CN104787857A - Method for minimizing total dissolved solids in industrial wastewater and system thereof - Google Patents
Method for minimizing total dissolved solids in industrial wastewater and system thereof Download PDFInfo
- Publication number
- CN104787857A CN104787857A CN201410022152.1A CN201410022152A CN104787857A CN 104787857 A CN104787857 A CN 104787857A CN 201410022152 A CN201410022152 A CN 201410022152A CN 104787857 A CN104787857 A CN 104787857A
- Authority
- CN
- China
- Prior art keywords
- anode
- negative electrode
- electrode
- influent
- pairing
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4616—Power supply
- C02F2201/4617—DC only
Abstract
The invention relates to a system for minimizing total dissolved solids in industrial wastewater. The system comprises a DC power supply for powering an electrocoagulation system. The electrocoagulation system forms a serpentine flow of an incoming fluid between a series pairs of anodes and cathodes. When flowing away, the incoming fluid is immediately transferred into a dissolving water module. The dissolving water module also generates hydrogen bubble and oxygen bubble between the pairs of anodes and cathodes by the utilization of the DC power supply. The pairs of anodes and cathodes allow and guide the incoming fluid to be discharged into a second chamber containing a filtering medium. According to the implementation scheme of the invention, the system can be configured into one or more modules which can operate individually or can be combined to work, or can be refitted into existing systems, troughs, water channels or other containers. In addition, the module system can be manufactured temporarily and removed after used. The module system can realize low-cost upgrade in usage because the modules can be integrated into existing systems. Refitted systems can be widely applied to more different end users at remote locations in a feasible way.
Description
Technical field
The present invention relates to a kind of system of wastewater treatment, and more specifically, relating to for from the system by being used for extracting in wastewater streams that recirculation or release gets back in environment organic and inorganic total dissolved solidss.
Background technology
The cleaning water of price material benefit becomes the urgent technical problem that the whole world faces day by day, to 2025, has two people to live in water-deficient area according to estimates in every three people.Along with the growth of world population, for needing the demand of the goods produced with water also in growth, wherein estimate that the water being used for industrial application shortly will exceed human's demand.At present in some areas, just experiencing the huge shortage that arid causes, the waste wherein for this precious resources is under control now, and is applied with pressure to process to industrial sector and their waste water of recirculation.
Along with safety of America passing through at calendar year 2001 Drinking Water Act, total organic compound (TOC) analyzes the scheme fast and accurately having become an assessment water pollutant, with alternative classics but very long biological oxygen demand (BOD) and chemical oxygen demand (COD) (COD) test.
The total dissolved solidss (TDS) of industrial output water usually containing high density, its composition is made up of hydrocarbon, iron, sulfide, vitriol, calcium, magnesium, sodium, muriate and supercarbonate pollutent.High TDS may be maximum in recycling processing process and the most troublesome difficult problem, mainly owing to being dissolved in the charged moving iron in given volume water, wherein TDS can with after purification receive the water purity of water or water quality directly related.Briefly, TDS can be regarded as any material be present in except pure H2O molecule in water.
Number of chemical mixture can be touched or through multiple process, this causes a difficult problem in the recirculation suitability of water due to trade effluent.A factor of impact process is chemical unbalanced elimination and correction.
For example, from the oil well produced water on missile silo stratum when being back to earth's surface during the extraction stage, usually containing hydrocarbon, the distinctive chemical in stratum (salt, mineral substance) and in order to strengthen other composition that leaching process may add.The physical property of recovered water and chemical property may according to geographical position, geologic framework and extract the type of hydrocarbon product and noticeable change.High TDS level not only brings challenges to method for recycling, and high TDS may make extracted end product souring.
Owing to setting up new regulation and system about wastewater treatment, now more control is being applied with to final user, thus is implementing when possibility the new technology that preferred method for recycling is provided.
Although there are multiple technologies to be used to Industrial Wastewater Treatment at present, there is various cost height and immovable problem in these systems most.Such as, may be extremely expensive by the water treatment system that new improvement opportunity replaces old deficiency, and in addition, because many water treatment applications are positioned at remote position, so not always economical or feasible.By the present invention, these and other difficult problem will be resolved at least partly.
Summary of the invention
The object of the invention is to solve above-mentioned deficiency of the prior art, a kind of system for reducing the total dissolved solidss in trade effluent is provided.
The technical scheme realizing the object of the invention is:
A kind of system for reducing total dissolved solidss in trade effluent, first it comprises is the DC power supply of electrocoagulation system power supply, described electrocoagulation system forms the serpentine flow of influent between a series of anode and negative electrode pairing, and then be transferred to when this influent leaves in dissolved water module, described dissolved water module also utilizes DC power supply to produce bubble hydrogen and oxygen bubbles between anode and negative electrode pairing, anode and negative electrode pairing allow and guide influent to be discharged in connected second Room, and described second indoor have filtration medium.
