CN103787532A - System and method for reducing fluid chemical oxygen demand - Google Patents
System and method for reducing fluid chemical oxygen demand Download PDFInfo
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- CN103787532A CN103787532A CN201210433485.4A CN201210433485A CN103787532A CN 103787532 A CN103787532 A CN 103787532A CN 201210433485 A CN201210433485 A CN 201210433485A CN 103787532 A CN103787532 A CN 103787532A
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Abstract
The invention relates to a system and method for reducing fluid chemical oxygen demand. The system comprises an electrical separation unit and a chemical additive unit. The electrical separation unit can receive a first fluid to reduce the chemical oxygen demand and receive a second fluid so as to shift the chemical oxygen demand source removed from the first fluid out of the electrical separation unit and generate an effluent fluid. The chemical additive unit can input chemical additives into the effluent fluid so as to reduce the chemical oxygen demand of the effluent fluid.
Description
Technical field
The present invention relates to a kind of for reducing or reduce fluid chemistry oxygen requirement (Chemical Oxygen Demand, COD) system and method, relate in particular to a kind of electricity separation (Electrical Separation or Electrochemical Separation, E-separation) unit that utilizes and reduce the system and method for fluid chemistry oxygen requirement.
Background technology
Chemical oxygen demand (COD) typically refers to chemical oxygen demand (COD) source (or material) in fluid in treating processes, as the amount of the oxygen that consumes in its organic substance decomposing process or inorganics oxidising process.In industrial circle, a large amount of having compared with the waste water of high chemical oxygen demand is produced.Conventionally such waste water be not suitable for directly using in family or industry.In view of the finiteness of spendable water resources and to useless Water reuse and environment protection, the chemical oxygen demand (COD) that reduces this kind of fluid just seems particularly important.
There is multiple trial to reduce fluid chemistry oxygen requirement.Such as, utilize multiple treatment scheme, as Chemical Pretreatment (chemical pretreatment) and carry out biological restoration processing (biological remediation) or biological reinforced processing (bio-augmentation) reduces fluid chemistry oxygen requirement in active reactor.But these treatment schemees usually need the processing demands of more complicated, and processing efficiency is not high.Like this, just cause the increase of processing cost.In addition, also need the system of more complicated to complete these treatment schemees, this has just further increased processing cost.
So, a kind of new system and method that can be used to reduce fluid chemistry oxygen requirement need to be provided.
Summary of the invention
One embodiment of the present of invention provide a kind of system that reduces fluid chemistry oxygen requirement.This system bag electricity separating unit and chemical additive unit.Electricity separating unit can be accepted first fluid to reduce its chemical oxygen demand (COD) and receive second fluid so that the chemical oxygen demand (COD) source removing is shifted out to this electricity separating unit and produced effluent fluid from first fluid.Chemical additive can be inputted to reduce the chemical oxygen demand (COD) of this effluent fluid in chemical additive unit in described effluent fluid.
Another embodiment of the present invention provides a kind of system that reduces fluid chemistry oxygen requirement.This system comprises electric separating unit, precipitation unit and chemical additive unit.Electricity separating unit can be accepted first fluid to reduce its chemical oxygen demand (COD) and receive second fluid so that the chemical oxygen demand (COD) source removing is shifted out to this electricity separating unit and produced effluent fluid from first fluid.Precipitation unit and described electric separating unit fluid communication, with at the described effluent fluid that circulates between itself and described electric separating unit.Chemical additive can be inputted to reduce the chemical oxygen demand (COD) of this effluent fluid in chemical additive unit in described effluent fluid.
Inventive embodiment further provides a kind of method that reduces fluid chemistry oxygen requirement.The method comprise input first fluid in electric separating unit to reduce the chemical oxygen demand (COD) of this first fluid; Input second fluid shifts out this electricity separating unit and produces effluent fluid with a chemical oxygen demand (COD) source removing from first fluid in described electric separating unit; And input chemical additive to reduce the chemical oxygen demand (COD) of this effluent fluid in described effluent fluid.
Accompanying drawing explanation
Be described for embodiments of the invention in conjunction with the drawings, the present invention may be better understood, in the accompanying drawings:
Fig. 1 is the schematic diagram of the present invention for reducing an embodiment of the system of fluid chemistry oxygen requirement;
Fig. 2 is the schematic diagram that the present invention is provided with an embodiment of the system of pole-reversing electroosmosis (Electrodialysis Reverse, EDR) unit; And
Fig. 3 is the schematic diagram that the present invention is provided with an embodiment of the system of super capacitor desalination (Supercapacitor Desalination, SCD) unit.
