a water inlet pipe, and processing the water extracted from the reinjection ultra-low permeability layer sequentially through a first anaerobic chamber 4, a second anaerobic chamber 5, a third anaerobic chamber 6, an anoxic chamber 7, a first aerobic chamber 8 and a second aerobic chamber 9, and then entering an immersed membrane reaction chamber 10;
2. the reinjection ultra-low permeability layer produced water entering the immersed membrane reaction chamber 10 is alternately treated by two periods, in the former period, a first electric valve D1 and a third electric valve D3 in the immersed membrane reaction chamber 10 are opened, a second electric valve D2 and a fourth electric valve D4 are closed, and the reinjection ultra-low permeability layer produced water treated by the second aerobic chamber 9 passes through the first microporous membrane component M 1 Filtering, forming driving force by negative pressure generated by the connection of the suction pump 10-3, thereby obtaining transmembrane pressure difference and leading the produced water to pass through the first microporous membrane component M 1 And suction pump 10-3 for later delivery; at this stage, the compressed air supplied from the first fan 10-4 is directed to the first microporous membrane module M through the first aeration system P1 1 Internal aeration, wherein the active sludge mixed liquor in the reaction zone is forced to circulate, and an upward flow is formed on the left side of the partition board 10-9, and a downward flow is formed on the right side; the liquid on the right side of the partition board 10-9 passes through the second solid-liquid separation system G2 in the descending process, and at the moment, the second solid-liquid separation system G2 plays a role in drainage and mud sliding;
under the action of the first aeration system P1 and the second solid-liquid separation system G2, introducing the mixed solution on the right side of the partition board 10-9 to the left side of the partition board 10-9, and blocking most of the activated sludge in the activated sludge mixed solution when the mixed solution passes through the first solid-liquid separation system G1, so that most of the activated sludge stays at the bottom of a reaction zone, and the clear solution continuously rises and continuously flows in a forced circulation way under the action of the first aeration system P1; in the previous period, the first solid-liquid separation system G1 plays a role in solid-liquid separation from bottom to top, and the second solid-liquid separation system G2 plays a role in drainage and mud sliding from top to bottom; in the latter period, the first electric valve D1 and the third electric valve D3 are closed, the second electric valve D2 and the fourth electric valve D4 are opened, and the liquid from the reaction zone passes through the second microporous membrane component M 2 Filtering, forming driving force by negative pressure generated by the suction pump 10-3, thereby obtaining transmembrane pressure difference, and leading the incoming liquid to pass through the second microporous membrane component M 2 And the suction pump 10-3, in this stage, the compressed air provided by the first fan 10-4 is aerated into the right side of the partition board 10-9 of the reaction zone through the second aeration system P2, the activated sludge mixed liquor in the reaction zone is forced to circulate, and an ascending flow is formed on the right side of the partition board 10-9, a descending flow is formed on the left side, and forced circulation flow is formed; in the latter period, the second solid-liquid separation system G2 plays a role in solid-liquid separation from bottom to top, the first solid-liquid separation system G1 plays a role in drainage and mud sliding from top to bottom, the immersed membrane reaction chamber 10 is in an aerobic state at any running time and can continuously discharge water, and mud at the bottom of the immersed membrane reaction chamber 10 is periodically discharged into the bottom of the first aerobic chamber 8 or directly discharged into established sludge through the perforated mud discharge pipe 10-10.
Eighth embodiment: the present embodiment differs from the seventh embodiment in that: the hydraulic retention time in the immersed membrane reaction chamber 10 is 2-4 h, and the first microporous membrane component M 1 And a second microporous membrane module M 2 The cycle of the bottoming operation is 2-4 hours; the ratio of aeration gas to water is 20:1-30:1. The other steps are the same as in embodiment seven.