The above-mentioned system for reducing total dissolved solidss in trade effluent, the anode of described electrocoagulation system and negative electrode are paired into the anode and negative electrode pairing that to be clipped between end cap one or more keeps apart, and described end cap allows fluid to enter or leave.
The above-mentioned system for reducing total dissolved solidss in trade effluent, be set to make influent leave enter lower a series of electrode pair before or before leaving described electrocoagulation system orientation flow through described electrode surface, namely assign the surface of right anode and cathode.
The above-mentioned system for reducing total dissolved solidss in trade effluent, described anode and negative electrode pairing, be made up of one or more groups electrode, described electrode is the cated metal of surface coated or organic materials.
The above-mentioned system for reducing total dissolved solidss in trade effluent, described anode and negative electrode pairing comprise at least one uncharged neutral electrode, described neutral electrode and described anode and cathode electrode electric isolution, described neutral electrode is between described anode and cathode electrode pairing.
Above-mentioned match 0.062 to 10 inch, interval placement between the two poles of the earth for the system anode and negative electrode reducing total dissolved solidss in trade effluent, and on each anode and negative electrode pairing the applied voltage of configuration 0.1 to 300V
The above-mentioned system for reducing total dissolved solidss in trade effluent, the container holding the described dissolved water module of anode and negative electrode pairing is configured to produce the micron bubble be made up of hydrogen and oxygen from described incoming fluid.
The above-mentioned system for reducing total dissolved solidss in trade effluent, described anode and cathode electrode pairing are made up of silk screen or perforation plate, to form the electrode grid that the flowing of restriction incoming fluid is discharged.
The above-mentioned system for reducing total dissolved solidss in trade effluent, what described anode and negative electrode pairing guided influent to flow into comprise filtration medium is arranged in described dissolved water modular container bottom and the second Room be connected.
Adjoin and a contaminant collecting room for opening with the dissolved water modular container described in the above-mentioned system for reducing total dissolved solidss in trade effluent, it is received and deposits the pollutent skimmed from the surface of described influent by raking system.
Above-mentioned contaminant collecting room, it is provided with the container for the pipeline vertically raised, and the pipeline of described vertical rising is used for influent to transfer to next dissolved water modular container from a dissolved water modular container.
Above-mentioned contaminant collecting room, the entrance for influent transfer to be positioned under filter media chamber and to be connected to filter media chamber, and the outlet of wherein said pipeline is connected to next modular container, and wherein said outlet is positioned on anode and negative electrode pairing; Fluid level in the last modular container of pipeline Altitude control of the rising of described outlet and the residence time; It is provided with the valve being positioned at described collecting chamber lower vessel portion section, for the total dissolved solidss pollutent collected by removal.
Comprise a Waste Water Treatment for system described above and collecting chamber described above, with influent connect a series of repeat to increase electrocoagulation unit and dissolved water modular container can be used for reducing from waste water or produced fluid or removing total dissolved solidss or total suspended solid.
A kind of final dissolved water modular container of DC power supply, it comprises anode and negative electrode pairing, comprises the second Room of filtration medium and hold the 3rd Room of a series of porous electrode pairing, and described a series of porous electrode pair configuration becomes to allow to form a series of snakelike internal path for receiving effluent fluid stream.
The final dissolved water modular container of above-mentioned system DC power supply, its adsorbable total dissolved solidss ion being positioned at effluent fluid, wherein said ion can be collected and be stored in described a series of porous electrode.
The final dissolved water modular container of above-mentioned system DC power supply, by reducing or executing D/C voltage remove described ion from described porous electrode oppositely outward.
The final dissolved water modular container of above-mentioned system DC power supply, described ion can be collected as fluid saline from described porous electrode, described fluid saline by disposal be attached to described dissolved water modular container the contaminant collecting that connects indoor.
The final dissolved water modular container of above-mentioned DC power supply, described ion collection system should not be limited to a module, wherein have second and the 3rd Room a series of dissolved water modules that repeat to increase can be used for clean from effluent fluid and collection of ions.
In view of some difficult problems in prior art, be provided in combined for multiple system the technology modules utilized in the process of common organic or inorganic material in process trade effluent, wherein TDS pollutent comprises dissimilar bipolarity molecular compound.By applying electric current to wastewater streams, the key of these molecular compounds is dissociated, the some different technological system of wherein associated working can provide an essential core process.
Embodiment of the present invention can be configured to and can to operate separately or in conjunction with one or more modules of work, or are retrofitted in existing system, groove, water channel or other container.In addition, these modular systems can manufacture temporarily and remove after a procedure, and wherein the use of modular system can realize the upgrading of low cost, because they can be incorporated in existing system.The system of repacking can be enable to be widely used in a practical manner be in the how different final users of remote location.
