CN211688633U - Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater - Google Patents
Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater Download PDFInfo
- Publication number
- CN211688633U CN211688633U CN201921914241.1U CN201921914241U CN211688633U CN 211688633 U CN211688633 U CN 211688633U CN 201921914241 U CN201921914241 U CN 201921914241U CN 211688633 U CN211688633 U CN 211688633U
- Authority
- CN
- China
- Prior art keywords
- tank
- gas
- air
- jet
- water distribution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
- Physical Water Treatments (AREA)
Abstract
The utility model discloses a jet gas distribution and water distribution type oilfield wastewater electrocoagulation treatment system, wherein an air floatation system pumps oily wastewater into an air floatation tank at high pressure, scrapes off large pieces of oil stains floating on the surface and conveys the large pieces of oil stains to a homogenizing and adjusting system; the homogenizing adjusting system is used for monitoring and adjusting the pH value and the electrolyte concentration of the water body; the jet aeration water distribution system carries out aeration treatment to form gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electric flocculation system; the electric flocculation system carries out electric flocculation reaction treatment on the water body, scum generated by the reaction is scraped, the part of waste gas generated by the reaction is introduced into the jet aeration water distribution system for aeration treatment and the air floatation system for providing pumping high pressure, and the rest part is treated by the tail gas treatment system. Through the technical scheme of the utility model, multiple impurity in the oily waste water can once only be detached to realize no dead angle water distribution, improved the electricity and transmitted matter efficiency, reduced tail gas treatment pressure.
Description
Technical Field
The utility model relates to a waste water treatment technical field especially relates to a efflux gas distribution water distribution formula oil field waste water electric flocculation treatment system.
Background
At present, industries such as petroleum, chemical industry, steel, mechanical manufacturing and the like generate a large amount of oily wastewater every year, and the oily substances are generally complex in components, difficult to biodegrade and great in harm. At present, the main methods and processes for treating oily wastewater comprise: gravity separation, air flotation, coarse granulation, filtration, adsorption, oxidation, membrane, flocculation, electroflocculation, electromagnetic methods, and the like. In practical applications, a single treatment method is difficult to achieve, and thus, a combined process is often used.
The electroflocculation technology uses a soluble anode (Al or Fe) as a sacrificial electrode, and hydrogen and oxygen generated by a cathode can form a large amount of tiny bubbles through electrochemical reaction, so that the electroflocculation technology has a good air flotation separation effect; meanwhile, the anode generates a flocculating agent which has good flocculation, the flocculating agent is ferric hydroxide (aluminum hydroxide) precipitate, has adsorption performance and can effectively remove pollutants from the wastewater, thereby removing oil particles by air floatation or sedimentation.
At present, an aeration system needs to be put into an electrolytic cell in an electric flocculation system, so that bubbles are generated to accelerate the air floatation separation effect, and water in the electrolytic cell is disturbed to increase the electric electrolyte area. Micro-bubbles (H) are generated due to the cathodic hydrogen evolution reaction2) When the generation rate is high, the polymerization of metal ions is disturbed, the flocculant is slowly generated, and the polymerization degree and the density are small, so that the excessively slow water flow rate and the excessively large bubble volume are not beneficial to improving the electric flocculation decontamination efficiency.
The air distribution mode of the existing electric flocculation system adopts tubular air distribution mostly, the mode generates large bubbles, and the disturbance effect on sewage is limited. When traditional electric flocculation handles oil field sewage, configuration air supporting equipment is scraped the dregs of fat after electric flocculation and is got, and long-time piling up of this suspended solid dregs of fat can make electric mass transfer efficiency descend, and too much dross is piled up simultaneously, blocks up the pipeline export easily. In addition, hydrogen formed by the conventional electrocoagulation process has certain potential safety hazard and is not suitable to be released randomly in special occasions.
SUMMERY OF THE UTILITY MODEL
At least one to the above-mentioned problem, the utility model provides a efflux gas distribution water distribution formula oil field waste water electric flocculation processing system adopts efflux nanometer aeration electric flocculation combined process technique, supplementary air floatation system and tail gas processing system, have electric flocculation concurrently, the characteristic of electric floatation and electrochemistry, multiple impurity in the oily waste water can once only be detached, efflux aeration water distribution system can realize the electric flocculation water distribution simultaneously, the gas distribution function, and realize no dead angle water distribution, improve the electricity matter efficiency of electricity, reduce tail gas treatment pressure, avoid the potential safety hazard.