Detailed description nine: the present embodiment differs from the seventh to eighth embodiments in that: the first nutritional factor is administeredThe dosing point of the dosing device 1 is the total water inlet of the integrated reactor, and the nutrition in the first nutrition factor dosing device 1 is glucose, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 Wherein the glucose adding concentration is 50 mg/L-100 mg/L, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 According to COD: NH (NH) 4 + ：SO 4 2- : p=200:6:50:1 concentration ratio; the nutrition in the second nutrition factor adding device 2 is KNO 3 The nutrition adding point in the second nutrition factor adding device 2 is the bottom of the downward flow area at the front end of the anoxic chamber 7, KNO 3 According to the addition amount of the oxygen-deficient chamber 7, COD to NO in water 3 - Concentration ratio of 200:40; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the first anaerobic chamber 4 are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 30-35%; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the second anaerobic chamber 5 are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 35-40%; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the third anaerobic chamber 6 are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 45-50%; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the anoxic chamber 7 are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 50-55%; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the first aerobic chamber 8 are as follows: the hydraulic retention time is 3-6 h, the upward flow area is filled with filler, the gas-liquid ratio is 10:1-15:1, and the reflux ratio is 50% -100%; in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the second aerobic chamber 9 are as follows: the hydraulic retention time is 3-6 h, the upward flow area is filled with filler, and the gas-liquid ratio is 10:1-15:1. The other steps are the same as those of the seventh to eighth embodiments.
Glucose in the first nutrient factor adding device 1 and organic matters existing in the produced water are taken as microorganism co-metabolism substrates, so that microorganisms grow rapidly in a starting stage, and the starting period is shortened. KH (KH) 2 PO 4 Is used for neutralizing calcium ions in produced water to form calcium phosphate precipitate.
Detailed description ten: the present embodiment differs from the seventh to ninth embodiments in that: first microporous membrane module M 1 And a second microporous membrane module M 2 All are hollow fiber membrane components; the filtering precision is 30 nm-50 nm. The other steps are the same as those of the embodiments seven to nine.
The following examples are used to verify the benefits of the present invention:
example 1: the immersed membrane biological integrated reactor comprises a box body, wherein the inside of the box body is divided into a plurality of reaction chambers along the water flow direction by baffle plates, the reaction chambers are sequentially connected in series, namely a first anaerobic chamber 4, a second anaerobic chamber 5, a third anaerobic chamber 6, an anoxic chamber 7, a first aerobic chamber 8 and a second aerobic chamber 9, a water inlet is formed in the upper part of one side of the box body, which is close to the first anaerobic chamber 4, a backflow port is formed in the bottoms of the anoxic chamber 7 and the first aerobic chamber 8, and air inlets are formed in the bottoms of the first aerobic chamber 8 and the second aerobic chamber 9; the bottoms of all the reaction chambers are provided with mud phase outlets communicated with a mud discharge pipe, and the upper parts of all the reaction chambers are provided with oil phase outlets communicated with an oil discharge pipe; the inside of the box body is also provided with an immersed membrane reaction chamber 10, and the immersed membrane reaction chamber 10 is communicated with a second aerobic chamber 9;
a partition board 10-9 is arranged in the immersed membrane reaction chamber 10, and two sides of the partition board 10-9 are respectively provided with a first microporous membrane component M 1 And a second microporous membrane module M 2 The method comprises the steps of carrying out a first treatment on the surface of the First microporous membrane module M 1 The outside is provided with a first aeration system P1 and a second microporous membrane component M 2 The outside is provided with a second aeration system P2; first microporous membrane module M 1 A first solid-liquid separation system G1 and a second microporous membrane component M are arranged at the bottom part of the reactor 2 The bottom of the reactor is provided with a second solid-liquid separation system G2;
the reflux pump 10-1, the sludge pump 10-2, the suction pump 10-3, the first fan 10-4, the vacuum pressure gauge 10-5, the liquid flowmeter 10-6 and the gas flowmeter 10-7 are arranged outside the immersed membrane reaction chamber 10, one end of the gas flowmeter 10-7 is communicated with an air outlet of the first fan 10-4, and the other end is respectively communicated with one ends of the third electric valve D3 and the fourth electric valve D4; the other end of the third electric valve D3 is communicated with the first aeration system P1, and the other end of the fourth electric valve D4 is communicated with the second aeration system P2;
first microporous membrane module M 1 The water outlet end of the second microporous membrane component M is communicated with one end of the first electric valve D1 2 The water outlet end of the vacuum pump is communicated with one end of a second electric valve D2, the other ends of the first electric valve D1 and the second electric valve D2 are connected in parallel and are communicated with a vacuum pressure gauge 10-5 and a suction pump 10-3, and the other end of the suction pump 10-3 is connected with a liquid flowmeter 10-6.