Embodiment
Below will describe the specific embodiment of the present invention, and it is pointed out that in the specific descriptions process of these embodiments, in order to carry out brief and concise description, this specification sheets can not all be done detailed description to all features of actual embodiment.Should be understandable that; in the actual implementation process of any one embodiment; as in the process of any one engineering project or design item; in order to realize developer's objectives; in order to meet system restriction that be correlated with or that business is relevant; usually can make various concrete decision-makings, and this also can change to another kind of embodiment from a kind of embodiment.In addition, it will also be appreciated that, although the effort of having done in this performance history may be complicated and tediously long, but for those of ordinary skill in the art relevant to content disclosed by the invention, some designs of carrying out on the basis of the technology contents disclosing in the disclosure, the changes such as manufacture or production are conventional technique means, not should be understood to content of the present disclosure insufficient.
Unless otherwise defined, the technical term using in claims and specification sheets or scientific terminology should be has the ordinary meaning that the personage of general technical ability understands in the technical field of the invention." first ", " second " and the similar word that in patent application specification of the present invention and claims, use do not represent any order, quantity or importance, and are just used for distinguishing different integral parts.The similar words such as " one " or " one " do not represent quantity limitation, but represent to exist at least one." comprise " or " comprising " etc. similarly word mean to appear at " comprising " or " comprising " element above or object and contain and appear at element or object and the equivalent element thereof that " comprising " or " comprising " enumerate below, do not get rid of other elements or object." connection " or " being connected " etc., similar word was not defined in connection physics or machinery, was also not limited to directly or indirectly connected
Figure 1 shows that the schematic diagram of the present invention for reducing an embodiment of the system 10 of fluid chemistry oxygen requirement.As shown in Figure 1, system 10 is provided with electric separating unit (Electrical Separation Unit) 11 and the precipitation unit (Precipitation Unit) 12 with electric separating unit fluid communication.As mentioned above, " reduction chemical oxygen demand (COD) " can refer to reduce the amount of chemical oxygen demand (COD) source (or material) oxygen that consumes in fluid in embodiments of the present invention, to reduce in other words or removing fluids in chemical oxygen demand (COD) source (or material).This chemical oxygen demand (COD) source can refer to that convection cell consumes the contributive material of ability of the amount of oxygen, and it can comprise organism or other any suitable materials, as consumed the inorganics of oxygen in oxidising process.
In embodiments of the present invention, electric separating unit 11 can be used to receive the first fluid 13 that comes from first-class body source (not shown) and contain chemical oxygen demand (COD), to reduce the chemical oxygen demand (COD) of this first fluid 13.In other examples, first fluid 13 also can include many kinds of substance, and as salt or other impurity, like this, electric separating unit 11 can further be used for removing at least a portion salt in first fluid 13 so that it is carried out to desalting treatment.In non-limiting example, the material comprising in fluid 13 can comprise charged ion, such as magnesium ion (Mg
2+), calcium ion (Ca
2+), sodium ion (Na
+), chlorion (Cl
-) and other ions.In some applications, electric separating unit 11 can be used to remove at least a portion material in this first fluid 13 in the chemical oxygen demand (COD) that reduces first fluid 13.Like this, due to the processing of electric separating unit 11, compare with first fluid 13, the output fluid (product fluid) 14 that comes from this electricity separating unit 11 just contains chemical oxygen demand (COD) source and/or the charged ion of low concentration, as zwitterion.
In some applications, output fluid 14 also can be transfused in electric separating unit 11 or in other electric separating units again and be further processed.Effluent fluid 16 can be transfused in precipitation unit 12, to use as second fluid 15, thereby by passage 18 circulation between electric separating unit 11 and precipitation unit 12.
Along with the continuous circulation of fluid 15, material wherein or the concentration of other impurity continue to increase until it reaches capacity or super-saturated degree at fluid 15.Like this, in the time that saturated or over-saturation degree reach stagnation point, will there is deposited phenomenon.In certain embodiments, the exhaust fluid 19 that includes at least a portion effluent fluid 16 can be discharged by the discharge-channel (not mark) that is arranged at precipitation unit 12 bottoms.In addition, a certain amount of fluid replacement 20 can be transfused to into precipitation unit 12 so that the fluid in it is supplemented.In non-limiting example, fluid replacement 20 can be carried out with first fluid 13 fluid source of self similarity.