The present invention comprises one or more electrocoagulations (EC) system with the associated working of a series of dissolved water flotation (DWF) module, and described dissolved water flotation module combines the known media bed with organic or inorganic thing adsorptive power.Below these media bed anode and cathode being positioned at pairing, the influent entered wherein is forced first to enter media bed again by described pairing and transfer in next DWF module again.Once influent have passed through last the DWF module comprising adsorption medium, it just then directed and transfer to be equipped with the configuration of a series of active carbon electrode DWF module in allow capacitive deionization (CDI), this is a kind of technology used in for the terminal stage of fluid polishing.
In some respects, employ one or more groups electrode, such as anode and negative electrode match, but use with difference configuration and interval.When energized, described anode and/or negative electrode can make the TDS bipolarity molecular structure in wastewater streams that electricity cohesion altogether occurs.Meanwhile, the anode of dissolved water floatation process and/or negative electrode are used for producing the micron bubble be made up of bubble hydrogen and oxygen bubbles.Along with these micron bubbles rise in wastewater streams, they also adhere to the TDS throw out that is made up of organism and the molecular chaperones that dissociates and are risen on the surface for collection.
Is contaminant collecting groove between each DWF module, in described contaminant collecting groove raking system skimmed surface and deposition collected by pollutent for storage.Then collected pollutent can be discharged from receiving tank and dispose in the manager of environment approval.
Making after influent is exposed to dissolved water floatation process, then force it to pass and knownly have the media bed of chemical and metal adsorption ability, this auxiliary TDS removes process.These media bed can by activated carbon, clay, sand, rock, pH balance media or water pollutant from other known particular target in recycling processing process any to some type needed for sorbent material form.A series of independent dissolved water flotation module can comprise the known contaminant that dissimilar medium comprises in wastewater streams to allow particular target.This dielectric method is the efficiency that treating processes provides greater flexibility and Geng Gao.
Once influent is by being equipped with the final DWF module of filtration medium, just then it is transferred in final capacitive deionization (CDI) module, the any remaining TDS solute with electric value of described final capacitive deionization resume module, is wherein generally the electric field of about 0.8 to 1.5 volt by applying between two porous (being often carbon) electrode and from wastewater streams, adsorbs described TDS solute.Be in film to ring lower counter ion and be collected and be stored in porous electrode and once reach the ion adsorption capacity of electrode, just applied voltage can be reduced to zero or reverse, wherein only have little strong brine product stream to be released.Can estimate that this strong brine accounts for and always enter 25% of stream.
These and other feature and advantage of the present invention can comprise in certain embodiments of the invention and will become more obvious according to following explanation and claims, or by knowing in the practice of the invention as mentioned below.The present invention does not require that all favorable characteristics as herein described and all advantages are all included in each embodiment of the present invention.
Unless otherwise defined, otherwise all technical terms used herein all have understood identical implication usual with embodiment of the present invention those of ordinary skill in the field
The present invention has positive effect: (1) embodiment of the present invention can be configured to and can to operate separately or in conjunction with one or more modules of work, or are retrofitted in existing system, groove, water channel or other container; (2) modular system of the present invention can manufacture temporarily and remove after a procedure, and wherein the use of modular system can realize the upgrading of low cost, because they can be incorporated in existing system; (3) possesses mobility after repacking, the system of repacking can be enable to be widely used in a practical manner be in the more how dissimilar final user of remote location.
(4) do not use chemical reagent, can not secondary pollution be caused.
(5) instant onset, does not need the treatment time grown very much, effectively can save the treatment time.
(6) can increase flexibly or reduce module number, to adapt to the water treatment demand of different standards.
(7) do not need the Facilities serialized such as water tank or settling tank, effectively can save and take up an area space.
(8) power consumption is lower, and Energy Efficiency Ratio is higher.
(9) of many uses, be not only applicable to Industrial Wastewater Treatment, also can process polytype waste water, and can connect with the water treatment device of other types and use.
Accompanying drawing explanation
In order to make content of the present invention more easily be clearly understood, below according to specific embodiment also by reference to the accompanying drawings, the present invention is further detailed explanation, wherein
Fig. 1 relates in general to waste water schema and shows each step used needed for wastewater treatment of the present invention.
Fig. 2 shows electrocoagulation unit used in the present invention and the perspective of the water between a series of end cap, packing ring, positive plate, neutral plate and negative electrode schema.
Fig. 3 shows the perspective side elevation view of independent dissolved water flotation module and anode and the negative electrode pairing location relative to media adsorbs main body.
Fig. 4 shows the perspective top view had for influent electric storm dew and the preferred anodes of discharge and the independent dissolved water flotation module of cathode techniques.
Fig. 5 shows the perspective side elevation view of the contaminant collecting groove between each dissolved water flotation module, and wherein piping layout is used for transmitting influent between the modules.
How directed Fig. 6 shows and is arranged on the perspective side elevation view of CDI electrode in dissolved water flotation module and the influent of expection is flow through described system.
Fig. 7 shows the present invention for removing or reduce the analysis report of efficiency of total dissolved solidss and total suspended solid.