The first solid-liquid separation system G1 and the second solid-liquid separation system G2 have the same structure; the structure of the first solid-liquid separation system G1 and the second solid-liquid separation system G2 consists of two layers of a plurality of angle steels which are staggered and uniformly distributed up and down, a gap is reserved between two adjacent angle steels, and the flow velocity of the gap is less than or equal to 2m/h; the included angle of the angle steel is 90 degrees, and both ends of the angle steel are connected with the inner wall of the immersed membrane reaction chamber 10;
the second fan 3 arranged outside the box body is communicated with aeration pipes at the bottoms of the first aerobic chamber 8 and the second aerobic chamber 9;
the first nutrition factor adding device 1 and the second nutrition factor adding device 2 are arranged outside the box body, and the first nutrition factor adding device 1 is communicated with the anoxic chamber 7 through a return port at the bottom of the anoxic chamber 7; the second nutrient factor adding device 2 is communicated with a water inlet pipe and then communicated with the second nutrient factor adding device 2 through a water inlet at the upper part of the first anaerobic chamber 4;
the reflux horn mouth 10-8 at the upper part of the immersed membrane reaction chamber 10 is communicated with the anoxic chamber 7 through a reflux mouth at the bottom of the reflux pump 10-1 and the anoxic chamber 7;
the bottom of the immersed membrane reaction chamber 10 is provided with a perforated mud discharging pipe 10-10, and the perforated mud discharging pipe 10-10 is communicated with the first aerobic chamber 8 through a mud discharging pump 10-2 and a return port at the bottom of the first aerobic chamber 8.
Example 2: the immersed membrane biological integrated reactor for achieving the standard reinjection of the oilfield produced water into the ultra-low permeability layer in the embodiment 1 is utilized to treat the reinjection of the produced water into the ultra-low permeability layer, and the method is specifically completed according to the following steps:
1. adding nutrition to the first nutrition factor adding device 1 and the second nutrition factor adding device 2, opening a valve of a water inlet pipe, and reinjecting the raw water of the ultra-low permeability layer to sequentially pass through a first anaerobic chamber 4, a second anaerobic chamber 5, a third anaerobic chamber 6, an anoxic chamber 7, a first aerobic chamber 8 and a second aerobic chamber 9 for treatment, and then entering an immersed membrane reaction chamber 10;
the oil content in raw water of the reinjection ultra-low permeability layer produced water in the first step is 0.3mg/L, the suspended solid content is 4.0mg/L, and the median value of the suspended solid particle size is 1.2 mu m; no submerged membrane reaction zone;
in the first step, the dosing point of the first nutrition factor dosing device 1 is the total water inlet position of the integrated reactor, and the nutrition in the first nutrition factor dosing device 1 is glucose, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 Wherein the glucose adding concentration is 50 mg/L-100 mg/L, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 According to COD: NH (NH) 4 + ：SO 4 2- : p=200:6:50:1 concentration ratio; the nutrition in the second nutrition factor adding device 2 is KNO 3 The nutrition adding point in the second nutrition factor adding device 2 is the bottom of the downward flow area at the front end of the anoxic chamber 7, KNO 3 According to the addition amount of the oxygen-deficient chamber 7, COD to NO in water 3 - Concentration ratio of 200:40;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the first anaerobic chamber 4 are as follows:
the hydraulic retention time is 3h, the flow speed of the upward flow area is 0.9m/h, the upward flow area is filled with suspended filler, and the filling rate is 30%;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the second anaerobic chamber 5 are as follows:
the hydraulic retention time is 3h, the flow speed of the upward flow area is 0.9m/h, the upward flow area is filled with suspended filler, and the filling rate is 35%;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the third anaerobic chamber 6 are as follows:
the hydraulic retention time is 3h, the flow speed of the upward flow area is 0.9m/h, the upward flow area is filled with suspended filler, and the filling rate is 45%;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the anoxic chamber 7 are as follows:
the hydraulic retention time is 3h, the flow speed of the upward flow area is 0.9m/h, the upward flow area is filled with suspended filler, and the filling rate is 50%;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the first aerobic chamber 8 are as follows:
the hydraulic retention time is 3h, the upward flow area is filled with filler, the gas-liquid ratio is 10:1, and the reflux ratio is 80%;
in the first step, the process parameters of reinjecting the produced water of the ultra-low permeability layer in the second aerobic chamber 9 are as follows: the hydraulic retention time is 3h, the upward flow area is filled with filler, and the gas-liquid ratio is 10:1;
2. the reinjection ultra-low permeability layer produced water entering the immersed membrane reaction chamber 10 is alternately treated by two periods, in the former period, a first electric valve D1 and a third electric valve D3 in the immersed membrane reaction chamber 10 are opened, a second electric valve D2 and a fourth electric valve D4 are closed, and the reinjection ultra-low permeability layer produced water treated by the second aerobic chamber 9 passes through the first microporous membrane component M 1 Filtering, forming driving force by negative pressure generated by the connection of the suction pump 10-3, thereby obtaining transmembrane pressure difference and leading the produced water to pass through the first microporous membrane component M 1 And suction pump 10-3 for later delivery; at this stage, the compressed air supplied from the first fan 10-4 is directed to the first microporous membrane module M through the first aeration system P1 1 Internal aeration, wherein the active sludge mixed liquor in the reaction zone is forced to circulate, and an upward flow is formed on the left side of the partition board 10-9, and a downward flow is formed on the right side; the liquid on the right side of the partition board 10-9 passes through the second solid-liquid separation system G2 in the descending process, and at the moment, the second solid-liquid separation system G2 plays a role in drainage and mud sliding;
under the action of the first aeration system P1 and the second solid-liquid separation system G2, introducing the mixed solution on the right side of the partition board 10-9 to the left side of the partition board 10-9, and blocking most of the activated sludge in the activated sludge mixed solution when the mixed solution passes through the first solid-liquid separation system G1, so that most of the activated sludge stays at the bottom of a reaction zone, and the clear solution continuously rises and continuously flows in a forced circulation way under the action of the first aeration system P1; in the previous period, the first solid-liquid separation system G1 plays a role in solid-liquid separation from bottom to top, and the second solid-liquid separation system G2 plays a role in drainage and mud sliding from top to bottom; in the latter period, the first electric valve D1 and the third electric valve D3 are closed, the second electric valve D2 and the fourth electric valve D4 are opened, and the liquid from the reaction zone passes through the second microporous membrane component M 2 Filtering, forming driving force by negative pressure generated by the suction pump 10-3, thereby obtaining transmembrane pressure difference, and leading the incoming liquid to pass through the second microporous membrane component M 2 And the suction pump 10-3, in this stage, the compressed air provided by the first fan 10-4 is aerated into the right side of the partition board 10-9 of the reaction zone through the second aeration system P2, the activated sludge mixed liquor in the reaction zone is forced to circulate, and an ascending flow is formed on the right side of the partition board 10-9, a descending flow is formed on the left side, and forced circulation flow is formed; in the latter period, the second solid-liquid separation system G2 plays a role in solid-liquid separation from bottom to top, the first solid-liquid separation system G1 plays a role in drainage and mud sliding from top to bottom, the immersed membrane reaction chamber 10 is in an aerobic state at any running time and can continuously discharge water, and mud at the bottom of the immersed membrane reaction chamber 10 is periodically discharged into the bottom of the first aerobic chamber 8 or directly discharged into established station mud through the perforated mud discharge pipe 10-10;
in the second step, the hydraulic retention time in the immersed membrane reaction chamber 10 is 4h, and the first microporous membrane component M 1 And a second microporous membrane module M 2 The cycle of the bottoming operation is 2 hours; the ratio of aeration gas to water is 20:1.