In this example, precipitation unit 12 can be a container, it is for holding second fluid 15(or effluent fluid 16) and it is inputted into electric separating unit 11, thereby the chemical oxygen demand (COD) source and/or the charged ion that from first fluid 13, remove are shifted out to electric separating unit 11.Certainly, in certain example, precipitation unit 12 also can be set, precipitation, precipitation unit 12 can be set such as not occurring in the process when reducing first fluid 13 chemical oxygen demand (COD).
As shown in Figure 2, in certain application, electric separating unit 11 can comprise pole-reversing electroosmosis (Electrodialysis Reversal, EDR) unit 21.Similar, electric separating unit 11 also can comprise electrodialysis cell.Because electrodialysis cell has similar structure with pole-reversing electroosmosis unit, for convenience of explanation, in the present embodiment, describe as an example of pole-reversing electroosmosis unit example.In some instances, " pole-reversing electroosmosis " can refer to, under galvanic current and regularly polarity reversal (Polarity Reversal) effect, utilize the anion and cation exchange membrane of alternative arrangement to remove the Electrochemical separation process of water or other fluid intermediate ions or other charge specieses.
In non-limiting example, pole-reversing electroosmosis unit 21 can arrange pair of electrodes, and it can use as anode and negative electrode respectively.A plurality of anion and cation exchange membranes that are arranged alternately (Anion and Cation Exchange Membranes) are arranged between anode and cathode to form a plurality of He Dan chambers, dense chamber that are arranged alternately.Anion and cation exchange membrane can allow respectively zwitterion to pass through.In addition, pole-reversing electroosmosis unit 21 is being provided with filter unit between every pair of film and between electrode and the film of vicinity.
In some applications, electrode can comprise can heat conduction or athermanous electro-conductive material, and it can comprise the particle with reduced size and larger surface-area.In some instances, electrode also can be titanium plate or is coated with the titanium plate of the precious metals such as platinum.In other examples, electro-conductive material can comprise one or more carbon materials.In non-limiting example, carbon material can comprise activated carbon particle (Activated Carbon Particles), porous carbon particle (Porous Carbon Particles), carbon fiber (Carbon Fibers), carbon aerosol (Carbon Aerogels), porous carbonaceous mesophase spherules (Porous Mesocarbon Microbeads) or its combination.At other example, electro-conductive material can comprise conducing composite material, as manganese, and iron, the oxide compound of manganese and iron, the carbide of titanium, zirconium, vanadium, tungsten or its combination.
Filter unit can comprise that any ion can pass through material (Ion-permeable), non-electronic conduction (Electronically Nonconductive), and this material can be the material of film and many skies or atresia.In non-limiting example, the material of anion-exchange membrane can comprise and contain cation group, such as the ionic polymer of the polystyrene skeleton structure of quaternary amine base (Quaternary Amine Group).The material of cationic exchange membrane can comprise and includes anionic group, such as the ionic polymer of polystyrene skeleton structure sulfonic group (Sulfonic Acid Groups) and/or carboxylic acid group (Carboxylic Acid Group).
Like this, in operation, when pole-reversing electroosmosis unit 21 is during in normal polarity state, electric current applies thereon, input fluid, as the first and second fluids 13,15 enter in the He Nong chamber, light chamber being arranged alternately accordingly along the first input channel 24,25 and by valve 22,23 respectively.
In light chamber, first fluid 13 is ionized, positively charged ion wherein by cationic exchange membrane towards movable cathode to enter in contiguous chamber; Negatively charged ion wherein moves to enter in other contiguous chambers towards anode by anion-exchange membrane.In the chamber (dense chamber) of the vicinity of each side of light chamber, even if electric field can apply certain tractive force to ion, positively charged ion can not move by anion-exchange membrane; Negatively charged ion can not move by cationic exchange membrane.Like this, zwitterion is just retained in corresponding dense chamber and concentration constantly increases.
Like this, second fluid 15 removes pole-reversing electroosmosis unit 21 with a concentrated zwitterion coming from the migration of light chamber by dense chamber, thereby output fluid 14 and effluent fluid 16 enter in corresponding the first output channel 28,29 via corresponding valve 26,27 respectively.To in light chamber, first fluid 13 to be carried out to desalting treatment similar, the Ye Congdan chamber, chemical oxygen demand (COD) source in first fluid 13 enters corresponding dense chamber.Like this, compared to the first and second fluids 13,15, output fluid 14 and effluent fluid 16 have respectively lower and higher chemical oxygen demand (COD).