In order to achieve the above object, the utility model provides a efflux gas distribution water distribution formula oil field waste water electric flocculation processing system, include: the system comprises an air floatation system, a homogeneity adjusting system, an electric flocculation system, a jet aeration water distribution system and a tail gas treatment system; the air floatation system pumps the oily wastewater into an air floatation tank at high pressure, and conveys a large amount of oil stains floating on the surface to the homogenizing adjusting system after scraping; the homogeneous regulating system is used for monitoring and regulating the pH value and the electrolyte concentration of the water body; the jet aeration water distribution system carries out aeration treatment on the output water body of the homogenizing regulation system to form a gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electric flocculation system; the electric flocculation system carries out electric flocculation reaction treatment on a water body and scrapes scum generated by the reaction, part of waste gas generated by the reaction is introduced into the jet aeration water distribution system for aeration treatment and the air floatation system for providing pumping high pressure, and the rest part of the waste gas is treated by the tail gas treatment system.
In the above technical scheme, preferably, the air floatation system includes the air floatation tank, an air floatation slag scraper, a pressure vessel tank, a vessel pressure pump and a slag collection tank, the vessel pressure pump pumps oily wastewater into the pressure vessel tank, the pressure vessel tank pumps high-pressure air through an air pump, so that the pressure vessel tank conveys the oily wastewater to the air floatation tank, the oily wastewater forms large oil stains on the surface of the air floatation tank, and the air floatation slag scraper scrapes the large oil stains to the slag collection tank.
In the above technical scheme, preferably, the homogeneity governing system includes PH equalizing basin, acid-alkali liquid storage tank, PH on-line monitoring appearance, TDs detector and electrolyte storage tank, oily waste water after the air supporting system handles carry to in the PH equalizing basin, PH on-line monitoring appearance with the TDs detector is used for detecting respectively the pH value and the conductivity value in the solution of water in the PH equalizing basin, and through the acid-alkali liquid storage tank is adjusted the pH value of solution in the PH equalizing basin, through the electrolyte storage tank is adjusted the electrolyte concentration of solution in the PH equalizing basin.
In the above technical scheme, preferably, the jet aeration water distribution system includes self-oscillation jet mixer, diversion pump, draught fan, gas-liquid outgoing pipeline and jet nozzle, the diversion pump will the water pump after adjusting in the homogeneity governing system is arrived in the self-oscillation jet mixer, self-oscillation jet mixer with the draught fan is linked together, self-oscillation jet mixer's export with through gas-liquid outgoing pipeline is connected to jet nozzle, it is a plurality of jet nozzle set up in bottom in the flocculation reaction tank of electrocoagulation system.
In the above technical solution, preferably, the self-oscillating jet mixer includes a fluid driving nozzle, an air suction pipe, an air mixing chamber, a self-oscillating chamber, a collision wall and a diffuser pipe, the fluid driving nozzle is communicated with an outlet of the priming pump, the air mixing chamber is arranged at an outlet of the fluid driving nozzle, the air suction pipe is arranged on a side wall of the air mixing chamber and communicated with an outlet of the induced draft fan, the air sucked by the air suction pipe and the oily wastewater form a gas-liquid mixed flow in the air mixing chamber, the self-oscillating chamber is arranged at the outlet of the air mixing chamber, the collision wall is formed inside the self-oscillating chamber, the gas-liquid mixed flow forms a discrete vortex ring in the self-oscillating chamber through self-oscillating shearing, and generates a pressure oscillation wave under the action of the collision wall, and the outlet of the self-oscillating chamber is communicated with the diffuser pipe, the diffusion pipe is communicated with the gas-liquid emergent pipeline, and the gas-liquid mixed flow is sprayed out from the diffusion pipe.
In the above technical scheme, preferably, the electric flocculation system includes a power supply, an anode plate, a cathode plate, a flocculation reaction tank, a slag scraping machine, a conical slag collecting tank, a sludge pump and a slag collecting tank, the anode plate and the cathode plate are respectively connected with the anode and the cathode of the power supply, the anode plate and the cathode plate are respectively arranged in the flocculation reaction tank at intervals in a staggered manner, the slag scraping machine is arranged in the flocculation reaction tank and used for scraping scum on the liquid level of the flocculation reaction tank to the conical slag collecting tank, and the sludge pump pumps the sludge in the conical slag collecting tank to the slag collecting tank.
In the above technical scheme, preferably, the tail gas treatment system includes a gas collecting hood, an air inducing pipe and a combustion tower, the gas collecting hood is disposed on the flocculation reaction tank, one end of the air inducing pipe is communicated with the inside of the gas collecting hood, and the other end of the air inducing pipe is respectively connected to the jet aeration water distribution system for aeration treatment, connected to the air floatation system through an air inducing pipe for providing high pumping pressure, and communicated to the combustion tower through an electric valve for tail gas treatment.