Embodiment
(embodiment 1)
See Fig. 1 ~ 7
At this, embodiment of the present invention are described with reference to the accompanying drawings.In the following description, be not described in detail to avoid fuzzy the present invention due to unnecessary details to well-known function or structure.
The present invention relates to a kind of method and apparatus, wherein comprising wastewater streams that is organic or inorganic substance has impact to ion-conductance value, and wherein dissociating of molecular compound occurs.Therefore, when use produce bubble hydrogen and the oxygen bubbles of micron size with the fluid of ion time, utilize outer execute electric field to increase anode and negative electrode match between phase boundary potential.This electric field uses the one or more DC power supplys being electrically connected to anode and cathode electrode pairing to produce.
More of the present invention in, electrode can comprise configure with horizontal or vertical position and the group be made up of porous or non-porous material, described electro-conductive material can have the coating be coated with on metallic rod, metal strip or metal sheet top.Other electrode can comprise opening, multiple perforation or superficial makings, as silk screen or perforation plate, which increases the edge of electrode, thus helps to promote to generate bubble hydrogen and oxygen bubbles.Electrode also can be separated to form internal path by the non-conducting material being used as isolator or fluid-tight.Plate electrode can comprise directed fluid openings to allow relatively large contact area, thus reduces the treatment time by allowing higher flow velocity in treating processes.In addition, the layout of these electrodes can realize and strengthen electrocoagulation and micron bubble generation.Such as, in some embodiments, can by anode and negative electrode pairing about 0.062 to 10 inch of placements in interval, thus configure be applied to the voltage of about 0.1 to the 300V in described pairing with initial fluid handling.In some embodiments, single modular system can comprise by the isolated a series of anode of a series of packing ring and space bar being called neutrals and negative electrode and therefore form following layout: end cap, packing ring, positive plate, packing ring, neutral plate, packing ring, negative plate, packing ring and end cap.
When using in bulk solutions, as at large container or when using in open water, multiple electrode pair can be placed to end-to-end or stacked up and down, and/or be positioned over the different depths place in described solution.This kind of configuration can be decreased through the time and increase bubble concentration.Such as, these system and methods can be used for using sun power as in the evaporation settling bowl of purifying pool water propulsion source.These systems can be further used in pond, river or ocean environment to extract them after oil or other pollutent overflow.
As described in Figure 1 influent by during present system some column processing of process.First influent is sent to system through feed-pipe 2, and influent is provided to volute chamber 4 by described feed-pipe 2.Mud, sand or other inflow particle are removed in similar centrifugal mode, and the fluid high-speed wherein entered rotates and eliminates more hyperbaric particle.Vortex systems makes the particle of suspension arrive the outward flange of fluid column, there, between the inner wall section being built into vortex container and outer wall section, powder collection occurs.
Vortex process can allow the chemical being collected in valuable mineral substance or the high value used in manufacture or leaching process in some cases, and the valve be positioned under volute chamber then allows the pollutent collected by discharge.May be valuable product in these pollutents, separate the by product that described product can be collected from other.
Still with reference to Fig. 1 and after vortex procedure, then influent is displaced through electrocoagulation (EC) system 6, wherein, the influent entered stands electrical contact so that condensation product formation is polluted in excitation, and bipolarity contaminant compound wherein starts molecular dissociation.Known coating applications to anode and negative electrode pairing can will be conducive to the extra electrochemical reaction of result with generation.Such as, the negative electrode being coated with ruthenium matched with the anode be made up of titanium can provide to the effluent liquid of going out and disinfect.If or use iron in some cases, then iron ion can be discharged in influent, and described iron ion is useful to the hydrocarbon pollutant eradicated in wastewater streams.
One leaves EC unit, flows into water and just flows in a series of dissolved water flotation (DWF) module 8 through feed-pipe, the hydrogen wherein gone out by the electrolysis of water and oxygen, and risen on the surface by the flocculation solute of suspension.Produce micron bubble by anode and negative electrode pairing (electrolysis) now, wherein execute bubble hydrogen and oxygen bubbles that anode under DC power supply and negative electrode pairing produce large volume outside.Along with these micron bubbles rise through fluid, they adhere to particles of solute, thus are risen on the surface.Repel and gathering bubble hydrogen that attractor system causes mixing with TDS solute, oxygen bubbles are formed, wherein solute density thickens from the teeth outwards, and this is by skimming for the raking system of contaminant collecting or remove to otherwise.Cleaner inflow water allows by anode and negative electrode pairing and discharges, wherein under described pairing, be provided with filter bed on effluent liquid vent pipe, described filter bed forms by meticulous sand, rock or activated carbon or for other known chemisorbed material that heavy metal and chemical pollutant are removed.One through filtration medium, and influent is just then transported in the second module through pipe, the DWF module wherein along a series of extra increase carrys out repetitive process.Once the effluent liquid of process leaves the DFW module 8 of described series, just then being transferred to comprises in the final DFW module 10 of a series of porous active carbon dioxide process carbon electrode, wherein guiding influent flows through the path between electrode with voltage, and wherein other bipolarity compound may escaping flotation and medium process is adsorbed and is stored, and effluent liquid leaves system through feed-pipe 12 afterwards.