In some examples, the polarity of the electrode of pole-reversing electroosmosis unit 21 has been reduced in the possibility that fouling occurs in this unit 21 since can reversing.Like this, under the state of falling the utmost point, original light chamber under normal polarity state becomes dense chamber to receive second fluid 15, and original dense chamber under normal polarity state just becomes light chamber and receives first fluid 13.Like this, in the time of operation, the first and second fluids 13,15 can enter in pole-reversing electroosmosis unit 21 and process along corresponding the second input channel 30,31.Output fluid 14 and effluent fluid 16 flow out pole-reversing electroosmosis unit 21 along the second output channel 32,33 respectively.In example of the present invention, electric separating unit 11 is not limited to any specific pole-reversing electroosmosis unit and processes fluid.
In other examples, as shown in Figure 3, electric separating unit 11 can comprise super capacitor desalination unit (Supercapacitor Desalination Unit, SCD) 34.So-called " super capacitor desalination unit " can refer to utilize capacitor cell (Supercapacitor) thus to seawater or other salt water carry out desalination or or deionize reduce salt in it or other ionized impurities amount to receivable level, so that family or industrial application.
In certain application, super capacitor desalination unit 34 conventionally can be by one or more super capacitor desalination monomer compositions.In non-limiting example, each super capacitor desalination monomer comprises pair of electrodes, separation screen device and is arranged on the collector in respective electrode.In the time that more than one super capacitor desalination monomer is superimposed, can between every pair of adjacent super capacitor desalination unit, corresponding electrical isolation separator be set.
In the present embodiment, electrode can comprise can heat conduction or athermanous electro-conductive material, and it can comprise the particle with reduced size and larger surface-area.In some instances, electrode also can be titanium plate or is coated with the titanium plate of the precious metals such as platinum.In other examples, electro-conductive material can comprise one or more carbon materials.
Collector can be set to tabular (Plate), netted (Mesh), paper tinsel shape (Foil) or sheet (Sheet), and it can be made up of metal or metal alloy.In non-limiting example, metal can comprise titanium, platinum, iridium or rhodium.In one example, metal alloy can comprise stainless steel.In other examples, collector also can comprise graphite (Graphite) or plastic material, as polyolefine (Polyolefin).In addition, the collector of plastic material can be mixed with conduction carbon black or metallic particles mix the electric conductivity that reaches certain.In some applications, collector can be connected with negative pole with the positive pole of power supply (not shown) respectively, and like this, pair of electrodes just can be used as anodal and negative pole respectively.
Separation screen device can comprise that any ion can pass through material (Ion-permeable), non-electronic conduction (Electronically Nonconductive), thereby adjacent pair of electrodes is kept apart.In non-limiting example, separation screen device can have or itself can be provided with space to form passage, thereby fluid can flow through between electrode pair by this passage.
In the embodiment shown in fig. 3, in the time that super capacitor desalination unit 34 is charged, be gathered in respectively on anode and negative electrode from the positive and negative charge of power supply.First fluid 13 is entered and in super capacitor desalination unit 34, is carried out desalination by valve 35.At this moment, the path that second fluid 15 enters super capacitor desalination unit 34 is closed by valve 35.Charged ion in first fluid 13 is adsorbed onto on corresponding electrode by positive and negative charge.Due to the gathering of charged ion on electrode, output fluid 14 can be thin out fluid (or product fluid), and it flows out super capacitor desalination unit 34 to use by valve 36.Compared to first fluid 13, the charge species that it contains low concentration.
In the time of electric discharge, the zwitterion being adsorbed in respective electrode departs from from the surface of electrode.Second fluid 15 enters super capacitor desalination unit 34 to shift out the ion removing from first fluid 13 from this super capacitor desalination unit 34 by valve 35.Effluent fluid 16 flows out super capacitor desalination unit 34 by valve 36.Compared to second fluid 15, in effluent fluid 16, contain material or other impurity of higher concentration.Now, the passage that first fluid 13 enters super capacitor desalination unit is closed by valve 35.
To in super capacitor desalination unit 34, first fluid 13 to be carried out to desalting treatment similar, in treating processes, chemical oxygen demand (COD) in first fluid 13 is reduced, meanwhile, concentrated in second fluid 15 from the chemical oxygen demand (COD) source in first fluid 13 and shifted out super capacitor desalination unit 34 to produce effluent fluid 16 by second fluid 15.Like this, compared to the first and second fluids 13,15, input fluid 14 and effluent fluid 16 have respectively lower and higher chemical oxygen demand (COD).