In the above technical solution, preferably, when the air sources required by the jet aeration water distribution system and the air floatation system are insufficient and the air draft tube has negative pressure, the electric valve is reversely opened to supplement the air sources to the jet aeration water distribution system and the air floatation system, and when the air draft tube has positive pressure, the combustion tower is opened to consume the remaining tail gas.
In the above technical solution, preferably, the PH value of the solution in the PH adjusting tank is controlled, the PH value is 5-7 when the anode plate is an iron anode, the PH value is 6-8 when the anode plate is an aluminum anode, and the electrolyte storage tank is controlled to add the electrolyte into the PH adjusting tank so that the conductivity of the solution is above 3000 us/cm.
In the above technical solution, preferably, the axial center line of the jet nozzles intersects the horizontal surface downward at an angle of 30 ° to 150 °, and the plurality of jet nozzles are respectively arranged at the bottom of the flocculation reaction tank at a preset angle of incidence.
Compared with the prior art, the beneficial effects of the utility model are that: the jet flow nano aeration and electric flocculation combined process technology, the auxiliary air floatation system and the tail gas treatment system have the characteristics of electric flocculation, electric floatation and electrochemistry, can remove various impurities in oily wastewater at one time, can simultaneously realize the functions of electric flocculation water distribution and air distribution by the jet flow aeration water distribution system, realizes water distribution without dead angles, improves the electric transmission efficiency, reduces the tail gas treatment pressure and avoids potential safety hazards.
Drawings
FIG. 1 is a schematic view of the overall structure of an embodiment of the present invention, which discloses a jet gas distribution and water distribution type oilfield wastewater electrocoagulation treatment system;
FIG. 2 is a schematic view of a connection structure of an electric flocculation system and a jet aeration water distribution system disclosed in an embodiment of the present invention;
fig. 3 is a schematic side view of an electric flocculation system according to an embodiment of the present invention;
fig. 4 is a schematic structural diagram of a self-oscillating jet mixer according to an embodiment of the present invention;
fig. 5 and fig. 6 are schematic diagrams of the arrangement of the jet nozzles according to two embodiments of the present invention.
In the drawings, the correspondence between each component and the reference numeral is:
1. an air flotation system, 11, an air flotation tank, 12, an air flotation slag scraping machine, 13, a pressure container tank, 14, a container pressure pump, 15, a slag collecting tank, 16, a pressure gauge, 17, an air release valve, 18, a water outlet valve, 19, an air guide pipe, 2, a homogeneity adjusting system, 21, a PH adjusting tank, 22, an acid-alkali liquid storage tank, 23, a PH on-line monitor, 24, a TDs detector, 25, an electrolyte storage tank, 3, an electric flocculation system, 31, a power supply, 32, an anode plate, 33, a cathode plate, 34, a slag scraping machine, 35, a conical slag collecting tank, 36, a flocculation reaction tank, 37, a slag flowing pipe, 38, a sludge pump, 39, a slag collecting tank, 4, a jet aeration water distribution system, 41, a self-excited oscillation jet mixer, 411, a fluid driving nozzle, 412, an air suction pipe, 413, a gas mixing chamber, 414, a self-excited oscillation chamber, 415, a collision wall, 416, a diffusion pipe, 42, 43, a water inlet pipeline, 45. gas-liquid outgoing pipeline, 46 fan pipe, 47 jet nozzle, 48 nozzle connecting pipeline, 5 tail gas treatment system, 51 gas collecting hood, 52 induced air pipe, 53 electric valve, 54 combustion tower.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
The invention is described in further detail below with reference to the accompanying drawings:
as shown in figure 1 and figure 2, according to the utility model provides a pair of efflux gas distribution water distribution formula oil field waste water electric flocculation processing system, include: the device comprises an air floatation system 1, a homogeneity adjusting system 2, an electric flocculation system 3, a jet aeration water distribution system 4 and a tail gas treatment system 5; the air floatation system 1 pumps the oily wastewater into an air floatation tank 11 at high pressure, scrapes off large pieces of oil flowers floating on the surface and conveys the oil flowers to a homogenizing regulation system 2; the homogeneity adjusting system 2 is used for monitoring and adjusting the pH value and the electrolyte concentration of the water body; the jet aeration water distribution system 4 carries out aeration treatment on the output water body of the homogenizing regulation system 2 to form gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electric flocculation system 3; the electric flocculation system 3 carries out electric flocculation reaction treatment on the water body, scum generated by the reaction is scraped, the part of waste gas generated by the reaction is introduced into the jet aeration water distribution system 4 for aeration treatment and the air floatation system 1 for providing pumping high pressure, and the rest part is treated by the tail gas treatment system 5.
