CN209411983U - A kind of oil-gas field fracturing returns the wastewater treatment equipment of drain - Google Patents
A kind of oil-gas field fracturing returns the wastewater treatment equipment of drain Download PDFInfo
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Abstract
The utility model relates to the wastewater treatment equipments that a kind of oil-gas field fracturing returns drain.Described device includes: electrolysis cells, mixed gas generating unit, and the agitating device below the electrolysis cells.Device described in the utility model has cooperateed with the effect of Electro Sorb, electrochemical oxidation and electro-catalysis ozone oxidation, solves conventional three-dimensional electrode current low efficiency, the slow problem of organic matter degradation rate, significantly improve the treatment effeciency and processing cost of fracturing outlet liquid discharge, it is discharged COD removal rate and is greater than 90%, biochemical ratio is greater than 0.4, and effluent quality is obviously improved, and water stabilization.
Description
Technical Field
The utility model belongs to the waste water treatment field, concretely relates to three-dimensional electrode coupling ozone oxidation handles device of flowing back is returned to oil gas field fracturing.
Background
The fracturing flowback fluid generated in the process of oil and gas field exploitation is one of the main pollution sources of oil and gas enterprises. With the continuous update of water treatment technology and treatment equipment, the fracturing flow-back fluid treatment technology is continuously advanced. Wherein, the treatment technology taking advanced oxidation as a core can generate a non-selective strong oxidant OH so as to mineralize organic pollutants more efficiently and further reduce the discharge of COD.
The three-dimensional electrode electrochemical advanced oxidation technology is a novel electrochemical advanced oxidation technology which is widely researched in recent years, and granular or clastic particle electrodes are filled between a cathode and an anode to form a three-dimensional electrode, so that the mass transfer limit of pollutants which is ubiquitous in the traditional two-dimensional electrode electrochemical oxidation process is greatly improved.
However, the three-dimensional electrode system is lack of a sufficient amount of strong oxidant, a long treatment time is still needed for high-concentration industrial wastewater, pollutants are gradually adsorbed on the particle electrode, the particle electrode is easily inactivated, the continuous operation of the system is not facilitated, and the COD discharge is difficult to reach the standard.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems, the utility model provides a device for treating the fracturing flow-back fluid of an oil and gas field by utilizing a three-dimensional electrode coupled with ozone oxidation; the device combines electric adsorption, electrochemical oxidation and electrocatalytic ozone oxidation, utilizes good adsorption performance and catalytic performance of the particle electrode, and efficiently and continuously generates H at the cathode by an electrochemical method2O2And with the exposed O3The peroxone reaction is generated to generate OH, and the refractory organic pollutants in the fracturing flow-back fluid of the oil-gas field are efficiently removed from multiple ways.
The technical scheme of the utility model as follows.
An apparatus for treating wastewater, comprising: the device comprises an electrolysis unit, a mixed gas generation unit and a stirring device positioned below the electrolysis unit;
the electrolysis unit includes: an electrolytic cell, a three-dimensional electrode, a direct current power supply and a microporous disc; the micropore plate is arranged below the three-dimensional electrode and at the bottom of the electrolysis unit and used for supporting and fixing the three-dimensional electrode, and meanwhile, mixed gas is changed into micro bubbles after passing through the micropore plate, so that mass transfer is facilitated, and the particle electrode can be slightly disturbed.
The mixed gas generation unit includes: an ozone generator, an aeration head and an ozone breaker; wherein the ozone generator located outside the electrolysis unit is connected with the aeration head pipeline located inside the electrolysis unit; the ozone destructor is located outside the electrolysis unit and is connected with an air outlet pipeline at the top of the electrolysis unit.
Further, the electrolytic bath is a cuboid, and the specific size can be adjusted according to actual needs, for example, the size is 3.5cm × 12.5cm × 20cm, and the electrolytic bath is arranged above the center of the stirring device.
Further, the three-dimensional electrode consists of an inert anode, a cathode and a particle electrode;
wherein the area of the inert anode is 100-150 cm2Preferably 121-144 cm2(ii) a The inert anode is selected from a platinum electrode, a stainless steel electrode, a graphite electrode, a titanium ruthenium-iridium plated electrode, a titanium alloy electrode or a boron-doped diamond electrode, and is preferably a titanium ruthenium-iridium plated electrode. The utility model discloses an inert anode can strengthen the catalytic oxidation degradation of organic pollutant on the positive pole surface, and low price, and stability is good.
