CN216890548U - Flowing back advanced treatment recycling system is returned in oil field fracturing - Google Patents
Flowing back advanced treatment recycling system is returned in oil field fracturing Download PDFInfo
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- CN216890548U CN216890548U CN202220537030.6U CN202220537030U CN216890548U CN 216890548 U CN216890548 U CN 216890548U CN 202220537030 U CN202220537030 U CN 202220537030U CN 216890548 U CN216890548 U CN 216890548U
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Abstract
The utility model relates to the technical field of recovery treatment of oilfield fracturing flowback fluid, and provides a deep treatment and recycling system of oilfield fracturing flowback fluid, which comprises an adjusting tank, a three-phase separator, a primary catalytic Fenton tower, a primary cavitation air flotation machine, a secondary dissolved air flotation machine, an A/O biochemical reaction tank, an MBR membrane tank, a secondary catalytic Fenton tower, a filter tank and an ultrafiltration device which are sequentially connected in series; in addition, the device also comprises a reverse osmosis device communicated with the ultrafiltration device, when the conductivity of the outlet water is not required, the outlet water of the ultrafiltration device is directly discharged or recycled, and when the conductivity of the outlet water is required, the reverse osmosis device is adopted to further reduce the conductivity of the outlet water. The system provided by the utility model has the advantages of good oil removal effect, stable effluent quality, capability of meeting the discharge and reuse standards, less sludge amount, low treatment cost and wide application prospect in deep treatment of the fracturing flow-back fluid of the oil field.
Description
Technical Field
The utility model discloses oil field fracturing returns flowing back recovery processing technology field especially relates to an oil field fracturing returns flowing back deep treatment recycling system.
Background
The oil field fracturing flow-back fluid has the characteristics of high viscosity, large oil content, high COD (chemical oxygen demand), high suspended matter content and the like, and the conventional treatment process comprises chemical oxidation, flocculation precipitation, electrolytic oxidation, filtration, chemical oxidation, flocculation magnetic separation, filtration and the like, wherein in the electrolytic oxidation process, the electrodes need to be replaced frequently due to the fact that the electrodes are prone to passivation, scaling and the like, and the system stability is poor. The latter separator can shorten the settling time, but still has the problems of substandard treatment and the like.
Chemical oxidation, flocculation precipitation and filtration are the most widely applied main flow processes in the current market, but the method has poor oil removal effect, the effluent still contains a large amount of boron ions, the filter is often blocked, the effluent quality is unstable, the discharge and reuse standards are not met, and a large amount of waste of water resources is caused.
SUMMERY OF THE UTILITY MODEL
In view of the above, the utility model provides a deep treatment and recycling system for oil field fracturing flow-back fluid. The system provided by the utility model has the advantages of good oil removing effect, stable effluent quality, less sludge amount and low treatment cost, and meets the discharge and reuse standards.
In order to achieve the purpose of the utility model, the utility model provides the following technical scheme:
the utility model provides an oil field fracturing flow-back fluid deep treatment recycling system, includes:
a regulating tank 1;
a three-phase separator 2 with an inlet communicated with an outlet of the regulating tank 1;
a first-stage catalytic Fenton tower 3 with an inlet communicated with an outlet of the three-phase separator 2;
a first-stage cavitation air flotation machine 4 with an inlet communicated with an outlet of the first-stage catalytic Fenton tower 3;
a second-stage dissolved air flotation machine 5 with an inlet communicated with an outlet of the first-stage cavitation air flotation machine 4;
an A/O biochemical reaction tank 6 with an inlet communicated with an outlet of the secondary dissolved air flotation machine 5;
an MBR membrane tank 7 with an inlet communicated with the outlet of the A/O biochemical reaction tank 6;
a secondary catalytic Fenton tower 8 with an inlet communicated with an outlet of the MBR membrane tank 7;
the inlet of the filter 9 is communicated with the outlet of the secondary catalytic Fenton tower 8;
an ultrafiltration device 10 with an inlet communicated with the outlet of the filter chamber 9.
Preferably, the system further comprises a reverse osmosis unit 11 having an inlet in communication with an outlet of the ultrafiltration unit 10.
Preferably, a flow divider and an oil baffle are arranged in the three-phase separator 2.