The trace of oil content in the effluent of example 2 was undetectable, the suspended solids content was 0.4mg/L, and the median particle size of the suspended solids was 0.6. Mu.m; the flux of the membrane operation is 90L/h.m 2 In the case of (a), the chemical cleaning period of the membrane component can reach 6About month, compared with the prior art, the chemical cleaning period is improved by more than 5 times on average.
Claims (9)
1. The immersed membrane biological integrated reactor comprises a box body, wherein the inside of the box body is divided into a plurality of reaction chambers along the water flow direction by baffle plates, the reaction chambers are sequentially connected in series, namely a first anaerobic chamber (4), a second anaerobic chamber (5), a third anaerobic chamber (6), an anoxic chamber (7), a first aerobic chamber (8) and a second aerobic chamber (9), a water inlet is formed in the upper part of one side, close to the first anaerobic chamber (4), of the box body, return ports are formed in the bottoms of the anoxic chamber (7) and the first aerobic chamber (8), and air inlets are formed in the bottoms of the first aerobic chamber (8) and the second aerobic chamber (9); all reaction chamber bottoms are equipped with the mud phase export that is linked together with the row mud pipe, and upper portion is equipped with the oil phase export that is linked together with row oil pipe, its characterized in that: an immersed membrane reaction chamber (10) is also arranged in the box body, and the immersed membrane reaction chamber (10) is communicated with a second aerobic chamber (9);
a partition board (10-9) is arranged in the immersed membrane reaction chamber (10), and first microporous membrane components (M) are respectively arranged at two sides of the partition board (10-9) 1 ) And a second microporous membrane module (M 2 ) The method comprises the steps of carrying out a first treatment on the surface of the First microporous membrane module (M) 1 ) The outside is provided with a first aeration system (P1), and a second microporous membrane component (M) 2 ) The outside is provided with a second aeration system (P2); first microporous membrane module (M) 1 ) A first solid-liquid separation system (G1) is arranged at the bottom of the reactor, and a second microporous membrane component (M 2 ) The bottom of the reactor is provided with a second solid-liquid separation system (G2);
the device comprises a reflux pump (10-1), a sludge discharge pump (10-2), a suction pump (10-3), a first fan (10-4), a vacuum pressure gauge (10-5), a liquid flowmeter (10-6) and a gas flowmeter (10-7), wherein the liquid flowmeter and the gas flowmeter (10-7) are arranged outside a submerged membrane reaction chamber (10), one end of the gas flowmeter (10-7) is communicated with an air outlet of the first fan (10-4), and the other end of the gas flowmeter is respectively communicated with one ends of a third electric valve (D3) and a fourth electric valve (D4); the other end of the third electric valve (D3) is communicated with the first aeration system (P1), and the other end of the fourth electric valve (D4) is communicated with the second aeration system (P2);
first microporous membrane module (M) 1 ) Is communicated with one end of a first electric valve (D1), and a second microporous membrane component (M 2 ) The water outlet end of the vacuum pump is communicated with one end of a second electric valve (D2), the other ends of the first electric valve (D1) and the second electric valve (D2) are connected in parallel and are communicated with a vacuum pressure gauge (10-5) and a suction pump (10-3), and the other end of the suction pump (10-3) is connected with a liquid flowmeter (10-6);
the first solid-liquid separation system (G1) and the second solid-liquid separation system (G2) have the same structure; the structure of the first solid-liquid separation system (G1) and the second solid-liquid separation system (G2) is composed of two layers of a plurality of angle steels which are uniformly distributed in an up-down staggered way, a gap is reserved between two adjacent angle steels, and the flow velocity of the gap is less than or equal to 2m/h; the included angle of the angle steel is 90-120 degrees, and both ends of the angle steel are connected with the inner wall of the immersed membrane reaction chamber (10).