Still with reference to Fig. 1, illustrate that the overview flow chart of each step of the present invention depends on the anode and cathode arrangement, material type used in the ion-exchange in the solution of ion, the electric charge of particles of solute caused during the electrode of wherein one or more release ions has neutralized TDS cohesion.The ion of these releases is therefore coalescent with colloidal materials, and described colloidal materials removes by skimming method from the teeth outwards.
In some applications, TDS density or type may exceed the ability of separate payment, therefore can utilize one or more electrocoagulation (EC) unit 6 and dissolved water flotation (DWF) module 8 and CDI module 10.
Fig. 2 shows the sectional view of electrocoagulation (EC) unit 6.EC unit receives the influent entered from vortex systems 4, and wherein EC unit is by two end caps, and end cap 1 and end cap 2 22 form, and these two end caps have the fluid inlet 2 for entering or the fluid outlet 24 for leaving respectively.End cap 1 and end cap 2 22 are further used for, by a series of nuts and bolt, a series of positive plate 18 and negative plate 20 and perimeter gasket 16 are clipped in appropriate location.Perimeter gasket 16 be further used for providing positive plate 18 and negative plate 20 match between electric isolution, by doing like this, provide anode and negative electrode match between the sealed insulation of internal path.
The influent entered between the described serial band electric pathway be made up of charged positive plate and negative plate back and forth through.The bipolarity compound formation pollutent condensation product that EC system incentive comprises in wastewater streams, wherein molecular dissociation starts.
Require that each anode and negative electrode pairing have at least one opening, described opening can be regarded as the inlet point of the influent entered or leave a little.Positive plate 18 and negative plate 20 are locked like this: make inlet point and leave some placement opposite each other, wherein force the fluid under pumping pressure between anode and negative electrode pairing.This practice allows fluid through the whole spacing anode and cathode surface, then leaves and enter next anode and negative electrode and match.Be provided for the residence time of electric storm dew in this method to allow TDS to condense or throw out formation.Such as, when powering to EC unit, anode and negative electrode pairing provide ion-transfer, thus neutralize the electric charge in the bipolarity solute of some types, thus initial TDS cohesion.
In figure 3, due to the repeated increase of the structure of module 8, each module of Fig. 3 and Fig. 4 describes and will only provide once, unless required other specific amendments for TDS results.Therefore, Fig. 3 shows the side-view of DWF module 8, and influent flows into described module from EC unit 6 through entrance 26, wherein allows streaming fluid 34 to accumulate between underpunch negative electrode base plate 30 and top anode grid system 28.Between perforation negative electrode base plate 30 and top grid 28, collect fluid along with in applying DC power supply process, form bubble hydrogen and oxygen bubbles 32, these bubbles rise on the surface.Along with these micron bubbles are advanced to surface, they start adhere in its road and promote solute throw out, define the condensation product formation or foam layer that are made up of the mixture of bubble and pollutent solute.
Once this foam layer thickens, just it can be skimmed from surface or floatingly select, and cleaner outflow water 34 starts to be discharged in meticulous rock, sand or chemical or metal absorbent 36, then leaves system by the outlet 38 be positioned under filtration medium.
In order to higher efficiency, place by tactic the formation that anode and cathode electrode (wherein they near each other) promote bubble hydrogen and oxygen bubbles in DWF module.Such as, in some embodiments, anode and cathode separation can be opened between about 0.1 inch and about 10 inches.Separate than changing according to the electroconductibility of the fluid with ion or the power limit between anode and negative electrode pairing needed for ion-transfer.Such as, the salinity in fluid or electroconductibility less, the gap requiring to be used between pairing that bubble hydrogen and oxygen bubbles generate is less.In some configurations, near single negative electrode, place two or more anodes can increase turbulent flow, thus produces the mixed effect strengthened, and this can help cohesion and promote solute pass surface and arrive on the surface.
In some embodiments, operating voltage and the amperage of about 1 to 300 volt can be applied, but may require that higher applied voltage is to compensate the resistance in solution in some applications.The voltage applied and the actual range of amperage can change according to the density of TDS solute and their relative electrical conductivity.When use be connected to the positive source of power supply and one or more anode in negative source and negative electrode pairing respectively time, the interface realizing them by a series of contact needed for DC power transmission or terminal connects.
In some cases, one or more anode and negative electrode pairing can have non-solid surface, as having the multiple perforation allowing fluid to pass through.Such as, grid can is made up or be configured to one or more anode and negative electrode pairing to allow fluid to pass through or to discharge of silk screen.In the configuration of these types, relatively large opening promotes flow velocity and potential larger electric interface between fluid and solute faster, thus the TDS producing higher degree is separated.