After 34 electric discharges of super capacitor desalination unit finish, then it can be used for preparing ensuing electric discharge in charging state for some time.This that is to say, electric discharge and the charging of super capacitor desalination unit 34 hocket, thereby have reduced chemical oxygen demand (COD) and/or the charged ion in first fluid 13 since the chemical oxygen demand (COD) source in first fluid 13 and/or charged ion are transferred in second fluid 17.
In other non-limiting examples, the super capacitor desalination unit being set together to stack is similar, collector that super capacitor desalination unit 34 can comprise pair of electrodes, contact with respective electrode, be arranged on the one or more bipolar electrodes between pair of electrodes and be arranged on every pair of adjacent interelectrode a plurality of filters unit, thereby process first fluid 13 and process second fluid 15 in discharge condition at charging unit.Each bipolar electrode is provided with positive pole and the negative side of being isolated by ionic isolation layer (Ion-impermeable Layer).U. S. application publication 20110024287 can be used as reference further the super capacitor desalination unit that is provided with bipolar electrode is described.
As mentioned above, effluent fluid 16 has higher chemical oxygen demand (COD).In the embodiment shown in Fig. 1-3, system 10 can further be provided with chemical additive unit 37, and it can be used for inputting chemical additive in effluent fluid 16, is used for reducing the chemical oxygen demand (COD) in this effluent fluid 16.In embodiments of the present invention, chemical additive unit 37 can be used as chemical additive source chemical additive is provided.Chemical additive can be added in effluent fluid 16 manually or automatically.
In non-limiting example, chemical additive can comprise condensing agent (Coagulant), oxygenant (Oxidant) or its combination.Condensing agent can comprise aluminium salt, as polymerize aluminum chloride (Polyaluminum Chloride) and molysite, as ferric sulfate (Ferric Sulfate), iron(ic) chloride (Ferric Chloride) and ferrous sulfate (Ferrous Sulfate).Oxygenant can comprise hypochlorite (Hypochlorite Salts), as clorox (Sodium Hypochlorite) and Losantin (Calcium Hypochlorite) and ozone (Ozone) and hydrogen peroxide (Hydrogen Peroxide).In a non-limiting example, chemical additive can be clorox.
In the present embodiment, chemical additive unit 37 can be used for chemical additive input in precipitation unit 12 to reduce the chemical oxygen demand (COD) of the effluent fluid 16 in precipitation unit 12.In other examples, chemical additive also can be transfused in effluent fluid 16 or be imported in exhaust fluid 19 to reduce the chemical oxygen demand (COD) of this exhaust fluid 19, so that it discharges by discharge-channel before effluent fluid 16 enters precipitation unit 12.In certain application, precipitation unit 12 also can be set, like this, chemical additive also can be transfused to into effluent fluid 16 is recycled in the passage 18 of electric separating unit 11.
In certain embodiments, in to the treating processes of first fluid 13, the salt in effluent fluid 16 or other contamination precipitations until its saturation ratio or over-saturation degree just can occur while reaching relatively high level.Therefore, in some instances, seed particles (Seed Particles) can be added in precipitation unit 12 and precipitate under relatively low concentration with the salt or other impurity that contain in inducing fluid.Seed particles can comprise solid particulate, and it includes but not limited to calcium sulfate particle or its hydroxide particles.At least a portion throw out can be used as exhaust fluid 19 and discharges by discharge-channel.
Below for reducing the non-limiting example of the chemical oxygen demand (COD) in first fluid 13 and effluent fluid 16.
Example 1
In this is schematically tested, use the pole-reversing electroosmosis unit shown in Fig. 2.This pole-reversing electroosmosis unit includes two electric power classifications, and each electric power classification comprises the hydraulic classification of two fluid communication, and these four hydraulic classification series connection arrange.Like this, the first and second fluids 13,15 can be exported fluid 14 and effluent fluid 16 by four hydraulic classifications to produce respectively successively.In this pole-reversing electroosmosis unit, each hydraulic classification is provided with five pairs of ion-exchange membranees.Two power supplys are provided for being electrically connected respectively with each electric power classification.
In experiment, experiment condition can comprise that the voltage in the each electric power classification being applied in pole-reversing electroosmosis unit is roughly 7 volts; The utmost point is once for each 1000 seconds of this pole-reversing electroosmosis unit; The flow velocity of first fluid 13 is roughly 0.5 liter/per minute; Effluent fluid 16 be recycled in precipitation unit 12 to use as second fluid 15; The calcium sulfate particle of about 300 grams is added in precipitation unit 12 as seed particles, and like this, the starting point concentration of the calcium sulfate in precipitation unit 12 is approximately 10wt%(wt%: weight percent).Certainly, as mentioned above, in certain application, precipitation unit 12 also can not arrange.