2. The immersed membrane biological integrated reactor for the oil field produced water reaching the standard and reinjecting the ultra-low permeability layer according to the claim 1 is characterized in that a second fan (3) arranged outside the tank body is communicated with aeration pipes at the bottoms of the first aerobic chamber (8) and the second aerobic chamber (9).
3. The immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer is characterized in that a first nutrition factor adding device (1) and a second nutrition factor adding device (2) are arranged outside a tank body, and the first nutrition factor adding device (1) is communicated with an anoxic chamber (7) through a backflow port at the bottom of the anoxic chamber (7); the second nutrition factor adding device (2) is communicated with the water inlet pipe, and then is communicated with the first anaerobic chamber (4) through a water inlet at the upper part of the first anaerobic chamber (4).
4. The immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer according to claim 1 is characterized in that a backflow horn mouth (10-8) at the upper part of an immersed membrane reaction chamber (10) is communicated with a backflow port at the bottom of an anoxic chamber (7) through a backflow pump (10-1) and the anoxic chamber (7).
5. The immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer according to claim 1, wherein the bottom of the immersed membrane reaction chamber (10) is provided with a perforated mud discharging pipe (10-10), and the perforated mud discharging pipe (10-10) is communicated with the first aerobic chamber (8) through a mud discharging pump (10-2) and a return port at the bottom of the first aerobic chamber (8).
6. The use of an immersed membrane bio-integrated reactor for the up-to-standard reinjection of oilfield produced water into very low permeability layers according to claim 1, characterized in that the reactor is used for the treatment of oilfield produced water, in particular by the following steps:
1. nutrition is added to the first nutrition factor adding device (1) and the second nutrition factor adding device (2), a water inlet pipe valve is opened, oilfield produced water sequentially passes through the first anaerobic chamber (4), the second anaerobic chamber (5), the third anaerobic chamber (6), the anoxic chamber (7), the first aerobic chamber (8) and the second aerobic chamber (9) for treatment, and then enters the immersed membrane reaction chamber (10);
2. the oilfield produced water entering the immersed membrane reaction chamber (10) is alternately treated through two periods, in the former period, a first electric valve (D1) and a third electric valve (D3) in the immersed membrane reaction chamber (10) are opened, a second electric valve (D2) and a fourth electric valve (D4) are closed, and oilfield produced water treated through the second aerobic chamber (9) passes through a first microporous membrane component (M) 1 ) Filtering, forming driving force by negative pressure generated by communication of suction pump (10-3), thereby obtaining transmembrane pressure difference, and enabling oilfield produced water to pass through a first microporous membrane component (M 1 ) And the suction pump (10-3) is used for external transmission; at this stage, the compressed air supplied by the first fan (10-4) is directed to the first microporous membrane module (M) through the first aeration system (P1) 1 ) Internal aeration, wherein the activated sludge mixed solution in the reaction chamber is forced to circulate, and an upward flow is formed on the left side of the partition board (10-9), and a downward flow is formed on the right side; the liquid on the right side of the partition plate (10-9) passes through a second solid-liquid separation system (G2) in the descending process, and the second solid-liquid separation system (G2) plays a role in drainage and mud sliding;
in the first aeration system (P1) andunder the action of the second solid-liquid separation system (G2), the mixed liquid on the right side of the partition board (10-9) is introduced into the left side of the partition board (10-9), and most of activated sludge in the activated sludge mixed liquid is blocked and stays at the bottom of the reaction chamber when passing through the first solid-liquid separation system (G1), and clear liquid continuously rises and continuously flows in a forced circulation way under the action of the first aeration system (P1); in the previous period, the first solid-liquid separation system (G1) plays a role in solid-liquid separation from bottom to top, and the second solid-liquid separation system (G2) plays a role in drainage and mud sliding from top to bottom; in the latter period, the first electric valve (D1) and the third electric valve (D3) are closed, the second electric valve (D2) and the fourth electric valve (D4) are opened, and the liquid coming from the reaction chamber passes through the second microporous membrane component (M 2 ) Filtering, forming driving force by negative pressure generated by suction pump (10-3), thereby obtaining transmembrane pressure difference, and making the liquid pass through second microporous membrane component (M 2 ) And the suction pump (10-3) and then is conveyed outwards, in this stage, the compressed air provided by the first fan (10-4) is aerated into the right side of the reaction chamber partition board (10-9) through the second aeration system (P2), the activated sludge mixed liquor in the reaction chamber is forced to circulate, and an upward flow is formed on the right side of the partition board (10-9), a downward flow is formed on the left side of the partition board, and forced circulation flow is formed; in the latter period, the second solid-liquid separation system (G2) plays a role in solid-liquid separation, liquid is discharged from bottom to top, the first solid-liquid separation system (G1) plays a role in drainage and mud sliding, liquid is discharged from top to bottom, the immersed membrane reaction chamber (10) is in an aerobic state at any running time, water is continuously discharged, and sludge at the bottom of the immersed membrane reaction chamber (10) is periodically discharged into the bottom of the first aerobic chamber (8) through a perforated mud discharge pipe (10-10) or directly discharged into sludge at a built station.
7. The use of an immersed membrane bio-integrated reactor for the up-to-standard reinjection of oilfield produced water into very low permeability layers according to claim 6, characterized in that the hydraulic residence time in the immersed membrane reaction chamber (10) is 2-4 hours, the first microporous membrane module (M 1 ) And a second microporous membrane module (M 2 ) The period of alternate running is 2-4 h; the ratio of aeration gas to water is 20:1-30:1.
8. The application of the immersed membrane biological integrated reactor for the oilfield produced water reaching the standard and reinjecting the ultra-low permeability layer as claimed in claim 6, wherein the dosing point of the second nutrition factor dosing device (2) is the total water inlet of the integrated reactor, and the nutrition in the second nutrition factor dosing device (2) is glucose, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 Wherein the glucose adding concentration is 50 mg/L-100 mg/L, (NH) 4 ) 2 SO 4 、Na 2 SO 4 And KH 2 PO 4 According to COD: NH (NH) 4 + ：SO 4 2- : p=200:6:50:1 concentration ratio; the nutrition in the first nutrition factor adding device (1) is KNO 3 The nutrition adding point in the first nutrition factor adding device (1) is the bottom of the downward flow area at the front end of the anoxic chamber (7), KNO 3 According to the addition amount of COD to NO in water coming from the anoxic chamber (7) 3 - Concentration ratio of 200:40; in the first step, the technological parameters of the oilfield produced water in the first anaerobic chamber (4) are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 30-35%; in the first step, the technological parameters of the oilfield produced water in the second anaerobic chamber (5) are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 35-40%; in the first step, the technological parameters of the oilfield produced water in the third anaerobic chamber (6) are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 45-50%; in the first step, the technological parameters of the oilfield produced water in the anoxic chamber (7) are as follows: the hydraulic retention time is 3-6 h, the flow speed of the upward flow area is 0.6-2.0 m/h, the upward flow area is filled with suspended filler, and the filling rate is 50-55%; in the first step, the technological parameters of the oilfield produced water in the first aerobic chamber (8) are as follows: the hydraulic retention time is 3-6 h, the upward flow area is filled with filler, the gas-liquid ratio is 10:1-15:1, and the reflux ratio is 50% -100%; in the first step, the technological parameters of the oilfield produced water in the second aerobic chamber (9) are as follows: hydraulic powerThe residence time is 3-6 h, the upward flow area is filled with filler, and the gas-liquid ratio is 10:1-15:1.
9. Use of an immersed membrane bio-integrated reactor for the standard-reaching reinjection of oilfield produced water into very low permeability layers according to claim 6, characterized in that the first microporous membrane module (M 1 ) And a second microporous membrane module (M 2 ) All are hollow fiber membrane components; the filtering precision is 30 nm-50 nm.
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