In the embodiment, the jet flow nano aeration and electroflocculation combined process technology, the auxiliary air floatation system 1 and the tail gas treatment system 5 are adopted, the characteristics of electroflocculation, electroflotation and electrochemistry are achieved, various impurities in oily wastewater can be removed at one time, the jet flow aeration water distribution system 4 can achieve the functions of electroflocculation water distribution and air distribution, dead-angle-free water distribution is achieved, the electric transmission efficiency is improved, the tail gas treatment pressure is reduced through the tail gas treatment system 5, and potential safety hazards are avoided.
Specifically, the oily wastewater enters an air flotation system 1 to remove a large amount of oil stains. The sewage enters a homogenizing adjusting system 2 to adjust the pH value and the conductivity of the oily sewage. The homogenized sewage enters the electric flocculation system 3 through the jet aeration water distribution system 4, and the gas part introduced by the jet aeration water distribution system 4 is hydrogen generated by a negative plate of the device. And part of tail gas generated by the electric flocculation system 3 enters a tail gas treatment system 5 for treatment.
In the above embodiment, preferably, the air floatation system 1 includes an air floatation tank 11, an air floatation slag scraper 12, a pressure container tank 13, a container pressure pump 14 and a slag collection tank 15, the container pressure pump 14 pumps the oily wastewater into the pressure container tank 13, the pressure container tank 13 pumps high-pressure air through an air pump, and an air release valve 17 is connected to the air pump, so that the pressure container tank 13 conveys the oily wastewater to the air floatation tank 11, the oily wastewater forms large oil stains on the surface of the air floatation tank 11, and the air floatation slag scraper 12 scrapes the large oil stains to the slag collection tank 15.
Specifically, oily wastewater is pumped into a pressure container tank 13 by a container pressure pump 14, preferably, part of tail gas in the tail gas treatment system 5 is pressed into oily wastewater, the wastewater enters the air floatation tank 11 by a pressure reducing valve, at the moment, the pressed gas is released into micro bubbles, large oil flowers float on the surface of the air floatation tank 11 and are scraped into a residue collection tank 15 by an air floatation residue scraping machine 12, and preferably, the oily wastewater is conveyed to the residue collection tank by the residue collection tank 15 for uniform treatment. Preferably, a pressure gauge 16 is installed on the pressure vessel tank 13 for detecting the internal pressure. The oily wastewater treated by the air floatation system 1 is conveyed to the homogenization regulating system 2, and a water outlet valve 18 is arranged on the conveying pipeline.
In the above embodiment, preferably, the homogeneity adjusting system 2 includes a PH adjusting tank 21, an acid-alkali solution storage tank 22, an online PH monitor 23, a TDs detector 24, and an electrolyte storage tank 25, the oily wastewater treated by the air floatation system 1 is conveyed to the PH adjusting tank 21, the online PH monitor 23 and the TDs detector 24 are respectively used for detecting the PH value and the conductivity value in the solution of the water body in the PH adjusting tank 21, adjusting the PH value of the solution in the PH adjusting tank 21 through the acid-alkali solution storage tank 22, and adjusting the electrolyte concentration of the solution in the PH adjusting tank 21 through the electrolyte storage tank 25.
Specifically, the pH value of the solution in the pH adjusting tank 21 is controlled to be 5 to 7 when the anode plate 32 is an iron anode, and 6 to 8 when the anode plate 32 is an aluminum anode. And controlling the conductivity of the solution in the pH adjusting tank 21 to be more than 3000us/cm, and controlling the electrolyte storage tank 25 to add electrolytes such as NaCl and the like into the pH adjusting tank 21 when the conductivity is less than 3000us/cm, so that the conductivity of the solution reaches more than 3000 us/cm.
As shown in fig. 3, in the above embodiment, preferably, the electrocoagulation system 3 includes a power supply 31, an anode plate 32, a cathode plate 33, a flocculation reaction tank 36, a slag scraper 34, a conical slag collection tank 35, a slag pump 38 and a slag collection tank 39, the anode plate 32 and the cathode plate 33 are respectively connected with the anode and the cathode of the power supply 31, the anode plate 32 and the cathode plate 33 are respectively arranged in the flocculation reaction tank 36 at intervals in a staggered manner, the slag scraper 34 is arranged in the flocculation reaction tank 36, the slag scraper 34 is used for scraping scum on the liquid level of the flocculation reaction tank 36 into the conical slag collection tank 35, and the slag pump 38 pumps the slag in the conical slag collection tank 35 into the slag collection tank 39 through the slag flow pipe 37.