In operation, first fluid 13, output (or desalination) fluid 14 and outflow (or concentrated) fluid 16 are sampled and analyzed.Table one is depicted as the characteristic of first fluid 13, output fluid 14 and the effluent fluid 16 of sampling gained.
Table one:
| Sample | First fluid | Desalination fluid | Concentrated fluid |
| Specific conductivity (μ S/cm) | 4650 | 490 | 22600 |
| PH value | 6.0 | 5.7 | 7.2 |
| Basicity (mg/l) | 67.2 | 28.4 | 598.8 |
| Chemical oxygen demand (COD) (mg/l) | 187.0 | 29.0 | 975.0 |
| Calcium ion Ca 2+(mg/l) | 267.1 | 6.1 | 1387.1 |
| Potassium ion K +(mg/l) | 36.9 | 1.7 | 242.8 |
| Magnesium ion Mg 2+(mg/l) | 78.5 | 2.5 | 647.5 |
| Sodium ion Na +(mg/l) | 590.7 | 73.4 | 3258.1 |
| Chlorion Cl -(mg/l) | 663.1 | 80.0 | 4174.1 |
| Sulfate ion SO 4 2-(mg/l) | 932 | 35.6 | 4674.9 |
As shown in Table 1, this pole-reversing electroosmosis unit can effectively remove the charged ion in first fluid 13, thereby compared to first fluid 13 and second fluid 15, output fluid 14 and effluent fluid 16 just have respectively lower and higher charged ion concentration.Meanwhile, this pole-reversing electroosmosis unit also effectively reduces the chemical oxygen demand (COD) of first fluid 13.As shown in Table 1, the initial chemical oxygen demand (COD) of first fluid 13 is 187.0 mg/litre (mg/l).Passing through after pole-reversing electroosmosis cell processing, the chemical oxygen demand (COD) of output (or desalination) fluid 14 is only 29 mg/litre, and the chemical oxygen demand (COD) that flows out (or concentrated) fluid 16 is 975 mg/litre.
Compared to first fluid 13, the per-cent that the chemical oxygen demand (COD) of output fluid 14 accounts for the initial chemical oxygen demand (COD) of first fluid 13 is less than 16%.That is to say, the initial chemical oxygen demand (COD) that exceedes 84% first fluid 13 is removed or is reduced by pole-reversing electroosmosis unit.This shows the reduction of pole-reversing electroosmosis unit to chemical oxygen demand (COD) or removes to have beyond thought high-performance.In certain application, can proceed to process further to reduce its chemical oxygen demand (COD) to output fluid 14.
Example 2
In this experiment, use the pole-reversing electroosmosis unit shown in Fig. 2.This experiment has the experiment condition identical with above-mentioned example 1.Table two is depicted as the experimental result of utilizing chemical additive to process the chemical oxygen demand (COD) of effluent fluid 16.In operation, gather two samples of effluent fluid 16.The initial chemical oxygen demand (COD) of this effluent fluid 16 is 1300ppm.
Table two:
| Chemical additive | Dosage | Initial chemical oxygen demand (COD) | Chemical oxygen demand (COD) after treatment |
| Clorox | 1200ppm | 1300ppm | 121ppm |
| Polymerize aluminum chloride | 2000ppm | 1300ppm | 621ppm |
As shown in Table 2, in processing, approximately the clorox of 1200ppm and approximately the polymerize aluminum chloride of 2000ppm be added in the sample of corresponding effluent fluid 16 to reduce its chemical oxygen demand (COD).Visible, the chemical oxygen demand (COD) of effluent fluid 16 is effectively reduced.Using when clorox, the initial chemical oxygen demand (COD) 1300ppm of effluent fluid 16 is reduced to 121ppm especially, and it has dropped to the 1/10th also low of initial chemical oxygen demand (COD) 1300ppm.That is to say, exceed 90% initial chemical oxygen demand (COD) and be removed or reduce.This shows through pole-reversing electroosmosis unit, first fluid 13 to be processed with after chemical oxygen demand (COD) source is concentrated, and chemical additive has shown very high performance and reduced chemical oxygen demand (COD).