Under the negative plate of perforation, place the layer comprising the known chemical of meticulous sand or rock or other and metal absorbent, before leaving each module at effluent liquid, provide filtration.The present invention can utilize for cleaning from waste water and the natural or known sorbing material of any type of filtering contaminants in addition.Any known sorbing material can be utilized alone or in combination to realize pollutant removal, as usually visible metal, chemical, organic substance or inorganic substance in well, evaporation tank or trade effluent.
Such as, in a DWF module, meticulous RKB can be used prevent the more heavy contaminant throw out may escaping floatation process from transferring to and may comprise in the 2nd DWF module of sand layer.Described sand layer is used to filter out less throw out, thus prevents from transferring in the 3rd DWF module, and described 3rd DWF module may comprise for preventing the chemical of some types from transferring to activated carbon layer in four module.After each transfer, effluent liquid comprises less pollutent and this degree of final arrival: described effluent liquid can be used for recirculation to be got back in commercial run, or for irrigating, or after process in discharge winding border.
Fig. 4 shows the vertical view of the independent DWF module 8 with perforation negative electrode base plate 30.Perforation 31 in negative plate limits the rate of flow of fluid that leaves to provide the residence time for the throw out occurred between perforation negative electrode base plate 30 and anode grid 28.The flow velocity left is controlled by the per-cent of boring a hole in restriction negative electrode backplate surface.This TDS of being restricted to throw out provides the time by attaching to the bubble risen being escaped effluent liquid discharge.Further this process auxiliary by some types of ion of release generation when Coating is upper to pairing in addition, this can assist TDS solute coalescent before being thus lifted on the surface.
Fig. 5 shows a series of DWF module, the side-view of DWF module 1, DWF module 2 32, DWF module 3 38 and DWF module 4 44.Influent enters system by entrance 22 and starts to import in first in a series of DWF module.
Between each DWF module, use partition wall, described partition wall forms a series of contaminant collecting room, contaminant collecting room 1, contaminant collecting room 2 34 and contaminant collecting room 3 42.These intervals allow for the installation leaving space of internal duct 1, internal duct 2 36 and internal duct 3 40 further.Pipeline 1, internal duct 2 36 and internal duct 3 40 are for transfer to water in next DWF module and to regulate the water level in each DWF module further.Only just can transfer in next module after reaching water and heavily accumulating (head pressure), wherein before fluid transfer occurs, the vertical height of transfer pipeline opening requires it is the equal fluid height in last DWF module.The time length of fluid filled additionally provides the residence time of electric storm dew, and described electric storm dew allows pollutent throw out to be evacuated on the surface by bubble formation.Such as, water to be transferred to module 32 and the number of modules of this process needed for TDS process carrys out repetition from module 26 by pipeline 28.
In addition, make contaminant collecting room 1, a chamber wall of contaminant collecting room 2 34 and contaminant collecting room 3 42 reduces, to serve as the weir point of raking process and to allow the accumulation surface straw mats be made up of throw out collected and store for suitable disposal.Be positioned at the valve on the base plate plane of each collecting chamber, the pollutent collected in collecting chamber can be removed by valve.
* Fig. 6 shows one or more final DWF module 10, and it comprises porous conductive material electrode 1 for capacitive deionization (CDI) process and porous conductive material electrode 2 50.CDI process is considered as the multistage from initially entering fluid and remove a large amount of salt by the present invention, and be considered as to overall TDS remove extra auxiliary.Therefore Fig. 6 shows the DWF module 8 being equipped with active carbon electrode pairing, wherein with the water 34 of sodium-chlor ion between the electrode 48 and 50 of a series of oppositely charged.This allows electronegative ion to be adsorbed by anode 48, and the ion of positively charged is adsorbed by negative electrode 50.
Therefore for the industrial output water containing salt or metal or brackish water, once begin to pass the electrode path 52 of described series with the influent 34 of ion, salinity just reduces or metal collection just starts, because the salt ion may escaping any prior procedures is attracted in porous electrode now with other molecule with ion.
Fig. 7 shows the present invention for from the efficiency removing or reduce total dissolved solidss and total suspended solid in the fluid of ion.
Analytical results:
Analytical test is carried out to the brackish water produced during road construction project, wherein this matrix is processed to use press over system of the present invention (flow through method) to process.
The influent entered preparing process is expressed as " 1 & 2 of intaking " by analysis report, and " water outlet 1 & 2 " that leave system is the water after process:
Above explanation of the present invention clearly discloses the present invention and can change by many modes.This kind of change is not regarded as departing from scope of the present invention, and is regarded as being included by accompanying claims for the obvious all this kind of amendments of those of ordinary skill in the art yet.
Claims (18)
1. one kind for reducing the system of total dissolved solidss in trade effluent, first it comprises is the DC power supply of electrocoagulation system power supply, described electrocoagulation system forms the serpentine flow of influent between a series of anode and negative electrode pairing, and then be transferred to when this influent leaves in dissolved water module, described dissolved water module also utilizes DC power supply to produce bubble hydrogen and oxygen bubbles between anode and negative electrode pairing, anode and negative electrode pairing allow and guide influent to be discharged in connected second Room, and described second indoor have filtration medium.