Specifically, sewage flows into the flocculation reaction tank 36 through the jet aeration water distribution system 4 to be processed by an electric flocculation reaction, sewage generates a flocculation structure through multiple flocculation reactions and simultaneously generates certain scum, the scum above the flocculation reaction tank 36 works by opening the scum scraping machine 34 after reaching a certain thickness, so that the scum on the liquid level is scraped into the conical scum collecting tank 35, the scum is separated from the liquid, a small amount of liquid falls into the conical scum collecting tank 3535 along with the scum, and after a certain unit time, the scum is pumped into the scum collecting tank 39 by opening the scum pump 38. Because a large amount of micro oxygen is exposed in the electrolysis process, the air flotation process has a good air flotation effect, an electrochemical oxidation reaction can be generated on the surface of the anode plate 32, and iron ions (or aluminum ions) generated by electrolysis and nascent hydrogen separated out from the cathode plate 33 have strong reducibility, so that the electrocoagulation process also has an oxidation-reduction function and certain degradation capability on organic matters so as to stay in sewage for a long time. And the water body after the electric flocculation reaction treatment continues to enter a subsequent treatment stage.
In the above embodiment, preferably, the jet aeration water distribution system 4 includes a self-oscillation jet mixer 41, a water pump 42, an induced draft fan 44, a gas-liquid exit pipeline 45 and jet nozzles 47, the water pump 42 pumps the water adjusted in the homogenization adjustment system 2 into the self-oscillation jet mixer 41 through a water inlet pipeline 43, the self-oscillation jet mixer 41 is communicated with the induced draft fan 44, an outlet of the self-oscillation jet mixer 41 is connected to the jet nozzles 47 through the gas-liquid exit pipeline 45, and the plurality of jet nozzles 47 are disposed at the bottom inside the flocculation reaction tank 36 of the electrocoagulation system 3.
As shown in fig. 4, in the above embodiment, preferably, the self-oscillating jet mixer 41 includes a fluid driving nozzle 411, an air suction pipe 412, an air mixing chamber 413, a self-oscillating chamber 414, an impact wall 415 and a diffuser 416, the fluid driving nozzle 411 is communicated with an outlet of the priming pump 42, the air mixing chamber 413 is arranged at an outlet of the fluid driving nozzle 411, an air suction pipe 412 is arranged on a side wall of the air mixing chamber 413 and is communicated with an outlet of the induced draft fan 44, the air suction pipe 412 sucks the gas and the oil-containing wastewater to form a gas-liquid mixed flow in the air mixing chamber 413, the self-oscillating chamber 414 is arranged at the outlet of the air mixing chamber 413, the impact wall 415 is formed inside the self-oscillating chamber 414, the gas-liquid mixed flow is self-oscillated and sheared to form a discrete vortex ring in the self-oscillating chamber 414 and generates a pressure oscillation wave by the impact wall 415, the outlet of the self-oscillating chamber, the gas-liquid mixture flow is ejected from the diffuser 416.
Specifically, the industrial wastewater is introduced into the self-oscillation jet mixer 41 by the water guide pump 42, is sprayed out through the fluid driving nozzle 411, negative pressure is formed in the gas mixing chamber 413, a part of tail gas of the tail gas treatment system 5 is sucked by the gas suction pipe 412, and the induced draft fan 44 plays a tail gas traction role. The gas-liquid mixed flow is disturbed in the self-oscillation chamber 414 by the vorticity within a certain frequency range, amplified in the self-oscillation chamber 414, forms a violent shear field by the self-oscillation action, forms a series of discrete vortex rings in the shear layer, and when the discrete vortex rings reach and interact with the collision wall 415, pressure oscillation waves are generated in the area near the collision wall 415, and the waves propagate upstream at the sound velocity, and induce new vorticity pulsation upstream. If the pressure pulsation of the separation area and the pressure pulsation of the collision area are opposite, a positive feedback circulation process of vortex disturbance-amplification-new vortex pulsation generation is formed, the process is repeated continuously, strong self-oscillation is formed in the cavity, after a certain circulation time, repeated and violent shearing is carried out on gas-liquid mixed liquid flowing through the self-oscillation cavity, the size of generated bubbles is reduced, and micron-sized bubbles are generated. The two-phase gas-liquid flow is ejected from the diffuser pipe 416 in a pulse form.