Wherein the area of the cathode is 100-150 cm2Preferably 121-144 cm2(ii) a The cathode is selected from a graphite electrode, a carbon felt electrode, an activated carbon fiber electrode, a glassy carbon electrode and a carbon black-polytetrafluoroethylene gas diffusion electrode, and is preferably a carbon black-polytetrafluoroethylene gas diffusion electrode. The cathode adopted by the utility model can be used for leading O2Two-electron reduction reaction on the surface of the substrate to generate H2O2。
The electrode adopted by the utility model is a self-made electrode except for carbon black-polytetrafluoroethylene gas diffusion electrode, and other electrodes are purchased directly from the market;
the preparation method of the carbon black-polytetrafluoroethylene gas diffusion electrode comprises the following steps:
(1) cutting the whole nickel screen into a rectangle with a certain size, cleaning the rectangle with methanol, carrying out ultrasonic treatment for 15 minutes, and drying the rectangle for later use.
(2) Weighing 6g of carbon black, placing the carbon black in a beaker, adding 80mL of absolute ethyl alcohol, performing ultrasonic treatment for 10 minutes, adding 8mL of polytetrafluoroethylene emulsion, and performing ultrasonic treatment for 15 minutes.
(3) The beaker is placed on an electric furnace to be heated and continuously stirred until the beaker is pasty.
(4) Pressing the paste into sheets with the thickness of 0.5mm, respectively attaching the sheets to two sides of a spare nickel net, and tabletting for 1 minute under the pressure of 20 MPa.
(5) And (3) putting the electrode formed by tabletting into a muffle furnace, heating the temperature in the furnace from room temperature to 350 ℃ and maintaining for 1 hour, and naturally cooling to obtain the carbon black-polytetrafluoroethylene gas diffusion electrode.
The inert anode and the cathode are vertically inserted in parallel along two walls of the electrolytic cell and are respectively connected with the anode and the cathode of the direct current power supply.
A particle electrode is filled between the inert anode and the cathode, and the particle electrode is selected from one or more of columnar activated carbon, granular activated carbon, silica gel, graphite, ceramsite or quartz sand; preferably columnar activated carbon; the diameter of the particle electrode is 1-4mm, preferably 1.5 mm; the loading of the particle electrode is 100 to 150g, preferably 120 to 130 g. Particle electrode loading can guarantee that particle electrode adsorbs the gathering organic pollutant as much as possible, can slightly disturb under the bubble effect simultaneously, do benefit to the regeneration.
Further, the stirring unit includes a magnetic stirrer and a rotor.
Further, the aeration head is a stainless steel pipe type micropore aeration head, and the aperture of each micropore is 2-20 microns.
Furthermore, the mixed gas generating unit also comprises auxiliary equipment such as an ozone detector, a gas flowmeter and an oxygen cylinder.
The working principle of the device is as follows: waste water (flowing back is returned in oil gas field fracturing) gets into through the peristaltic pump electrolysis trough bottom, oxygen entering simultaneously ozone generator, the mist of gained ozone and oxygen pass through behind ozone detector and the gas flowmeter aeration head lets in electrolysis trough bottom, and waste water passes through the micropore dish under the magnetic stirrers effect, from bottom to top the warp behind the three-dimensional electrode is handled, by delivery port discharge on electrolysis trough upper portion, and remaining ozone gas lets in the ozone destroyer through the electrolysis trough top and destroys.
The utility model also provides a method for utilizing above-mentioned device to handle flowing back is returned to oil gas field fracturing, include:
(1) the fracturing flow-back fluid of the oil and gas field enters the bottom of an electrolysis unit of the device;
(2) oxygen enters an ozone generator of a mixed gas generating unit of the device, and the generated mixed gas of the ozone and the oxygen is introduced into the bottom of an electrolytic unit and is mixed with the fracturing flow-back fluid of the oil-gas field;
(3) under the stirring action, the fracturing flow-back fluid of the oil-gas field passes through the microporous disc and is treated by the three-dimensional electrode from bottom to top, finally, the water after electrolytic treatment is discharged from the water outlet at the upper part of the electrolytic unit, and the residual mixed gas is introduced into the ozone destructor through the top of the electrolytic unit for destruction.