Example 3
In this experiment, use the pole-reversing electroosmosis unit shown in Fig. 2.This experiment has the experiment condition identical with above-mentioned example 2.Table three is depicted as the experimental result of utilizing chemical additive to process the chemical oxygen demand (COD) of effluent fluid 16.In operation, gather three samples of effluent fluid 16.The initial chemical oxygen demand (COD) of this effluent fluid 16 is 2048ppm.
Table three:
| Chemical additive | Dosage | Initial chemical oxygen demand (COD) | Chemical oxygen demand (COD) after treatment | Removal rate |
| Clorox | 500ppm | 2048ppm | 99ppm | 95% |
| Clorox | 1000ppm | 2048ppm | 121ppm | 94% |
| Clorox | 1500ppm | 2048ppm | 51ppm | 98% |
As shown in Table 3, in processing, the clorox of various dose is added in three samples of effluent fluid 16.Visible, the chemical oxygen demand (COD) of effluent fluid 16 obtains effectively and significantly reduces.For the clorox of corresponding dosage, the removal rate in chemical oxygen demand (COD) source is up to 95%, 94% and 98%.This shows through pole-reversing electroosmosis unit, first fluid 13 to be processed with after chemical oxygen demand (COD) source is concentrated again, and chemical additive has shown very high performance and reduced chemical oxygen demand (COD).
Comparative example 1
Conventionally, to industry those of ordinary skill, utilize chemical additive, such as chemical oxidizing agent can part reduction fluid, as the chemical oxygen demand (COD) of first fluid 13, but it is lower that this kind utilizes chemical additive to reduce the removal rate of mode of chemical oxygen demand (COD), and need heavy dose of chemical additive.Table four is depicted as at fluid, the result of utilizing chemical additive to process its chemical oxygen demand (COD) before without pole-reversing electroosmosis cell processing as first fluid 13.In processing, gather two samples of first fluid 13, its initial chemical oxygen demand (COD) is 173ppm.
Table four:
| Chemical additive | Dosage | Initial chemical oxygen demand (COD) | Chemical oxygen demand (COD) after treatment | Removal rate |
| Clorox | 500ppm | 173ppm | 54ppm | 69% |
| Clorox | 1000ppm | 173ppm | 41ppm | 76% |
As shown in Table 4, in this comparative example 1, corresponding to the clorox of various dose, when first fluid 13 is during without pole-reversing electroosmosis cell processing, the removal rate in the chemical oxygen demand (COD) source of first fluid 13 is 69% and 76%.This that is to say, on average needs 4.2ppm to reduce the chemical oxygen demand (COD) of 1ppm to the clorox of 7.6ppm.
But, in example 3, when first fluid 13 is processed through pole-reversing electroosmosis device, after chemical oxygen demand (COD) source is concentrated in effluent fluid 16, the clorox convection cell of dosage communicates, as the removal rate of the chemical oxygen demand (COD) of effluent fluid reaches 95% and 94%, 69% and 76% the removal rate in its chemical oxygen demand (COD) source apparently higher than the clorox of corresponding same dose in comparative example 1.This that is to say, in example 2 and 3, on average only needs 0.3ppm to reduce the chemical oxygen demand (COD) of 1ppm to the clorox of 1ppm.With respect on average needing 4.2ppm to reduce to the clorox of 7.6ppm for the chemical oxygen demand (COD) of 1ppm in comparative example 1, this experiment has beyond thought result, it has not only improved the removal rate in chemical oxygen demand (COD) source, and can significantly reduce processing cost.
Visible, in embodiments of the present invention, after the chemical oxygen demand (COD) source of first fluid 13 is concentrated in effluent fluid 16 by pole-reversing electroosmosis unit, utilize chemical additive, the removal rate in its chemical oxygen demand (COD) source is significantly improved.The poor efficiency producing compared to traditional industry librarian use chemical additive and expensive, the embodiment of the present invention has beyond thought high-performance to the reduction of chemical oxygen demand (COD).
In addition, compared to system or the flow process of traditional reduction chemical oxygen demand (COD), the embodiment of the present invention, except having beyond thought high-performance, also has relatively simple framework and flow process, and this also just shows that the embodiment of the present invention has the high performance lower cost that simultaneously also has.
Although describe the present invention in conjunction with the specific embodiments, those skilled in the art will appreciate that and can make many modifications and modification to the present invention.Therefore, recognize, the intention of claims is to cover all such modifications and the modification in true spirit of the present invention and scope.
Claims (21)
1. a system that reduces fluid chemistry oxygen requirement, comprising:
Electricity separating unit, it can accept first fluid to reduce its chemical oxygen demand (COD) and receive second fluid so that the chemical oxygen demand (COD) source removing is shifted out to this electricity separating unit and produced effluent fluid from first fluid; And
Chemical additive unit, it can input chemical additive to reduce the chemical oxygen demand (COD) of this effluent fluid in described effluent fluid.
2. system as claimed in claim 1, the concentration in the chemical oxygen demand (COD) source of wherein said effluent fluid is higher than the concentration in the chemical oxygen demand (COD) source in described second fluid.
3. system as claimed in claim 1, wherein said chemical additive can comprise aluminium salt, molysite, hypochlorite, ozone, hydrogen peroxide and combination thereof.
4. system as claimed in claim 3, wherein said chemical additive comprises clorox.
5. system as claimed in claim 1, further comprises and the precipitation unit of described electric separating unit fluid communication, and this precipitation unit is used in the described effluent fluid that circulates between itself and described electric separating unit.
6. system as claimed in claim 5, wherein said chemical additive unit can be to the chemical oxygen demand (COD) of inputting described chemical additive in described precipitation unit and reduce described effluent fluid.
7. system as claimed in claim 5, wherein said precipitation unit can be discharged exhaust fluid, and described chemical additive unit can reduce its chemical oxygen demand (COD) to inputting chemical additive in described exhaust fluid.
8. system as claimed in claim 1, wherein said electric separating unit comprises one or more in super capacitor desalination unit, pole-reversing electroosmosis unit and electrodialysis cell.
9. system as claimed in claim 8, wherein said electric separating unit comprises described pole-reversing electroosmosis unit.
10. system as claimed in claim 1, wherein said electric separating unit is the ion in removable this first fluid in the chemical oxygen demand (COD) that reduces described first fluid.
11. 1 kinds are reduced the system of fluid chemistry oxygen requirement, comprising:
Electricity separating unit, it can accept first fluid to reduce its chemical oxygen demand (COD) and receive second fluid so that the chemical oxygen demand (COD) source removing is shifted out to this electricity separating unit and produced effluent fluid from first fluid;
Precipitation unit, itself and described electric separating unit fluid communication, with at the described effluent fluid that circulates between itself and described electric separating unit; And
Chemical additive unit, it can input chemical additive to reduce the chemical oxygen demand (COD) of this effluent fluid in described effluent fluid.
12. systems as claimed in claim 11, wherein said chemical additive unit can be to the chemical oxygen demand (COD) of inputting described chemical additive in described precipitation unit and reduce described effluent fluid.
13. systems as claimed in claim 11, wherein said precipitation unit can be discharged exhaust fluid, and described chemical additive unit can reduce its chemical oxygen demand (COD) to inputting chemical additive in described exhaust fluid.
14. systems as claimed in claim 11, wherein said chemical additive can comprise aluminium salt, molysite, hypochlorite, ozone, hydrogen peroxide and combination thereof.
15. systems as claimed in claim 11, wherein said electric separating unit comprises pole-reversing electroosmosis unit.
16. 1 kinds are reduced the method for fluid chemistry oxygen requirement, comprising:
Input first fluid in electric separating unit to reduce the chemical oxygen demand (COD) of this first fluid;
Input second fluid shifts out this electricity separating unit and produces effluent fluid with a chemical oxygen demand (COD) source removing from first fluid in described electric separating unit; And
In described effluent fluid, input chemical additive to reduce the chemical oxygen demand (COD) of this effluent fluid.
17. methods as claimed in claim 16, wherein said chemical additive can comprise aluminium salt, molysite, hypochlorite, ozone, hydrogen peroxide and combination thereof.
18. methods as claimed in claim 16, wherein said chemical additive comprises clorox.
19. methods as claimed in claim 16, be further included in described electric separating unit and and the precipitation unit of this electricity separating unit fluid communication between the described effluent fluid that circulates.
20. methods as claimed in claim 19, wherein comprise in described precipitation unit and input described chemical additive to reduce the chemical oxygen demand (COD) of described effluent fluid to inputting chemical additive in described effluent fluid.
21. methods as claimed in claim 16,, wherein said electric separating unit comprises pole-reversing electroosmosis unit.
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| CN201210433485.4A CN103787532A (en) | 2012-11-02 | 2012-11-02 | System and method for reducing fluid chemical oxygen demand |
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| CN201210433485.4A CN103787532A (en) | 2012-11-02 | 2012-11-02 | System and method for reducing fluid chemical oxygen demand |
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