2. the system for reducing total dissolved solidss in trade effluent according to claim 1, it is characterized in that: the anode of described electrocoagulation system and negative electrode are paired into the anode and negative electrode pairing that to be clipped between end cap one or more keeps apart, and described end cap allows fluid to enter or leave.
3. the system for reducing total dissolved solidss in trade effluent according to claim 2, it is characterized in that: be set to make influent leave enter lower a series of electrode pair before or before leaving described electrocoagulation system orientation flow through described electrode surface, namely assign the surface of right anode and cathode.
4. the system for reducing total dissolved solidss in trade effluent according to claim 3, is characterized in that: described anode and negative electrode pairing, be made up of one or more groups electrode, described electrode is the cated metal of surface coated or organic materials.
5. according to claim 4 for reducing the system of total dissolved solidss in trade effluent, it is characterized in that: described anode and negative electrode pairing comprise at least one uncharged neutral electrode, described neutral electrode and described anode and cathode electrode electric isolution, described neutral electrode is between described anode and cathode electrode pairing.
6. according to the arbitrary described system for reducing total dissolved solidss in trade effluent of claim 2 ~ 5, it is characterized in that: anode and negative electrode match 0.062 to 10 inch, interval placement between the two poles of the earth, and on each anode and negative electrode pairing the applied voltage of configuration 0.1 to 300V
7. the system for reducing total dissolved solidss in trade effluent according to claim 1, the container holding the described dissolved water module of anode and negative electrode pairing is configured to produce the micron bubble be made up of hydrogen and oxygen from described incoming fluid.
8. the system for reducing total dissolved solidss in trade effluent according to claim 4, is characterized in that: described anode and cathode electrode pairing are made up of silk screen or perforation plate, to form the electrode grid that the flowing of restriction incoming fluid is discharged.
9. as claimed in claim 8 for reducing the system of total dissolved solidss in trade effluent, it is characterized in that: what described anode and negative electrode pairing guided influent to flow into comprise filtration medium is arranged in described dissolved water modular container bottom and the second Room be connected.
10. adjoin with the dissolved water modular container described in the system for reducing total dissolved solidss in trade effluent according to claim 9 and a contaminant collecting room for opening, it is received and deposits the pollutent skimmed from the surface of described influent by raking system.
11. contaminant collecting rooms according to claim 10, it is provided with the container for the pipeline vertically raised, and the pipeline of described vertical rising is used for influent to transfer to next dissolved water modular container from a dissolved water modular container.
12. contaminant collecting rooms according to claim 11, entrance for influent transfer to be positioned under filter media chamber and to be connected to filter media chamber, the outlet of wherein said pipeline is connected to next modular container, and wherein said outlet is positioned on anode and negative electrode pairing; Fluid level in the last modular container of pipeline Altitude control of the rising of described outlet and the residence time; It is provided with the valve being positioned at described collecting chamber lower vessel portion section, for the total dissolved solidss pollutent collected by removal.
13. 1 kinds comprise as arbitrary in claim 1 ~ 9 as described in system and as arbitrary in claim 9 ~ 12 as described in the Waste Water Treatment of collecting chamber, with influent connect a series of repeat to increase electrocoagulation unit and dissolved water modular container can be used for reducing from waste water or produced fluid or removing total dissolved solidss or total suspended solid.
The final dissolved water modular container of 14. 1 kinds of DC power supplies, it comprises anode and negative electrode pairing, comprises the second Room of filtration medium and hold the 3rd Room of a series of porous electrode pairing, and described a series of porous electrode pair configuration becomes to allow to form a series of snakelike internal path for receiving effluent fluid stream.
The final dissolved water modular container of 15. system DC power supplies as claimed in claim 14, is characterized in that: its adsorbable total dissolved solidss ion being positioned at effluent fluid, wherein said ion can be collected and be stored in described a series of porous electrode.
The final dissolved water modular container of 16. system DC power supplies as claimed in claim 14, is characterized in that: by reducing or executing D/C voltage remove described ion from described porous electrode oppositely outward.
The final dissolved water modular container of 17. system DC power supplies as claimed in claim 14, it is characterized in that: described ion can be collected as fluid saline from described porous electrode, described fluid saline by disposal be attached to described dissolved water modular container the contaminant collecting that connects indoor.