In the step (1), the oil-gas field fracturing flow-back fluid is a fracturing waste liquid stock solution generated after fracturing construction of an oil-gas field, the COD concentration of the oil-gas field fracturing flow-back fluid is 2000-8000 mg/L, the biodegradability B/C ratio is 0.1-0.3, the pH value is 5-9, and the electric conductivity is more than 6000 muS/cm.
In the step (2), the mixed gas is O35-10% by volume of a mixed gas consisting of oxygen and ozone.
The mixed gas is prepared by adopting an ozone generator, and the method comprises the following steps: pure O is added2Passing through an ozone generator, part of O2Electrochemical reaction under high-voltage discharge to convert into O3。
In the step (2), O is exposed to the electrolytic cell2And O3When gas is mixed, a bottom micropore aeration mode is adopted; the gas flow rate of the micropore aeration is 0.2-0.8L/min, and O3The concentration of (b) is 30-120 mg/L.
In the step (3), the power supply used in the three-dimensional electrode is a common direct current stabilized power supply, and the current density capable of being provided is 10-50 mA/cm2。
The utility model discloses in, the hydraulic power dwell time of flowing back is returned in the oil gas field fracturing is 30 ~ 90 min. In the actual industrial treatment process, each item of operation is carried out in succession.
The principle of the method is as follows: in a direct current electric field, the activated carbon particle electrodes generate certain adsorption and filtration interception effects on organic matters; o dissolved in water2Two-electron reduction reaction (1) is carried out on a carbon black-polytetrafluoroethylene cathode to generate H2O2With O which can be exposed to the solution3Further, a peroxine reaction occurs to produce OH (2) having a strong oxidizing property; while O is3Can catalyze and generate OH on an active carbon particle electrode, and can generate OH (3) and (4) through an electroreduction reaction on a cathode; the multiple OH generation ways can effectively and rapidly degrade pollutants in a solution and adsorbed on the activated carbon particle electrode, and simultaneously regenerate the particle electrode, thereby continuously and efficiently degrading organic pollutants.
O2+2H++2e-→H2O2 (1)
2H2O2+2O3→H2O+3O2+HO2·+·OH (2)
Compare with the method of flowing back is returned to advanced oxidation treatment oil gas field fracturing of traditional electrochemistry, the utility model discloses a unique advantage and beneficial effect as follows:
(1) by cooperating with the effects of electro-adsorption, electrochemical oxidation and electro-catalytic ozonation, the emission can reach the standard within a short time;
(2) no medicament is required to be added, so that secondary pollution can be reduced, and the treatment cost is reduced;
(3) the treatment device is simple, and the generation of the strong oxidant in the process is convenient to control and regulate, so that the treatment efficiency is improved;
(4) the active carbon particle electrode can be regenerated simultaneously in the treatment process and can be used for a long time.
Therefore, the treatment method is a method for efficiently removing COD in the treatment process of the fracturing flow-back fluid of the oil and gas field, and has good development and application prospects.
Drawings
Fig. 1 is a schematic view of the apparatus shown in embodiment 1 of the present invention.
In the figure: 1. an electrolytic cell; 2. an anode; 3. a cathode; 4. an activated carbon particle electrode; 5. a direct current power supply; 6. a magnetic stirrer; 7. a rotor; 8. a micro-porous disk; 9. an ozone destructor; 10. a water storage tank; 11. a peristaltic pump; 12. an oxygen cylinder; 13. an ozone generator; 14. an ozone detector; 15. a gas flow meter; 16. an aeration head.
Detailed Description
The following examples are intended to illustrate the invention, but are not intended to limit the scope of the invention.
The water body to be treated in each embodiment is taken from the stock solution of the fracturing flow-back fluid of the oil and gas field, the initial concentration of COD in each embodiment is in the range of 2000-8000 mg/L, and the concentration range of COD in the wastewater of the fracturing flow-back fluid of the common oil and gas field is covered.
The electrode adopted by the utility model is self-made except the carbon black-polytetrafluoroethylene gas diffusion electrode, and other electrodes are directly purchased from the market.