As shown in fig. 5 and fig. 6, specifically, the gas-liquid mixed flow is introduced into the electric flocculation system 3 through the gas-liquid outlet line 45, and is further distributed with gas and water through a plurality of jet nozzles 47. Preferably, a plurality of jet nozzles 47 are arranged around the bottom of the flocculation reaction tank 36 of the electric flocculation system 3 at a predetermined injection angle. Further preferably, the axial centerline of the jet nozzle 47 intersects the horizontal face downwardly at an angle of 30 to 150. Preferably, the jet nozzle 47 adopts a venturi throat structure, and 1 volume of gas-liquid mixed fluid ejected by the jet nozzle 47 can shear 4 times of volume of sewage and can drive 12 times of volume of sewage in the tank to stir. The combined arrangement of a plurality of jet nozzles 47 can further realize the uniformity of air and water distribution and improve the efficiency of the electric flocculation electrolyte.
Specifically, as shown in fig. 5, if the flocculation reaction tank 36 is circular, the gas-liquid exit pipeline 45 is also circular and surrounds the circumferential edge of the bottom in the circular flocculation reaction tank 36, the jet nozzles 47 are respectively and uniformly arranged on the gas-liquid exit pipeline 45 at preset intervals, because the anode plate 32 and the cathode plate 33 of the electric flocculation system 3 are also arranged at the bottom in the flocculation reaction tank 36, the anode plate 32 and the cathode plate 33 are arranged in the diameter direction along the circular flocculation reaction tank 36, the jet nozzles 47 are respectively arranged on the circumferences of the gas-liquid exit pipeline 45 at both sides of the diameter direction and both face the diameter direction, and the axial center line and the horizontal plane intersect downwards to form 30-150 degrees, so that the sewage in the flocculation reaction tank 36 can be sheared under the impact of the liquid column sprayed by the jet nozzles 47. Agitation and shearing of the fluid occurs primarily in the regions of the anode and cathode plates 32, 33 where the reaction is taking place, thereby increasing the efficiency of the electrocoagulation reaction.
As shown in fig. 6, if the flocculation reaction tank 36 is rectangular or square, the gas-liquid outlet pipeline 45 is also rectangular or square, and is disposed at the edge of the tank wall at the bottom in the flocculation reaction tank 36, the jet nozzles 47 are respectively and uniformly disposed on the gas-liquid outlet pipeline 45 at preset intervals, because the anode plate 32 and the cathode plate 33 of the electric flocculation system 3 are also disposed at the bottom in the flocculation reaction tank 36, the anode plate 32 and the cathode plate 33 are transversely disposed at the middle of the rectangular or square flocculation reaction tank 36, the jet nozzles 47 are respectively disposed on the gas-liquid outlet pipelines 45 at both sides of the anode plate 32 and the cathode plate 33, and both face the middle region direction, and the axial center line and the horizontal plane intersect downward to form 30-150 °, so that the sewage in the flocculation reaction tank 36 can be sheared under the impact of the liquid column ejected from the jet nozzles 47. The agitation and shearing of the fluid occurs mainly in the regions of the anode plate 32 and the cathode plate 33 where the reaction takes place in the middle, thereby increasing the efficiency of the electrocoagulation reaction.
In the above embodiment, preferably, the tail gas treatment system 5 includes a gas collecting hood 51, an air guiding pipe 52 and a combustion tower 54, the gas collecting hood 51 is hermetically covered on the flocculation reaction tank 36, one end of the air guiding pipe 52 is communicated with the inside of the gas collecting hood 51, and the other end is respectively connected to the jet aeration water distribution system 4 through a fan pipe 46 for aeration treatment, connected to the air flotation system 1 through an air guiding pipe 19 for providing pumping high pressure, and connected to the combustion tower 54 through an electric valve 53 for tail gas treatment.