The final dissolved water modular container of 18. DC power supplies according to claim 14, described ion collection system should not be limited to a module, wherein have second and the 3rd Room a series of dissolved water modules that repeat to increase can be used for clean from effluent fluid and collection of ions.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410022152.1A CN104787857A (en) | 2014-01-17 | 2014-01-17 | Method for minimizing total dissolved solids in industrial wastewater and system thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410022152.1A CN104787857A (en) | 2014-01-17 | 2014-01-17 | Method for minimizing total dissolved solids in industrial wastewater and system thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104787857A true CN104787857A (en) | 2015-07-22 |
Family
ID=53553109
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410022152.1A Pending CN104787857A (en) | 2014-01-17 | 2014-01-17 | Method for minimizing total dissolved solids in industrial wastewater and system thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104787857A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105274556A (en) * | 2015-11-09 | 2016-01-27 | 武汉科技大学 | Directional flow electrolysis technology |
| CN109052587A (en) * | 2017-06-13 | 2018-12-21 | 郭洪飞 | A kind of open capacitive deionization desalter |
| CN111908567A (en) * | 2019-05-08 | 2020-11-10 | 中国石油天然气集团有限公司 | Volume fracturing waste liquid electric flocculation destabilization separation treatment device and method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6346197B1 (en) * | 2000-01-28 | 2002-02-12 | Mckay Creek Technologies Ltd. | Water and wastewater treatment system and process for contaminant removal |
| CN1382638A (en) * | 2001-04-24 | 2002-12-04 | 中国科学院生态环境研究中心 | Process and equipment for quickly cleaning water and used water |
| CN2848826Y (en) * | 2005-05-24 | 2006-12-20 | 武汉大学 | Device for deepling purification of drinking water |
-
2014
- 2014-01-17 CN CN201410022152.1A patent/CN104787857A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6346197B1 (en) * | 2000-01-28 | 2002-02-12 | Mckay Creek Technologies Ltd. | Water and wastewater treatment system and process for contaminant removal |
| CN1382638A (en) * | 2001-04-24 | 2002-12-04 | 中国科学院生态环境研究中心 | Process and equipment for quickly cleaning water and used water |
| CN2848826Y (en) * | 2005-05-24 | 2006-12-20 | 武汉大学 | Device for deepling purification of drinking water |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105274556A (en) * | 2015-11-09 | 2016-01-27 | 武汉科技大学 | Directional flow electrolysis technology |
| CN105274556B (en) * | 2015-11-09 | 2017-12-08 | 武汉科技大学 | A kind of oriented flow electrolysis process |
| CN109052587A (en) * | 2017-06-13 | 2018-12-21 | 郭洪飞 | A kind of open capacitive deionization desalter |
| CN111908567A (en) * | 2019-05-08 | 2020-11-10 | 中国石油天然气集团有限公司 | Volume fracturing waste liquid electric flocculation destabilization separation treatment device and method |
| CN111908567B (en) * | 2019-05-08 | 2022-06-03 | 中国石油天然气集团有限公司 | Volume fracturing waste liquid electric flocculation destabilization separation treatment device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8460520B2 (en) | Electrochemical system and method for the treatment of water and wastewater | |
| US10329174B2 (en) | Apparatus and process for separation and selective recomposition of ions | |
| CN105399271B (en) | Oily phenol recycling and wastewater treatment regenerating unit and method in oil extraction waste water | |
| US10662087B2 (en) | Electrochemical system and method for the treatment of water and wastewater | |
| CN104478045A (en) | Efficient electrodialysis desalinizing device and method for coking wastewater | |
| CN103130363B (en) | Desalination system and desalination method | |
| CN101560030A (en) | Method for realizing resource utilization of copper-containing waste water by electrolysis-electrodialysis united technology | |
| CN101250013A (en) | Novel electrolysis air-float sewage water processing unit | |
| CN104787857A (en) | Method for minimizing total dissolved solids in industrial wastewater and system thereof | |
| CN108467140A (en) | A kind of coking wastewater combination desalinating process | |
| CN105236682A (en) | Treatment method and device for waste water containing greasy dirt | |
| US10287187B2 (en) | Microreactor and method for desalinating salt water | |
| CN105417845A (en) | Treating device and method for rubbish infiltration membrane concentrated solution | |
| CN207391164U (en) | A kind of oil field integrates waste liquid processing equipment | |
| CN1800041A (en) | Electrolystic sterilization apparatus for oil field affusion | |
| CN204619444U (en) | High salinity waste water flocculation sedimentation tank | |
| CN204434420U (en) | Process high concentrated organic wastewater RO concentrated solution equipment | |
| CN110776166A (en) | Advanced treatment method and device for oil extraction sewage in oil field | |
| CN206970371U (en) | A kind of casing processes sewage-treatment plant | |
| CN205151970U (en) | Processing system and industrial wastewater processing system of strong brine that reverse osmosis unit discharged | |
| US9896355B2 (en) | Method and apparatus for an expandable industrial waste water treatment system | |
| US20210171368A1 (en) | Waste Water Treatment Process | |
| CN106995250A (en) | A kind of casing processes sewage-treatment plant | |
| KR101415701B1 (en) | Electrolysis equiqment for sewage treatment | |
| CN211813884U (en) | Advanced treatment device for oil extraction sewage in oil field |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20150722 |