EXAMPLE 1 an apparatus for treating wastewater
The present embodiment provides an apparatus for treating wastewater, as shown in fig. 1, comprising: the device comprises an electrolysis unit, a mixed gas generation unit and a stirring device positioned below the electrolysis unit;
the electrolysis unit includes: the electrolytic cell comprises an electrolytic cell 1, a three-dimensional electrode, a direct current power supply 5 and a microporous disc 8; the micropore plate is arranged below the three-dimensional electrode and at the bottom of the electrolysis unit and used for supporting and fixing the three-dimensional electrode, and meanwhile, mixed gas is changed into micro bubbles after passing through the micropore plate, so that mass transfer is facilitated, and the particle electrode can be slightly disturbed.
The mixed gas generation unit includes: an ozone generator 13, an aeration head 16 and an ozone breaker 9; wherein the ozone generator located outside the electrolysis unit is connected with the aeration head pipeline located inside the electrolysis unit; the ozone destructor is located outside the electrolysis unit and is connected with an air outlet pipeline at the top of the electrolysis unit.
The electrolytic bath is a cuboid, the size of the electrolytic bath is 3.5cm multiplied by 12.5cm multiplied by 20cm, and the electrolytic bath is arranged in the center of the stirring unit.
The three-dimensional electrode consists of an inert anode 2, a cathode 3 and a particle electrode 4;
wherein the area of the inert anode is 144cm2The ruthenium iridium plated titanium electrode (available from Qixin titanium industry Co., Ltd., Bao chicken city).
Wherein,the area of the cathode is 144cm2The carbon black-polytetrafluoroethylene gas diffusion electrode.
The preparation method of the carbon black-polytetrafluoroethylene gas diffusion electrode comprises the following steps:
(1) cutting the whole nickel screen into a rectangle with a certain size, cleaning the rectangle with methanol, carrying out ultrasonic treatment for 15 minutes, and drying the rectangle for later use.
(2) Weighing 6g of carbon black, placing the carbon black in a beaker, adding 80mL of absolute ethyl alcohol, performing ultrasonic treatment for 10 minutes, adding 8mL of polytetrafluoroethylene emulsion, and performing ultrasonic treatment for 15 minutes.
(3) The beaker is placed on an electric furnace to be heated and continuously stirred until the beaker is pasty.
(4) Pressing the paste into sheets with the thickness of 0.5mm, respectively attaching the sheets to two sides of a spare nickel net, and tabletting for 1 minute under the pressure of 20 MPa.
(5) And (3) putting the electrode formed by tabletting into a muffle furnace, heating the temperature in the furnace from room temperature to 350 ℃ and maintaining for 1 hour, and naturally cooling to obtain the carbon black-polytetrafluoroethylene gas diffusion electrode.
The inert anode and the cathode are vertically inserted in parallel along two walls of the electrolytic cell and are respectively connected with the anode and the cathode of the direct current power supply, columnar granular activated carbon with the diameter of 1.5mm is filled between the two electrodes to serve as a particle electrode, and the specific filling amount is 120 g.
The stirring unit comprises a magnetic stirrer 6 and a rotor 7. The electrolytic cell is arranged in the center of the magnetic stirrer 6, the magnetic rotor 7 is arranged at the bottom of the electrolytic cell, and the rotation speed of the rotor 7 is 600-1200rpm under the action of the magnetic stirrer 6, so that the pollutant mass transfer is facilitated, and the treatment effect is improved.
The aeration head is a stainless steel pipe type microporous aeration head, and the aperture of each micropore is 2-20 microns.
The mixed gas generating unit also comprises an ozone detector 14, a gas flowmeter 15 and an oxygen cylinder 12;
the device for treating the wastewater also comprises auxiliary equipment such as a water storage tank 10, a peristaltic pump 11 and the like.
Embodiment 2 method for treating fracturing flow-back fluid of oil and gas field
The embodiment provides a method for treating a fracturing flow-back fluid of an oil and gas field by using the device in the embodiment 1, which comprises the following steps:
(1) the fracturing flow-back fluid of the oil and gas field enters the bottom of an electrolysis unit of the device;
(2) oxygen enters an ozone generator of a mixed gas generating unit of the device, and the generated mixed gas of the ozone and the oxygen is introduced into the bottom of an electrolytic unit and is mixed with the fracturing flow-back fluid of the oil-gas field;
(3) under the stirring action, the fracturing flow-back fluid of the oil-gas field passes through the microporous disc and is treated by the three-dimensional electrode from bottom to top, finally, the water after electrolytic treatment is discharged from the water outlet at the upper part of the electrolytic unit, and the residual mixed gas is introduced into the ozone destructor through the top of the electrolytic unit for destruction.