In the above embodiment, preferably, when the air sources required by the jet aeration water distribution system 4 and the air floatation system 1 are insufficient and the air guiding pipe 52 is under negative pressure, the electric valve 53 is reversely opened to supplement the air sources to the jet aeration water distribution system 4 and the air floatation system 1, and when the air guiding pipe 52 is under positive pressure, the electric valve 53 is forwardly opened and the combustion tower 54 is opened to consume the remaining tail gas.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The utility model provides a efflux gas distribution water distribution formula oil field waste water electric flocculation processing system which characterized in that includes: the system comprises an air floatation system, a homogeneity adjusting system, an electric flocculation system, a jet aeration water distribution system and a tail gas treatment system;
the air floatation system pumps the oily wastewater into an air floatation tank at high pressure, and conveys a large amount of oil stains floating on the surface to the homogenizing adjusting system after scraping;
the homogeneous regulating system is used for monitoring and regulating the pH value and the electrolyte concentration of the water body;
the jet aeration water distribution system carries out aeration treatment on the output water body of the homogenizing regulation system to form a gas-liquid mixed flow, and the gas-liquid mixed flow is sprayed into the electric flocculation system;
the electric flocculation system carries out electric flocculation reaction treatment on the water body and scrapes scum generated by the reaction, part of waste gas generated by the reaction is introduced into the jet aeration water distribution system for aeration treatment and the air floatation system for providing pumping high pressure, and the rest part of the waste gas is treated by the tail gas treatment system.
2. The electric flocculation treatment system for oil field wastewater with jet air distribution and water distribution according to claim 1, wherein the air flotation system comprises the air flotation tank, an air flotation residue scraping machine, a pressure container tank, a container pressure pump and a residue collecting tank, the container pressure pump pumps the oily wastewater into the pressure container tank, the pressure container tank pumps high-pressure air through an air pump, so that the pressure container tank conveys the oily wastewater to the air flotation tank, the oily wastewater forms large oil stains on the surface of the air flotation tank, and the air flotation residue scraping machine scrapes the large oil stains to the residue collecting tank.
3. The electric flocculation treatment system for the jet air distribution and water distribution type oilfield wastewater of claim 1, wherein the homogeneity regulation system comprises a pH regulation tank, an acid-alkali solution storage tank, an online pH monitor, a TDs detector and an electrolyte storage tank, the oily wastewater treated by the air flotation system is conveyed into the pH regulation tank, the online pH monitor and the TDs detector are respectively used for detecting the pH value and the conductivity value in the solution of the water body in the pH regulation tank, the pH value of the solution in the pH regulation tank is regulated through the acid-alkali solution storage tank, and the electrolyte concentration of the solution in the pH regulation tank is regulated through the electrolyte storage tank.
4. The electric flocculation treatment system for jet gas distribution and water distribution type oilfield wastewater of claim 1, wherein the jet aeration and water distribution system comprises a self-oscillation jet mixer, a water diversion pump, an induced draft fan, a gas-liquid exit pipeline and jet nozzles, the water diversion pump pumps the water body after adjustment in the homogenization adjustment system into the self-oscillation jet mixer, the self-oscillation jet mixer is communicated with the induced draft fan, an outlet of the self-oscillation jet mixer is connected to the jet nozzles through the gas-liquid exit pipeline, and the jet nozzles are arranged at the bottom in a flocculation reaction tank of the electric flocculation system.
5. The electric flocculation treatment system for water distribution type oilfield wastewater with jet flow air distribution according to claim 4, wherein the self-oscillation jet mixer comprises a fluid-driven nozzle, an air suction pipe, a gas mixing chamber, a self-oscillation chamber, a collision wall and a diffusion pipe, the fluid-driven nozzle is communicated with an outlet of the water-induced pump, the gas mixing chamber is arranged at an outlet of the fluid-driven nozzle, the air suction pipe is arranged on a side wall of the gas mixing chamber and communicated with an outlet of the induced draft fan, the air sucked by the air suction pipe and the oily wastewater form a gas-liquid mixed flow in the gas mixing chamber, the self-oscillation chamber is arranged at an outlet of the gas mixing chamber, the collision wall is formed inside the self-oscillation chamber, the gas-liquid mixed flow forms a discrete vortex ring through self-oscillation shearing in the self-oscillation chamber, and pressure oscillation waves are generated under the action of the collision wall, the outlet of the self-oscillation chamber is communicated with the diffusion pipe, the diffusion pipe is communicated with the gas-liquid outgoing pipeline, and the gas-liquid mixed flow is sprayed out from the diffusion pipe.
6. The electric flocculation treatment system for the jet flow gas distribution water distribution type oil field wastewater according to claim 3, which comprises a power supply, an anode plate, a cathode plate, a flocculation reaction tank, a residue scraper, a conical residue collection tank, a sludge pump and a residue collection tank, wherein the anode plate and the cathode plate are respectively connected with the anode and the cathode of the power supply, the anode plate and the cathode plate are respectively arranged in the flocculation reaction tank in a staggered manner at intervals, the residue scraper is arranged in the flocculation reaction tank, the residue scraper is used for scraping scum on the liquid level of the flocculation reaction tank into the conical residue collection tank, and the sludge pump pumps the sludge in the conical residue collection tank into the residue collection tank.