Preferably, the ultrafiltration membrane in the ultrafiltration device 10 is a polyvinylidene fluoride membrane.
Preferably, the ultrafiltration membrane has the molecular weight cutoff of 1000-500000 daltons.
Preferably, the primary cavitation air flotation machine 4, the secondary dissolved air flotation machine 5 and the filter 9 are all provided with a dosing system in a matching way.
Preferably, the reverse osmosis device 11 is provided with a concentrated water outlet and a clear water outlet; and the concentrated water outlet is communicated with the inlet of the first-stage catalytic Fenton tower 3.
Preferably, the filter 9 is a cloth filter.
The utility model provides a deep treatment and recycling system for oilfield fracturing flowback fluid, which comprises an adjusting tank 1, a three-phase separator 2, a primary catalytic Fenton tower 3, a primary cavitation air flotation machine 4, a secondary dissolved air flotation machine 5, an A/O biochemical reaction tank 6, an MBR membrane tank 7, a secondary catalytic Fenton tower 8, a filter tank 9, an ultrafiltration device 10 and a reverse osmosis device 11 which are sequentially connected in series. According to the utility model, the characteristics of complex pollutant components, high viscosity, high oil content, high suspended matter content, high polymer content and the like of the oilfield fracturing flowback fluid are fully considered, the oil contained in the wastewater is removed by using the three-phase separator 2, no agent is required to be added in the oil removing process, and the COD in the wastewater is greatly reduced by using the primary catalytic Fenton tower 3 and the secondary catalytic Fenton tower 8; removing suspended matters and other impurities in the wastewater by using a primary concave vortex air flotation machine 4 and a secondary dissolved air flotation machine 5; organic pollutants in the wastewater are removed by utilizing the degradation of microorganisms in the A/O biochemical reaction tank 6; sludge in the biochemical reaction is filtered by an MBR membrane tank 7 to realize sludge-water separation; removing solid matters and organic matters in the water by using a filter 9; the ultrafiltration device 10 is used to remove colloids, bacteria, macromolecular substances, etc. from water. In the utility model, the ultrafiltration effluent can meet the first class A standard of pollutant discharge standard of urban sewage treatment plants.
In addition, the utility model adopts the catalytic Fenton tower, and compared with the traditional Fenton method, the catalytic Fenton tower combines the in-phase chemical oxidation (Fenton method) and the heterogeneous chemical oxidation (H)2O2The novel technology with the functions of FeOOH), fluidized bed crystallization, FeOOH reduction and dissolution and the like can reduce iron salt and H2O2The dosage of the sludge treatment agent reduces the generation amount of the sludge and greatly reduces the process operation cost.
Further, the system provided by the utility model also comprises a reverse osmosis device 11, the inlet of which is communicated with the outlet of the ultrafiltration device 10, and the ultrafiltration effluent is desalted and concentrated through the reverse osmosis device 11 to obtain effluent meeting the recycling or discharge standard. In the specific embodiment of the utility model, water sources with different conductivities can be obtained according to different requirements of users on effluent, if the conductivity is not reduced, the ultrafiltration effluent can meet the recycling requirement, and when the conductivity of the produced water is required, the reverse osmosis effluent can be used to meet the recycling or discharge standard.
In conclusion, the system provided by the utility model has the advantages of good oil removal effect, stable effluent quality, capability of meeting the discharge and reuse standards, less sludge amount, low treatment cost and wide application prospect in the aspect of deep treatment of fracturing flow-back fluid of an oil field.
Drawings
Fig. 1 is a schematic structural diagram of a deep treatment and recycling system for oil field fracturing flow-back fluid provided by the utility model, wherein in fig. 1: 1-regulating tank, 2-three-phase separator, 3-catalytic Fenton tower, 4-first stage cavitation air flotation machine, 5-second stage dissolved air flotation machine, 6-A/O biochemical reaction tank, 7-MBR membrane tank, 8-second stage catalytic Fenton tower, 9-filter tank, 10-ultrafiltration device and 11-reverse osmosis device.
Detailed Description
The utility model provides a deep treatment and recycling system for oil field fracturing flow-back fluid, which comprises:
a regulating tank 1;
a three-phase separator 2 with an inlet communicated with an outlet of the regulating tank 1;
a first-stage catalytic Fenton tower 3 with an inlet communicated with an outlet of the three-phase separator 2;
a first-stage cavitation air flotation machine 4 with an inlet communicated with an outlet of the first-stage catalytic Fenton tower 3;
a second-stage dissolved air flotation machine 5 with an inlet communicated with an outlet of the first-stage cavitation air flotation machine 4;
an A/O biochemical reaction tank 6 with an inlet communicated with the outlet of the secondary dissolved air flotation machine 5;
an MBR membrane tank 7 with an inlet communicated with the outlet of the A/O biochemical reaction tank 6;
a secondary catalytic Fenton tower 8 with an inlet communicated with an outlet of the MBR membrane tank 7;
the inlet of the filter 9 is communicated with the outlet of the secondary catalytic Fenton tower 8;
an ultrafiltration device 10 with an inlet communicated with the outlet of the filter chamber 9.
The structural schematic diagram of the oil field fracturing flow-back fluid deep treatment recycling system provided by the utility model is shown in fig. 1, and the following description is given in detail by combining fig. 1.
The system provided by the utility model comprises a regulating reservoir 1. The utility model has no special requirements on the regulating tank 1, and the regulating tank which is well known by the technical personnel in the field can be adopted; in the utility model, the oilfield fracturing flow-back fluid is preferably discharged into the adjusting tank 1 to balance the water quantity, and large-particle solids such as silt carried by the oilfield fracturing flow-back fluid are removed through gravity settling.
The system provided by the utility model comprises a three-phase separator 2, the inlet of which is communicated with the outlet of the regulating reservoir 1. In the present invention, a flow divider and an oil baffle are preferably provided in the three-phase separator 2; the oil baffle plate divides the interior of the three-phase separator into a water pool and an oil pool; after the oil field fracturing flow-back fluid enters the three-phase separator, gas-liquid separation is realized through the flow divider, then oil overflows to the oil pool from the oil baffle plate, water is left in the water pool, solid particles are precipitated at the bottom of the water pool, so that gas-liquid-solid three-phase separation is realized, a water outlet valve is arranged in the water pool, and supernatant in the water pool is discharged from the water outlet valve.
The system provided by the utility model comprises a primary catalytic Fenton tower 3, the inlet of which is communicated with the outlet of the three-phase separator 2. The utility model has no special requirements on the specific structure of the first-stage catalytic Fenton tower, and the catalytic Fenton tower which is well known to a person skilled in the art can be adopted. In a specific embodiment of the utility model, the catalytic Fenton tower is provided with a ferrite and hydrogen peroxide adding device, and Fe is utilized2+The oxidation with hydrogen peroxide degrades organic compounds, and the removal rate of COD can reach about 90%. According to the utility model, the catalytic Fenton tower is adopted, so that the dosage of the traditional Fenton method can be greatly reduced, the chemical sludge yield is reduced, iron oxide can be formed on the surface of the carrier in the oxidation reaction process, the iron oxide has a heterogeneous catalysis effect, and the removal rate of COD can be further improved.
The system provided by the utility model comprises a primary cavitation air flotation machine 4, the inlet of which is communicated with the outlet of the primary catalytic Fenton tower 3. The utility model has no special requirements on the specific structure of the primary cavitation air flotation machine 4, and the cavitation air flotation machine which is well known by the technical personnel in the field can be adopted. In the utility model, the primary cavitation air flotation machine 4 preferably comprises a box body, an aerator and a mud scraping system, and the primary cavitation air flotation machine 4 is preferably also provided with a dosing system in a matching way, and is used for adding a coagulant and a flocculant into the primary cavitation air flotation machine 4 and reducing organic matters in water by matching with coagulation and flocculation reactions; the flocculant is preferably PAM (polyacrylamide) and the coagulant is preferably PAC (polyaluminium chloride). In the specific embodiment of the utility model, the effluent of the first-stage catalytic Fenton tower 3 enters a first-stage cavitation air flotation machine 4, bubbles are directly injected into the water by an aeration machine, PAC and PAM are added to convert most of soluble organic matters into non-soluble substances, and then the bubbles are used for removing suspended matters in the wastewater to the water surface, so that solid-liquid separation is realized; the diameter of the bubbles generated in the primary cavitation air flotation machine 4 is 30-50 μm.
The system provided by the utility model comprises a secondary dissolved air flotation machine 5, the inlet of which is communicated with the outlet of the primary cavitation air flotation machine 4. The utility model has no special requirements on the specific structure of the dissolved air flotation machine 5, and the dissolved air flotation machine known by the technical personnel in the field can be adopted. In the specific embodiment of the utility model, the secondary dissolved air flotation machine 5 is further provided with a dosing system in a matching manner, and is used for adding a coagulant and a flocculant into the secondary dissolved air flotation machine 5 to reduce organic matters in water by matching with coagulation and flocculation reactions; the flocculant is preferably PAM and the coagulant is preferably PAC. After the effluent of the primary cavitation air flotation machine 4 enters a secondary dissolved air flotation machine 5, a large amount of bubbles are generated in the water through an dissolved air system, PAC and PAM are added to convert most of soluble organic matters into non-soluble substances, suspended matters with the density similar to that of the water are adsorbed by the bubbles and rise to the water surface by virtue of buoyancy, and solid-liquid separation is realized; the diameter of bubbles generated in the secondary dissolved air floatation machine is 30-50 mu m.
The system provided by the utility model comprises an A/O biochemical reaction tank 6, the inlet of which is communicated with the outlet of the secondary dissolved air flotation machine 5. The utility model has no special requirements on the specific structure of the A/O biochemical reaction tank 6, and the A/O biochemical reaction tank which is well known by the technicians in the field is adopted; an anaerobic section and an aerobic section are preferably arranged in the A/O biochemical reaction tank 6, the effluent of the secondary dissolved air floatation machine 5 enters the A/O biochemical reaction tank 6 for biochemical reaction (including nitration reaction and denitrification reaction), organic matters in water are removed, and the A/O biochemical reaction tank has the functions of nitrogen and phosphorus removal.
The system provided by the utility model comprises an MBR membrane tank 7 with an inlet communicated with the outlet of the A/O biochemical reaction tank 6. The utility model has no special requirements on the specific structure of the MBR membrane tank 7, and can adopt the MBR membrane tank which is well known to the technical personnel in the field. In the specific embodiment of the utility model, the effluent of the A/O biochemical reaction tank 6 is discharged into an MBR membrane tank 7, and sludge produced in the biochemical reaction is filtered by using an MBR membrane component to realize sludge-water separation.
The system provided by the utility model comprises a secondary catalytic Fenton tower 8, the inlet of which is communicated with the outlet of the MBR membrane tank 7. In the utility model, the structure of the secondary catalytic Fenton tower 8 is consistent with that of the primary catalytic Fenton tower 3, and the description is omitted; the effluent of the MBR membrane tank 7 enters a secondary catalytic Fenton tower 8 and is treated by Fe2+And oxidizing the organic matters again under the action of hydrogen peroxide.
The system provided by the utility model comprises a filter tank 9 with an inlet communicated with the outlet of the secondary catalytic Fenton tower 8. In the utility model, the filter 9 is preferably a cloth filter, and the cloth filter is preferably provided with filter cloth, a filter disc and a central pipe; a dosing system is preferably arranged in the cloth filter in a matched manner and is used for adding a flocculating agent and a coagulant into the filter; the flocculant is preferably PAM, and the coagulant is preferably PAC; in the specific embodiment of the utility model, the effluent of the secondary catalytic Fenton tower 8 enters a cloth filter, the water is filtered and clarified by the cloth filter under the action of gravity, the filtered water enters a filter disc and is discharged through a central pipe, the solid is settled to the bottom of the filter, and in the filtering process, a coagulant and a flocculant are added into the cloth filter to reduce the organic matters in the water by matching with coagulation and flocculation reactions.
The system provided by the utility model comprises an ultrafiltration device 10, the inlet of which is communicated with the outlet of the filter chamber 9. In the utility model, an ultrafiltration membrane is preferably arranged in the ultrafiltration device, the ultrafiltration membrane is preferably made of PVDF (polyvinylidene fluoride), and the turbidity of produced water is less than or equal to 0.2 NTU; in the specific embodiment of the utility model, the effluent of the filter tank is lifted to an ultrafiltration device, and colloid, bacteria, macromolecular impurities and the like in the water are removed by an ultrafiltration membrane in a physical interception mode, so that the aim of purification is fulfilled. The ultrafiltration effluent can meet the first class A standard of pollutant discharge standard of urban sewage treatment plants, and can be directly discharged or recycled if the user does not have the requirement of reducing the conductivity.
The system provided by the present invention preferably further comprises a reverse osmosis unit 11 having an inlet in communication with the outlet of the ultrafiltration unit 10. In the present invention, a reverse osmosis membrane is preferably provided in the reverse osmosis apparatus; the reverse osmosis membrane preferably adopts original imported brands such as Dow, DelanMeier and the like, and the recovery rate is more than or equal to 55 percent; the ultrafiltration effluent enters a reverse osmosis device, desalination and concentration are realized through a reverse osmosis membrane, the conductivity of the effluent is reduced, and the effluent meets the reuse water standard. In the utility model, the reverse osmosis device is preferably provided with a concentrated water outlet and a clear water outlet, and the concentrated water outlet is preferably communicated with the inlet of the first-stage catalytic Fenton tower 3, so that the further treatment of the concentrated water is realized, and the recovery rate is improved; the desalting and filtering of the reverse osmosis device can reach more than 95%.
In the embodiment of the present invention, lift pumps are preferably disposed between adjacent devices for controlling the flow direction of the effluent of each device, that is, a lift pump is preferably disposed between the adjusting tank 1 and the three-phase separator 2, between the three-phase separator 2 and the catalytic fenton tower 3, between the catalytic fenton tower 3 and the primary cavitation air flotation machine 4, between the primary cavitation air flotation machine 4 and the secondary dissolved air flotation machine 5, between the secondary dissolved air flotation machine 5 and the a/O biochemical reaction tank 6, between the a/O biochemical reaction tank 6 and the MBR membrane tank 7, between the MBR membrane tank 7 and the secondary catalytic fenton tower 8, between the secondary catalytic fenton tower 8 and the filter tank 9, between the filter tank 9 and the ultrafiltration device 10, and between the ultrafiltration device 10 and the reverse osmosis device 11.
In a specific embodiment of the utility model, when the system is used for deep treatment and recycling of the oilfield fracturing flow-back fluid, the treatment steps are preferably as follows:
discharging the fracturing flow-back fluid into a regulating tank 1 to balance the water amount;
the effluent of the regulating reservoir 1 enters a three-phase separator 2 for three-phase separation;
the water phase obtained by three-phase separation enters a first-stage catalytic Fenton tower 3 for oxidation reaction to remove refractory organic matters;
the effluent of the first-stage catalytic Fenton tower 3 enters a first-stage cavitation air flotation machine 4, PAC and PAM are added into the first-stage cavitation air flotation machine 4, and the content of suspended matters, grease and jelly in water is reduced by micro-bubble, coagulation and flocculation reactions;
the effluent of the primary cavitation air flotation machine 4 enters a secondary dissolved air flotation machine 5 for secondary air flotation treatment, micro bubbles are generated under the pressurization condition, PAC and PAM are added into the secondary dissolved air flotation machine 5, and impurities in water are further reduced through the micro bubbles, coagulation and flocculation reactions;
the effluent of the secondary dissolved air flotation machine 5 enters an A/O reaction tank 6 to generate nitrification and denitrification, so that organic pollutants are degraded, and nitrogen and phosphorus removal is realized;
the effluent of the A/O reaction tank 6 enters an MBR membrane tank 7 for sludge-water separation;
the effluent of the MBR membrane tank 7 enters a secondary catalytic Fenton tower 8, and the content of organic pollutants is further reduced by using an oxidation reaction;
the effluent of the secondary catalytic Fenton tower 8 enters a filter 9 for filtering and clarification, PAC and PAM are added into the filter 9 at the same time, and the content of organic matters is reduced through coagulation and flocculation reactions;
the effluent of the filter 9 enters an ultrafiltration device 10 for ultrafiltration, and the obtained ultrafiltration effluent meets the first-class A standard of discharge Standard of pollutants for municipal wastewater treatment plants and is directly discharged or recycled;
when the conductivity of the outlet water is required, the outlet water of the ultrafiltration device 10 enters a reverse osmosis device 11 to realize concentration and desalination, and the conductivity of the outlet water is reduced, so that the outlet water meets the discharge or reuse standard; and (4) introducing concentrated water generated by the reverse osmosis device into the first-stage catalytic Fenton tower 3, and returning the concentrated water to the system for continuous treatment.
In the utility model, the dosage of PAC in the primary cavitation air flotation machine 4, the secondary dissolved air flotation machine 5 and the filter 9 is preferably 20-30 mg/L independently, and the dosage of PAM is preferably 0.03-1 mg/L independently.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention.
Example 1
(1) Firstly, pretreating fracturing flow-back fluid, discharging the fracturing flow-back fluid into a regulating tank 1 for balancing water quantity, feeding outlet water into a three-phase separator 2 to obtain filtered and clarified liquid, wherein the inlet water conductivity is 15000 us/cm;
(2) and then the wastewater is lifted to a first-stage catalytic Fenton tower 3 by a pump to carry out oxidation reaction to remove refractory organic matters, the effluent enters a first-stage cavitation air flotation machine 4, PAC and PAM are added into the first-stage cavitation air flotation machine 4, wherein the dosage of PAC is 20mg/L, the dosage of PAM is 0.03mg/L, and the impurities such as suspended matters, grease, jelly and the like in the incoming water are reduced by micro bubbles (the diameter is 40 mu m) and flocculation and coagulation reactions.
(3) The effluent of the cavitation air flotation machine 4 enters a secondary dissolved air flotation machine 5, micro bubbles (the diameter is 40 mu m) are generated under the pressurization condition, PAC and PAM are added into the primary cavitation air flotation machine 4, wherein the dosage of PAC is 20mg/L, the dosage of PAM is 0.03mg/L, and the micro bubbles are matched with PAC and PAM to further reduce impurities in the incoming water;
(4) the effluent of the secondary dissolved air flotation machine 5 enters an A/O reaction tank 6, and the wastewater is subjected to nitrification and denitrification, so that organic pollutants are degraded, and nitrogen and phosphorus removal is realized;
(5) after biochemical reaction, effluent enters an MBR (membrane bioreactor) membrane tank 7, sludge-water separation is realized by utilizing a high-efficiency membrane separation technology, the solid-liquid separation efficiency is greatly improved, the effluent enters a second-stage catalytic Fenton tower 8, the content of organic pollutants is further reduced by utilizing oxidation reaction, and the removal rate of COD is 90%;
(6) the effluent of the secondary catalytic Fenton tower 8 enters a filter 9 (a cloth filter), and is filtered and clarified after passing through filter cloth;
(7) the filtered effluent enters an ultrafiltration device 10 to purify and clarify the incoming water, and the effluent enters a reverse osmosis device 11 to realize concentration and desalination, so that the effluent meets the discharge or reuse standard, and the recovery rate of a reverse osmosis system is 60%. Wherein, the effluent of the ultrafiltration device and the effluent of the reverse osmosis device both meet the first class A standard of pollutant discharge Standard of urban wastewater treatment plant, and the conductivity of the effluent of the reverse osmosis device is 300 us/cm.
Example 2
(1) Firstly, pretreating fracturing flow-back fluid, discharging the fracturing flow-back fluid into a regulating tank 1 for balancing water quantity, feeding outlet water into a three-phase separator 2 to obtain filtered and clarified liquid, wherein the inlet water conductivity is 14000 us/cm;
(2) and then the wastewater is lifted to a first-stage catalytic Fenton tower 3 by a pump to carry out oxidation reaction to remove refractory organic matters, the effluent enters a first-stage cavitation air flotation machine 4, PAC and PAM are added into the first-stage cavitation air flotation machine 4, wherein the dosage of PAC is 20mg/L, the dosage of PAM is 0.05mg/L, and the impurities such as suspended matters, grease, jelly and the like in the incoming water are reduced by micro bubbles (the diameter is 50 mu m) and flocculation and coagulation reactions.
(3) The effluent of the cavitation air flotation machine 4 enters a secondary dissolved air flotation machine 5, micro bubbles (the diameter is 50 mu m) are generated under the pressurization condition, PAC and PAM are added into the primary cavitation air flotation machine 4, wherein the dosage of PAC is 20mg/L, the dosage of PAM is 0.05mg/L, and the micro bubbles are matched with PAC and PAM to further reduce impurities in the incoming water;
(4) the effluent of the secondary dissolved air flotation machine 5 enters an A/O reaction tank 6, and the wastewater is subjected to nitrification and denitrification, so that organic pollutants are degraded, and nitrogen and phosphorus removal is realized;
(5) after biochemical reaction, effluent enters an MBR (membrane bioreactor) membrane tank 7, sludge-water separation is realized by utilizing a high-efficiency membrane separation technology, the solid-liquid separation efficiency is greatly improved, the effluent enters a second-stage catalytic Fenton tower 8, the content of organic pollutants is further reduced by utilizing oxidation reaction, and the removal rate of COD is 92%;
(6) the effluent of the secondary catalytic Fenton tower 8 enters a filter 9 (a cloth filter), and is filtered and clarified after passing through filter cloth;
(7) the filtered effluent enters an ultrafiltration device 10 to purify and clarify the incoming water, and the effluent enters a reverse osmosis device 11 to realize concentration and desalination, so that the effluent meets the discharge or reuse standard, and the recovery rate of a reverse osmosis system is 55%. Wherein, the effluent of the ultrafiltration device and the effluent of the reverse osmosis device both meet the first class A standard of pollutant discharge Standard of urban wastewater treatment plant, and the conductivity of the effluent of the reverse osmosis device is 280 us/cm.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (8)
1. The utility model provides an oil field fracturing flow-back fluid deep treatment recycling system which characterized in that includes:
a regulating reservoir (1);
a three-phase separator (2) with an inlet communicated with an outlet of the regulating reservoir (1);
a first-stage catalytic Fenton tower (3) with an inlet communicated with an outlet of the three-phase separator (2);
a first-stage cavitation air flotation machine (4) with an inlet communicated with an outlet of the first-stage catalytic Fenton tower (3);
a second-stage dissolved air flotation machine (5) with an inlet communicated with the outlet of the first-stage cavitation air flotation machine (4);
an A/O biochemical reaction tank (6) with an inlet communicated with the outlet of the secondary dissolved air flotation machine (5);
an MBR membrane tank (7) with an inlet communicated with the outlet of the A/O biochemical reaction tank (6);
a secondary catalytic Fenton tower (8) with an inlet communicated with an outlet of the MBR membrane tank (7);
the inlet of the filter tank (9) is communicated with the outlet of the secondary catalytic Fenton tower (8);
an ultrafiltration device (10) with an inlet communicated with the outlet of the filter tank (9).
2. The system according to claim 1, further comprising a reverse osmosis device (11) having an inlet in communication with an outlet of the ultrafiltration device (10).
3. A system according to claim 1, characterized in that a flow divider and an oil baffle are arranged in the three-phase separator (2).
4. The system according to claim 1, wherein the ultrafiltration membrane in the ultrafiltration device (10) is a polyvinylidene fluoride membrane.
5. The system of claim 4, wherein the ultrafiltration membrane has a molecular weight cut-off of 1000 to 500000 Da.
6. The system as claimed in claim 1, wherein the primary cavitation air flotation machine (4), the secondary dissolved air flotation machine (5) and the filter (9) are all provided with dosing systems in a matching manner.
7. A system according to claim 2, characterized in that the reverse osmosis device (11) is provided with a concentrate outlet and a clean water outlet; the concentrated water outlet is communicated with the inlet of the first-stage catalytic Fenton tower (3).
8. A system according to claim 1, wherein the filter chamber (9) is a cloth filter chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220537030.6U CN216890548U (en) | 2022-03-11 | 2022-03-11 | Flowing back advanced treatment recycling system is returned in oil field fracturing |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220537030.6U CN216890548U (en) | 2022-03-11 | 2022-03-11 | Flowing back advanced treatment recycling system is returned in oil field fracturing |
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| CN216890548U true CN216890548U (en) | 2022-07-05 |
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