In the step (1), the oil-gas field fracturing flow-back fluid is a fracturing waste liquid stock solution generated after fracturing construction of an oil-gas field, the COD concentration of the oil-gas field fracturing flow-back fluid is 2500mg/L, the biodegradability B/C ratio is 0.13, the pH value is 7.5, and the conductivity is 12000 mu S/cm.
In the step (2), the mixed gas is O310% by volume of a gas mixture consisting of oxygen and ozone.
In the step (2), O is exposed to the electrolytic cell2And O3When gas is mixed, a bottom micropore aeration mode is adopted; the gas flow rate of the micropore aeration is 0.4L/min, O3The concentration of (3) was 40 mg/L.
In the step (3), the power supply used in the three-dimensional electrode is a common direct current stabilized power supply, and the current density capable of providing is 20mA/cm2。
The hydraulic retention time of the fracturing flow-back fluid of the oil and gas field is 30 min.
In the actual treatment process, all the operations are continuously performed.
The effluent from the liquid outlet was tested and had a COD removal of 90% and a biodegradability B/C ratio of 0.45.
Embodiment 3 method for treating fracturing flow-back fluid of oil and gas field
This example provides a method of treating a fracturing flow-back fluid from an oil and gas field using the apparatus of example 1, which differs from example 2 in that:
(1) the initial COD concentration of the fracturing flow-back fluid of the oil and gas field is 2500mg/L, the biodegradability B/C ratio is 0.13, the pH value is 7.5, and the conductivity is 12000 mu S/cm;
(2) the filling amount of the activated carbon particle electrode is 100 g;
(3) the flow rate of the mixed gas is 0.4L/min, O3The concentration is 40 mg/L;
the effluent from the liquid outlet was tested and had a COD removal of 90% and a biodegradability B/C ratio of 0.40.
Embodiment 4 method for treating fracturing flowback fluid of oil and gas field
This example provides a method of treating a fracturing flow-back fluid from an oil and gas field using the apparatus of example 1, which differs from example 2 in that:
(1) the initial COD concentration of the fracturing flow-back fluid of the oil and gas field is 2500mg/L, the biodegradability B/C ratio is 0.13, the pH value is 7.5, and the conductivity is 12000 mu S/cm;
(2) the loading of the active carbon particle electrode is 150 g;
(3) the flow rate of the mixed gas is 0.4L/min, O3The concentration is 40 mg/L;
the effluent from the liquid outlet was tested and had a COD removal of 92% and a biodegradability B/C ratio of 0.44.
Example 5 method for treating fracturing flow-back fluid of oil and gas field
This example provides a method of treating a fracturing flow-back fluid from an oil and gas field using the apparatus of example 1, which differs from example 2 in that:
(1) the initial COD concentration of the fracturing flow-back fluid of the oil and gas field is 7000mg/L, the biodegradability B/C ratio is 0.22, the pH value is 5.5, and the conductivity is 9000 mu S/cm;
(2) the hydraulic retention time is 60 min;
(3) the current density at the two ends of the cathode and the anode is 40mA/cm2；
(4) The filling amount of the activated carbon particle electrode is 120 g;
(5) the flow rate of the mixed gas is 0.8L/min, O3The concentration is 90 mg/L;
the effluent from the liquid outlet was tested and had a COD removal of 90% and a biodegradability B/C ratio of 0.47.
Embodiment 6 method for treating fracturing flowback fluid of oil and gas field
This example provides a method of treating a fracturing flow-back fluid from an oil and gas field using the apparatus of example 1, which differs from example 2 in that:
(1) the initial COD concentration of the fracturing flow-back fluid of the oil and gas field is 7000mg/L, the biodegradability B/C ratio is 0.22, the pH value is 5.5, and the conductivity is 9000 mu S/cm;
(2) the hydraulic retention time is 90 min;
(3) the current density at the two ends of the cathode and the anode is 40mA/cm2；
(4) The filling amount of the activated carbon particle electrode is 120 g;
(5) the flow rate of the mixed gas is 0.8L/min, O3The concentration is 90 mg/L;
the effluent from the liquid outlet was tested and had a COD removal of 98% and a biodegradability B/C ratio of 0.52.
Example 7 method for treating fracturing flowback fluid of oil and gas field
This example provides a method of treating a fracturing flow-back fluid from an oil and gas field using the apparatus of example 1, which differs from example 2 in that:
(1) the initial COD concentration of the fracturing flow-back fluid of the oil and gas field is 7000mg/L, the biodegradability B/C ratio is 0.22, the pH value is 5.5, and the conductivity is 9000 mu S/cm;
(2) the hydraulic retention time is 90 min;
(3) the current density at the two ends of the cathode and the anode is 40mA/cm2；
(4) The filling amount of the activated carbon particle electrode is 120 g;
(5) the flow rate of the mixed gas is 0.8L/min, O3The concentration is 120 mg/L;
the effluent from the liquid outlet was tested and had a COD removal of 95% and a biodegradability B/C ratio of 0.50.
Although the invention has been described in detail with respect to the general description and the specific embodiments, it will be apparent to those skilled in the art that modifications and improvements can be made based on the invention. Therefore, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (11)
1. An apparatus for treating wastewater, comprising: the device comprises an electrolysis unit, a mixed gas generation unit and a stirring device positioned below the electrolysis unit;
the electrolysis unit includes: an electrolytic cell, a three-dimensional electrode, a direct current power supply and a microporous disc; wherein the micro-porous disc is arranged at the bottom of the electrolytic unit and below the three-dimensional electrode;
the mixed gas generation unit includes: an ozone generator, an aeration head and an ozone breaker; wherein the ozone generator located outside the electrolysis unit is connected with the aeration head pipeline located inside the electrolysis unit; the ozone destructor is located outside the electrolysis unit and is connected with an air outlet pipeline at the top of the electrolysis unit.
2. The apparatus of claim 1, wherein the electrolytic cell is centrally disposed above the stirring device.
3. The device according to claim 1, wherein the three-dimensional electrode consists of an inert anode, a cathode, a particle electrode filled between the two electrodes;
the particle electrode is selected from one or more of columnar activated carbon, granular activated carbon, silica gel, graphite, ceramsite or quartz sand.
4. The device of claim 3, wherein the particulate electrode is selected from columnar activated carbon.
5. The device according to claim 3 or 4, wherein the particle electrode has a diameter of 1-4mm and a loading of 100-150 g.
6. The apparatus of claim 3, wherein the inert anode has an area of 100-150 cm2；
The inert anode is selected from a platinum electrode, a stainless steel electrode, a graphite electrode, a titanium ruthenium-coated iridium electrode, a titanium alloy electrode or a boron-doped diamond electrode.
7. The apparatus of claim 6, wherein the inert anode has an area of 121-144 cm2。
8. The apparatus of claim 3, wherein the cathode is ofThe area is 100-150 cm2；
The cathode is selected from a graphite electrode, a carbon felt electrode, an activated carbon fiber electrode, a glassy carbon electrode and a carbon black-polytetrafluoroethylene gas diffusion electrode.
9. The device of claim 8, wherein the area of the cathode is 121-144 cm2。
10. The apparatus of claim 1, wherein the aeration head is a microporous aeration head, and the pore size of the micropores is 2-20 microns.
11. The apparatus of claim 1, wherein the mixed gas generating unit further comprises an ozone detector, a gas flow meter, and an oxygen cylinder.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110921980A (en) * | 2019-11-13 | 2020-03-27 | 河海大学 | Electrochemical enhanced ozone-biological activated carbon water treatment equipment and method for treating water by using same |
| CN111115916A (en) * | 2018-10-31 | 2020-05-08 | 中石化节能环保工程科技有限公司 | Device and method for treating fracturing flow-back fluid of oil and gas field |
| CN113461231A (en) * | 2021-06-23 | 2021-10-01 | 长沙工研院环保有限公司 | Electrocatalytic oxidation wastewater treatment system |
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2018
- 2018-10-31 CN CN201821792033.4U patent/CN209411983U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115916A (en) * | 2018-10-31 | 2020-05-08 | 中石化节能环保工程科技有限公司 | Device and method for treating fracturing flow-back fluid of oil and gas field |
| CN110921980A (en) * | 2019-11-13 | 2020-03-27 | 河海大学 | Electrochemical enhanced ozone-biological activated carbon water treatment equipment and method for treating water by using same |
| CN113461231A (en) * | 2021-06-23 | 2021-10-01 | 长沙工研院环保有限公司 | Electrocatalytic oxidation wastewater treatment system |
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