7. The electric flocculation treatment system for jet gas distribution and water distribution type oilfield wastewater as claimed in claim 6, wherein the tail gas treatment system comprises a gas collecting hood, an air guiding pipe and a combustion tower, the gas collecting hood is sealed and arranged on the flocculation reaction tank, one end of the air guiding pipe is communicated with the inside of the gas collecting hood, the other end of the air guiding pipe is respectively connected to the jet aeration water distribution system for aeration treatment, the air guiding pipe is connected to the air floatation system for providing pumping high pressure, and the electric valve is communicated to the combustion tower for tail gas treatment.
8. The system of claim 7, wherein the electric valve is reversely opened to supplement air to the jet aeration water distribution system and the air floatation system when the air supply required by the jet aeration water distribution system and the air floatation system is insufficient and the air draft tube has negative pressure, and the combustion tower is opened to consume the residual tail gas when the air draft tube has positive pressure.
9. The electric flocculation treatment system for water distribution type oilfield wastewater through jet flow gas distribution according to claim 6, wherein the pH value of the solution in the pH adjusting tank is controlled to be 5-7 when the anode plate is an iron anode and 6-8 when the anode plate is an aluminum anode, and the electrolyte storage tank is controlled to add electrolyte into the pH adjusting tank so that the conductivity of the solution is above 3000 us/cm.
10. The electric flocculation treatment system for jet gas distribution and water distribution type oilfield wastewater of claim 4, wherein the axial center line of the jet nozzles and the horizontal surface are intersected downwards to form an angle of 30-150 degrees, and the plurality of jet nozzles are respectively arranged at the bottom of the flocculation reaction tank at a preset leading angle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921914241.1U CN211688633U (en) | 2019-11-07 | 2019-11-07 | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921914241.1U CN211688633U (en) | 2019-11-07 | 2019-11-07 | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211688633U true CN211688633U (en) | 2020-10-16 |
Family
ID=72786462
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921914241.1U Active CN211688633U (en) | 2019-11-07 | 2019-11-07 | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211688633U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110668621A (en) * | 2019-11-07 | 2020-01-10 | 辽阳博仕流体设备有限公司 | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater |
-
2019
- 2019-11-07 CN CN201921914241.1U patent/CN211688633U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110668621A (en) * | 2019-11-07 | 2020-01-10 | 辽阳博仕流体设备有限公司 | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8673129B2 (en) | High-throughput cavitation and electrocoagulation apparatus | |
| US20140116942A1 (en) | Air flotation and electrocoagulation system | |
| CN104888636A (en) | Micro-nano bubble generation device and sewage purification system | |
| WO2010107077A1 (en) | Microbubble generator, activated sludge aeration system, and ballast water sterilizing system | |
| CN104891616A (en) | Oily wastewater purification method and system | |
| CN103723867B (en) | A kind of economic benefits and social benefits air bearing algae blooms water processing equipment and its treatment process | |
| CN109485185A (en) | A kind of pulse electrochemical processing method and processing device of oil field operation waste liquid | |
| CN211688633U (en) | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater | |
| CN104341021A (en) | Progressive air floatation apparatus | |
| CN110668621A (en) | Jet gas distribution and water distribution type electric flocculation treatment system for oil field wastewater | |
| CN211999236U (en) | Ozone circulating tank and viscosity reduction device for reducing viscosity of oilfield chemical flooding produced water | |
| CN101327966A (en) | Heavy crude sewerage jet flow dissolved air flotation process | |
| CN218403755U (en) | Sludge thickening tank | |
| KR20200022960A (en) | Advanced treatment system having dissolved air floator using plasma ion gas | |
| CN111115923A (en) | Oily sewage treatment system and method based on electric flocculation technology | |
| CN110510710A (en) | Electric flocculation and electrocatalytic oxidation integrated waste-water treater | |
| CN212050667U (en) | Waste water treatment device | |
| CN212610122U (en) | Integrated activated sludge treatment device | |
| CN214114976U (en) | Microbubble air supporting machine | |
| CN111087106B (en) | Pretreatment process and treatment device for metal electroplating wastewater | |
| KR20010048040A (en) | Water processing method and apparatus for the same jointly using electro-coagulation and dissolved air flotation combined | |
| CN209835851U (en) | Waste cutting fluid purifying device | |
| CN204675880U (en) | A kind of split type microbubble aerating apparatus | |
| FI128091B (en) | Combiflotation for purification and disinfection of waste water | |
| CN216918882U (en) | Oily fluorescence waste water treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |