CN212425722U - Electrochemical phosphorus removal device - Google Patents
Electrochemical phosphorus removal device Download PDFInfo
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- CN212425722U CN212425722U CN202020807950.6U CN202020807950U CN212425722U CN 212425722 U CN212425722 U CN 212425722U CN 202020807950 U CN202020807950 U CN 202020807950U CN 212425722 U CN212425722 U CN 212425722U
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Abstract
The utility model discloses an electrochemical phosphorus removal device, which belongs to the technical field of environmental engineering sewage treatment, and the electrochemical phosphorus removal device of the utility model is provided with a reaction area and an electrolysis area in sequence, wherein the reaction area comprises a two-stage coagulation reaction tank which is separated by a baffle plate; the electrolysis zone comprises an accommodating tank, a water distribution zone, an electric connection electrode plate and an induction electrode plate, and the upper part of the accommodating tank is provided with an overflow tank. The utility model discloses a device reducible plate electrode passivation, sewage treatment back mud volume are little, equipment area is little, the utmost point water is than big, the treatment cost is low, can jointly use with current dephosphorization equipment, also is applicable to the preliminary treatment of high concentration phosphorus-containing sewage.
Description
Technical Field
The utility model belongs to the technical field of environmental engineering sewage treatment, specific phosphorus removal device who adopts electrochemical technology that says so.
Background
Phosphorus-containing wastewater generally exists in the surface treatment industry of mechanical parts, the pharmaceutical and chemical industry, the breeding and slaughtering industry, domestic sewage and the like, and the wastewater with excessive phosphorus is discharged into a water body, so that ecological deterioration phenomena such as water eutrophication, color change, red tide, fish death and the like are caused, and the method is a very serious environmental pollution source.
At present, the most common inorganic phosphorus wastewater treatment process in China comprises two types of phosphorus removal by a calcium method and phosphorus removal by an iron-based coagulant, the phosphorus removal process by the calcium method has the defects of large sludge amount, the pH value of effluent needs to be adjusted back by adding acid, the operation cost is increasingly improved, and the phosphorus removal is not thorough; the phosphorus removal of the iron-based polymer has strict requirements on the control of process parameters, has certain requirements on personal qualities of operators, and brings certain difficulty for the stable standard of the discharged water due to improper control of the process parameters, fluctuation of the concentration and the adding amount of the medicament and the like. The most common organic phosphorus wastewater treatment process is a combined process of a chemical oxidation method and a biochemical method. The chemical oxidation method has strict requirements on the control of process parameters and the dosage, if the chemical oxidation method is slightly improper, the oxidation is incomplete, organic phosphorus cannot be completely converted into orthophosphate, and the total phosphorus of the treatment result cannot reach the standard; while the independent biochemical method is not good for the organic phosphorus wastewater. In the current national sewage nano-tube discharge standard, the highest discharge concentration of phosphorus is 8mg/L, the concentration of inorganic phosphorus in sewage in the aluminum oxidation industry is generally up to more than 2000mg/L, but the highest concentration of phosphorus-containing wastewater which can be treated by the traditional process cannot exceed 200mg/L, so that the prior process for treating high-concentration phosphorus-containing wastewater has great difficulty in reaching the standard.
SUMMERY OF THE UTILITY MODEL
The utility model discloses to the mud volume that the phosphorus-containing sewage exists of handling among the prior art big, equipment area is big, the treatment cost is high, the phosphorus-containing sewage treatment of high concentration scheduling problem not up to standard, provide an adopt the device of electrochemistry technology processing inorganic phosphorus waste water of high concentration and organic phosphorus waste water of high concentration.
In order to realize the aim, the utility model provides an electrochemical phosphorus removal device, which comprises a water inlet and a water outlet, wherein a reaction area and an electrolysis area are sequentially arranged between the water inlet and the water outlet; the reaction zone comprises a primary coagulation reaction tank, a secondary coagulation reaction tank and a baffle plate, the primary coagulation reaction tank and the secondary coagulation reaction tank are separated by the baffle plate, the upper edge of the baffle plate is lower than the upper edge of the reaction zone tank body, and a water inlet is communicated with the primary coagulation reaction tank; the electrolytic area is provided with an accommodating tank, and electrode plates which are the same in distance and parallel to each other are arranged in the accommodating tank and comprise a power connection electrode plate and an induction electrode plate; the material of the electric electrode plate is selected from one or two of iron plate, aluminum plate and graphite, and the material of the induction electrode plate is iron plate or aluminum plate; a water distribution area is arranged below the electrode plate, and the secondary coagulation reaction tank is communicated with the water distribution area; the upper part of the holding tank is provided with an overflow trough, the overflow trough is provided with an overflow weir, sewage flows into the overflow trough through the overflow weir, and the overflow trough is communicated with the water outlet.
The electrolytic plate of the electrochemical phosphorus removal device adopts a multiple electrode connection method, namely, the electric connection electrode plate is respectively connected with the positive electrode and the negative electrode of a power supply, and the induction electrode plate is arranged in the middle and is not connected with electricity, so that the electrode plate can be conveniently replaced; meanwhile, all the polar plates are fixed by polar plate clamping grooves on two sides of the accommodating groove, the plate distance between the polar plates is ensured, the electrolytic short flow is avoided, the contact chance of pollutants in sewage and a high-concentration flocculating agent at the polar plates is increased, the flocculation precipitation is facilitated, and the electrolytic phosphorus removal efficiency is improved.
As a preferable measure of the utility model, the inner wall of the holding tank is provided with a polar plate clamping groove, and the polar plate is inserted into the polar plate clamping groove; two electric connection electrode plates on the outermost side of the electrode plates are respectively connected with the positive electrode and the negative electrode of the power supply, and the induction electrode plates are not connected with the electrodes, so that the electrode plates are convenient to disassemble and replace.
As the utility model discloses a preferred measure, above-mentioned overflow weir design is the profile of tooth, plate electrode top liquid layer evenly distributed, and the overflow is stable, avoids the bias current, helps sewage at electrolysis district evenly distributed and abundant electrolysis.
As the utility model discloses a preferred measure, above-mentioned water distribution district sets up the perforated pipe, and a plurality of apopores of evenly distributed on the perforated pipe, perforated pipe below set up the aeration pipe, and a plurality of ventholes of evenly distributed on the aeration pipe, aeration pipe and aeration mouth one are connected, the perforated pipe is in the top of aeration pipe, the perforated pipe passes through communicating pipe with second grade coagulation reaction tank and is connected, and water distribution district below sets up the mud collection groove, and the mud collection tank bottom sets up the mud pipe. The water distribution area adopts a mode of aeration and uniform mixing of the aeration pipes, so that the ion concentration of the solution near the polar plate and the concentration gradient of the bulk solution are reduced, the oxygen in the air enables ferrous ions to be quickly oxidized into ferric ions, and the flocculation dephosphorization capability is enhanced.
As the utility model discloses an optimal measure, above-mentioned one-level coagulation reaction tank sets up two and/or mechanical stirring device of aeration mouth, two aeration mouths are in the vertical below of water inlet, and second grade coagulation reaction tank sets up mechanical stirring device and/or aeration mouth, mechanical stirring device includes agitator motor and stirring rake, and the rational selection sewage mixing mode saves space, reduces equipment area.
As the preferred measure of the utility model, the bottom of the one-level coagulation reaction tank is provided with the first emptying pipe, and the bottom of the second-level coagulation reaction tank is provided with the second emptying pipe.
As a preferable measure of the present invention, the primary coagulation reaction tank is equipped with a drug adding system, the drug is selected from acid solution and alkali solution, the acid solution is selected from one of sulfuric acid, hydrochloric acid, ferric sulfate, nitric acid and phosphoric acid, and the alkali solution is selected from one of potassium hydroxide, calcium hydroxide and sodium hydroxide; the secondary coagulation reaction tank is provided with a dosing system, the medicament is selected from an oxidant, and the oxidant is selected from one of hydrogen peroxide, persulfate and sodium hypochlorite.
The distance between the electrode plates of the electrochemical phosphorus removal device is 1 cm-4 cm, and the current density of the electrode plates is 5mA/cm2～50mA/cm2The voltage between the polar plates is 0.1 v-5 v, the power supply is a high-frequency pulse direct current power supply, the pulse frequency is 5000-20000 Hz, the duty ratio is 10-100%, the aeration quantity of the first aeration opening is 20-40L/(L.min), and the aeration quantity of the second aeration opening is 5-15L/(L.min).
As a preferable measure of the utility model, the voltage between the polar plates is 1 v-3 v.
As the preferable measure of the utility model, the distance between the electrode plates is 1.5 cm-3 cm.
The utility model discloses an automatic source technique of falling utmost point of high frequency pulse because the polarity of the two poles of the earth changes frequently, has reduced "electrode polarization" and "negative pole passivation".
The utility model discloses can adopt the mode of multistage series connection to handle sewage, reach national sewage discharge standard until quality of water.
The electric flocculation dephosphorization process is suitable for the high-efficiency removal of industrial sewage such as high-turbidity industrial sewage, electroplating sewage, phosphating sewage, fluorine-containing sewage and the like. Compared with the traditional chemical method, the process has the advantages of high removal rate, small mud amount, simple and convenient operation and convenient realization of automatic control, and integrates current condensation, electric floatation and electrolytic oxidation-reduction. Electrolytic coagulation is the first generation of A1 under the action of current3+、Fe2+、Fe3+Aliovalent, then with OH in the liquid-The reaction takes place to produce high molecular hydroxyl polymer, thus having flocculation effect. If the liquid contains phosphate ions, iron ions or aluminum ions can react with the phosphate ions to generate insoluble substances, so that the aim of removing phosphorus is fulfilled. The electrolytic flotation means that a small amount of O is generated in water during electrolysis2And H2The micro bubbles have certain adsorption capacity and floating capacity, can adsorb pollutant flocculation generated in water and float to the water surface, and thus the effect of solid-liquid separation is achieved. The principle of electrolytic oxidation-reduction is that metal pollutants directly undergo oxidation-reduction reaction at an anode or a cathode, or Fe with strong reducibility generated by the anode2+Ions, so that organic matters or high-valence toxic metal ions in the sewage are reduced; OH free radicals generated in the electrolysis process have strong oxidizability and can be indiscriminately and directly reacted with organic pollutants in the sewage to degrade the organic pollutants into carbon dioxide and water.
The electrochemical Fenton treatment process based on the sacrificial anode method of the utility model is compared with the common chemical Fenton treatment process, and the electrochemical Fenton treatment process is carried out under the same hydrogen peroxide adding amountThe method has the characteristics of high treatment efficiency, high automation degree and short reaction time, and particularly has incomparable technical advantages in the field of pretreatment of high-concentration organic sewage. Which applies advanced oxidation technology to electrochemical system and continuously produces H at cathode2O2Fe in solution2+To OH and Fe under catalysis3+OH mineralization of organic phosphorus in solution, Fe3+Reduced to Fe at the cathode2+The catalytic reaction is continuously carried out, the mineralization degree of the organic matters is high, the energy consumption is relatively low, the iron ions can be continuously circulated, continuous addition of a medicament is not needed, and the generation of bottom mud is avoided.
In integrated wastewater discharge Standard GB8978-1996, established 1 month 1 2006, the primary standard for total phosphorus (in terms of P): the A standard is 0.5mg/L, and the B standard is 1.0 mg/L; the secondary standard is 3.0 mg/L; the tertiary standard was 5.0 mg/L.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses the stagnant water district is eliminated to the rational selection sewage mixing mode, reduces device area: the aeration port II is arranged in the primary coagulation reaction tank connected with the sewage water inlet, and is designed vertically below the water inlet in an aeration and uniform mixing mode, so that the quality of sewage flowing into the secondary coagulation reaction tank from the primary coagulation reaction tank through the baffle plate is ensured to be uniform, and the area of the sewage is smaller than that of a stirring device of a stirring paddle; the secondary coagulation reaction tank in the reaction zone adopts a stirring and mixing mode, so that the sewage is ensured to be uniformly discharged when flowing out from the lower part of the secondary coagulation tank; the sewage enters an electrolysis area uniformly and stably after two-stage coagulation reaction, and a dead water area is eliminated. The water distribution area adopts an aeration and uniform mixing mode that the aeration pipes are uniformly distributed with air outlets, so that the ion concentration of the solution near the polar plate and the concentration gradient of the bulk solution are reduced, the dissolved oxygen in water quickly oxidizes ferrous ions into ferric ions, and the flocculation dephosphorization capability is enhanced.
2. The utility model discloses an overflow weir of device of electrochemistry dephosphorization is the profile of tooth, and plate electrode top liquid layer evenly distributed, and the overflow is stable, avoids the bias current, helps sewage at electrolysis district evenly distributed and abundant electrolysis, improves the clearance of phosphorus in the phosphorus-containing sewage.
3. The device has compact arrangement design of all components, and the liquid is uniformly mixed by using an aeration mode, so that the equipment space is saved; the electric flocculation and the electric Fenton share one set of device, so that the occupied area of equipment is reduced by more than half compared with the traditional process, and the sludge amount per ton is also reduced by half compared with the traditional calcium dephosphorization process.
4. The utility model discloses a device of electrochemistry dephosphorization adopts response electric polar plate parallel arrangement, has increased the inter-plate spacing of negative and positive polar plate, has avoided the electrolysis short current, has increased the contact chance of the high concentration flocculating agent of pollutant and plate electrode department in the sewage, and the water ratio is 28m2：1m3The flocculation precipitation is facilitated, the electrolytic phosphorus removal efficiency is improved, the treatment capacity per hour is over 2.5 tons, and the sewage treatment capacity of a single device reaches 50 tons per day, so that the method is suitable for most surface treatment industries; in addition, the induction electrode plate is bipolar, namely a negative electrode is arranged on the surface close to the positive electrode, a positive electrode is arranged on the surface close to the negative electrode, and H is arranged on the cathode+Is reduced to H2Due to H+Consumption of OH-The concentration is increased, and metal ions and generated OH are generated due to small distance between the polar plates-The compound generated by the reaction is quickly flocculated into insoluble substance, OH by the flocculating substance generated by the anode-After the concentration has decreased, H is electrolyzed+Increased concentration and reduced to H2Due to OH produced-Or H+The reaction can be carried out in time, so that the pH value of the electrolytic zone can be kept relatively stable, and the electrolytic bath has the effect of removing various metal ions.
5. The utility model discloses an evenly distributed apopore on the perforated pipe in water distribution district, evenly distributed venthole on the aeration pipe, perforated pipe help the phosphorus-containing sewage misce bene in the top of aeration pipe, abundant electrolysis improves the clearance of phosphorus in the phosphorus-containing sewage.
6. The utility model discloses a device of electrochemistry dephosphorization in the plate electrode inserts the polar plate draw-in groove of holding tank inner wall, dismantle the change convenience.
7. The utility model discloses a device of electrochemistry dephosphorization handles sewage can adopt continuous type or intermittent type formula, according to the nimble operational mode of selecting of sewage condition, makes sewage play water quality of water reach national sewage discharge standard.
8. The utility model discloses an electrochemistry phosphorus removal device equipment is simple, degree of automation is high, easy operation, with low costs, operation are stable, save the cost of labor.
9. The maximum treatment concentration of the inorganic phosphorus-containing wastewater treated by the utility model can reach 3000mg/L, and the treatment efficiency is more than 30 times of that of the traditional process; the maximum treatment concentration of two-stage series connection can reach 8000mg/L, and the treatment efficiency is more than 40 times of that of the traditional process.
10. The maximum treatment concentration of the wastewater containing organic phosphorus treated by the utility model can reach 600mg/L, and the treatment efficiency is more than 30 times of that of the traditional process; the maximum treatment concentration of two-stage series connection can reach 8000mg/L, and the treatment efficiency is more than 160 times of that of the traditional process.
11. The utility model discloses an electrochemistry phosphorus removal device both had been suitable for and had used jointly with current dephosphorization equipment facility, also was applicable to the preliminary treatment of high concentration phosphorus-containing sewage.
12. The utility model discloses a high frequency pulse DC power supply technique because the polarity of the two poles of the earth changes frequently, has reduced "electrode polarization" and "negative pole passivation", improves the electrolytic efficiency, is favorable to the dissolution of soluble electrode and goes out the stability of water quality, reduces energy consumption and treatment cost, and ton water treatment cost is 1 ~ 3 yuan/ton water, for below 50% of traditional handicraft.
Drawings
Fig. 1 is a perspective view of an electrochemical phosphorus removal device of the present invention.
Fig. 2 is a front view of the electrochemical phosphorus removal device of the present invention.
FIG. 3 is a top view of the electrochemical phosphorus removal device shown in FIG. 2.
FIG. 4 is an enlarged view of a portion I of the electrochemical phosphorus removal device shown in FIG. 3.
FIG. 5 is a sectional view taken along the line A-A of the electrochemical phosphorus removal device shown in FIG. 3.
FIG. 6 is a sectional view taken along line B-B of the electrochemical phosphorus removal device shown in FIG. 3.
FIG. 7 is a left side view of an electrochemical phosphorus removal device shown in FIG. 2.
FIG. 8 is a right side view of an electrochemical phosphorus removal device shown in FIG. 2.
Description of reference numerals: 1-stirring motor, 2-binding post, 4-water outlet, 5-mud discharging pipe, 7-communicating pipe, 8-emptying pipe II, 9-water inlet, 10-induction electrode plate, 11-electric electrode plate, 13-overflow weir, 14-overflow groove, 15-holding tank, 16-water distribution area, 17-perforated pipe, 18-aeration pipe, 19-baffle plate, 20-primary coagulation reaction tank, 21-secondary coagulation reaction tank, 22-stirring paddle, 23-aeration port I, 24-aeration port II, 25-emptying pipe I, 26 pole plate clamping groove.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
On the contrary, the invention is intended to cover alternatives, modifications, equivalents and alternatives which may be included within the spirit and scope of the invention as defined by the appended claims. Furthermore, in order to provide a better understanding of the present invention to the public, certain specific details are set forth in the following detailed description of the invention. It will be apparent to those skilled in the art that the present invention may be practiced without these specific details.
The electrochemical phosphorus removal device shown in fig. 1-8 comprises a water inlet 9 and a water outlet 4, wherein a reaction zone and an electrolysis zone are sequentially arranged between the water inlet 9 and the water outlet 4; the reaction zone comprises a primary coagulation reaction tank 20, a secondary coagulation reaction tank 21 and a baffle plate 19, the primary coagulation reaction tank 20 and the secondary coagulation reaction tank 21 are separated by the baffle plate 19, the upper edge of the baffle plate 19 is lower than the upper edge of the reaction zone tank body, and sewage flows into the secondary coagulation reaction tank 21 from the primary coagulation reaction tank 20 through the baffle plate 19.
The lower part of the side wall of the primary coagulation reaction tank 20 is provided with a second aeration port 24, the second aeration port 24 is vertically below the water inlet 9, and the aeration mixing mode is adopted, so that the floor area of equipment is saved on one hand, and on the other hand, the uniform water quality of sewage flowing into the secondary coagulation reaction tank 21 from the baffle plate 19 is ensured. And a first emptying pipe 25 is arranged at the bottom of the first-stage coagulation reaction tank 20, and when the equipment stops running, solid-liquid waste in the tank body is emptied through the first emptying pipe 25.
Second grade coagulation reaction tank 21 sets up agitating unit, and this agitating unit includes agitator motor 1 and stirring rake 22, and second grade coagulation reaction tank 21 lateral wall lower part sets up communicating pipe 7, and sewage passes through communicating pipe 7 and flows into water distribution district 16, and second grade coagulation reaction tank 21's bottom sets up evacuation pipe two 8. The secondary coagulation reaction tank 21 is stirred and mixed by the stirring paddle 22, which is beneficial to the uniform water discharge when the sewage flows into the water distribution area 16 from the secondary coagulation reaction tank 21.
The water distribution area 16 is provided with a perforated pipe 17, the perforated pipe 17 is communicated with the communicating pipe 7, water outlet holes are uniformly distributed on the perforated pipe 17, an aeration pipe 18 is arranged below the perforated pipe 17, air outlet holes are uniformly distributed on the aeration pipe 18, the perforated pipe 17 is arranged above the aeration pipe 18 in the vertical direction, a sludge collection groove is arranged below the water distribution area 16, and a sludge discharge pipe 5 is arranged at the bottom of the sludge collection groove. The water distribution area 16 adopts an aeration and uniform mixing mode that air outlets are uniformly distributed on the aeration pipe 18, so that the ion concentration of the solution near the polar plate and the concentration gradient of the bulk solution are reduced, the oxygen in the air enables ferrous ions to be quickly oxidized into ferric ions, and the flocculation dephosphorization capability is enhanced.
The electrode plates are arranged in parallel at intervals at the upper part of the water distribution area 16 and comprise an electric electrode plate 11 and an induction electrode plate 10, wherein the electric electrode plate 11 is an electric electrode plate, the induction electrode plate 10 is an induction electrode plate, the electric electrode plate is an iron plate or an aluminum plate, and the electric electrode plate is provided with a binding post 2. The inner wall of the accommodating groove 15 is provided with a polar plate clamping groove 26, and the polar plate is inserted into the polar plate clamping groove 26, so that the polar plate is convenient to disassemble and replace. The utility model discloses an induction electric polar plate parallel arrangement has increased the inter-plate space of negative and positive polar plate, has avoided the electrolysis short current, has increased the contact chance of the high enriched flocculating agent of pollutant and plate electrode department in the sewage, and the utmost point water ratio is 28m2：1m3The flocculation precipitation is facilitated, the electrolytic phosphorus removal efficiency is improved, and the treatment capacity per hour is over 2.5 tons; in addition, the induction electrode plate is bipolar, which is beneficial to maintaining the relative stability of the pH value of the electrolysis area and is suitable for various typesThe metal ions have the removing effect.
The upper part of the accommodating groove 15 is provided with an overflow groove 14, the overflow groove 14 is provided with an overflow weir 13, the overflow weir 13 is in a tooth shape, sewage flows into the overflow groove 14 through the overflow weir 13, and the overflow groove 14 is communicated with the water outlet 4. The overflow weir 13 is designed to be in a tooth shape, so that liquid layers above the electrode plate are uniformly distributed, overflow is stable, bias flow is avoided, sufficient electrolysis of sewage is facilitated, and dead angles are prevented.
The primary coagulation reaction tank 20 is provided with a dosing system, and a medicament is selected from acid liquor and alkali liquor, wherein the acid liquor is selected from one or more of sulfuric acid, hydrochloric acid, ferric sulfate, nitric acid and phosphoric acid, and the alkali liquor is selected from one or more of soluble metal hydroxides; the secondary coagulation reaction tank 21 is provided with a dosing system, the medicament is selected from an oxidant, and the oxidant is selected from one or more of hydrogen peroxide, persulfate and sodium hypochlorite.
The concentration of hydrogen peroxide is 30%, and the volume ratio of sewage to hydrogen peroxide is 1000: 5 to 40.
The pH value of the sewage is adjusted to 3-9 by adding acid liquor or alkali liquor into the primary coagulation reaction tank.
The distance between the electrode plates is 1 cm-4 cm, and the current density of the electrode plates is 5mA/cm2～50mA/cm2The voltage between the polar plates is 0.1 v-5 v, the electrolysis time is 10 min-30 min, and the polar water ratio is 28m2：1m3The power supply is a high-frequency pulse direct-current power supply capable of automatically inverting the polarity, the pulse frequency is 5000-20000 Hz, the duty ratio is 10-100%, the aeration quantity of the first aeration opening 23 is 20-40L/(L.min), and the aeration quantity of the second aeration opening 24 is 5-15L/(L.min).
The utility model discloses a but high-frequency pulse direct current power supply technique of automatic pole-reversing because the polarity of the two poles often changes, has reduced "electrode polarization" and "negative pole passivation", improves the electrolytic efficiency, is favorable to the dissolving of soluble electrode and goes out the stability of water quality of water, reduces energy consumption and treatment cost, and ton water treatment cost is 1 ~ 3 yuan/ton water, for below 50% of traditional handicraft.
The utility model discloses an electrochemistry phosphorus removal device uses the principle of electric flocculation or the principle dephosphorization of electro fenton. When the electro-Fenton principle is used for dephosphorization, a dosing system is started, acid liquor and an oxidant are added, and when the electro-flocculation principle is used for treatment, alkali liquor is added.
The utility model discloses well one set of device of electricity flocculation and electro-fenton sharing compares traditional technology and reduces equipment area more than half, and ton water sludge volume also reduces half than traditional calcium method dephosphorization technology.
The following are several specific examples of the phosphorus removal by the electrochemical phosphorus removal device of the present invention:
example 1:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 2v, the electrolysis time of the sewage is 30min, and the polar water ratio is 28m2：1m3Current density of 50A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 5000Hz, the duty ratio is 10%, the aeration rate of the aeration port II 24 is 5L/(L.min), the aeration rate of the aeration port I23 is 20L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Introducing 256mg/L of phosphorized surface treatment sewage containing inorganic phosphorus (counted by P) into a primary coagulation reaction tank 20 through a water inlet 9 for uniformly aerating, introducing the uniformly aerated phosphorus-containing sewage into a secondary coagulation reaction tank 21, starting a dosing system, adjusting the pH value of the sewage to 8, and uniformly stirring; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plates from bottom to top, is electrolyzed by the electrode plates, flows into an overflow groove through an overflow weir after the electrolytic phosphorus removal, flows into a coagulating sedimentation device or an air floatation device through a water outlet 4 for solid-liquid separation and sampling detection after stable operation, the content of inorganic phosphorus (counted by P) in the effluent sewage is 0.5mg/L, and the total phosphorus discharge standard in the integrated wastewater discharge standard GB8978-1996 is reached.
Example 2:
the controlled process parameters are as follows: the space between the electrode plates is 1.5cm, the working voltage between the electrode plates is 1v, the electrolysis time is 10min, and the water-to-polar ratio is 28m2：1m3The power supply is a high-frequency pulse direct-current power supply with the current density of 100A/m2The pulse frequency is 20000Hz, the duty ratio is 100 percent, and the aeration quantity of the second aeration opening 24 is 10L/(L.min), the aeration quantity of the aeration port I23 is 40L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Introducing 256mg/L of phosphorized surface treatment sewage containing inorganic phosphorus (counted by P) into a primary coagulation reaction tank 20 through a water inlet 9 for uniformly aerating, introducing the uniformly aerated phosphorus-containing sewage into a secondary coagulation reaction tank 21, starting a dosing system, adjusting the pH value of the sewage to 8, and uniformly stirring; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electrolytic dephosphorization of the electrode plates flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air flotation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the content of inorganic phosphorus (counted by P) in the effluent sewage is 0.7mg/L, and the total phosphorus three-level discharge standard in the integrated wastewater discharge standard GB8978-1996 is reached.
Example 3:
the controlled process parameters are as follows: the space between the electrode plates is 4cm, the working voltage between the electrode plates is 3v, the electrolysis time is 20min, and the polar water ratio is 28m2：1m3The power supply is a high-frequency pulse direct-current power supply with the current density of 100A/m2The pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the aeration port II 24 is 15L/(L.min), the aeration rate of the aeration port I23 is 30L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 9.
Introducing 256mg/L of phosphorized surface treatment sewage containing inorganic phosphorus (counted by P) into a primary coagulation reaction tank 20 through a water inlet 9 for uniformly aerating, introducing the uniformly aerated phosphorus-containing sewage into a secondary coagulation reaction tank 21, starting a dosing system, adjusting the pH value of the sewage to 9, and uniformly stirring; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electrolytic dephosphorization of the electrode plates flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air flotation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, and the content of inorganic phosphorus (counted by P) in the effluent sewage is 5mg/L, thereby reaching the three-level total phosphorus discharge standard in the Integrated wastewater discharge Standard GB 8978-1996.
Example 4:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 2v, the electrolysis time of the sewage is 30min, and the polar water ratio is 28m2：1m3Current density of 50A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 5000Hz, the duty ratio is 10%, the aeration rate of the aeration port II 24 is 5L/(L.min), the aeration rate of the aeration port I23 is 20L/(L.min), the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 3, the concentration of the hydrogen peroxide in the added medicament is 30%, the flow rate of the hydrogen peroxide is adjusted, and the volume ratio of the sewage to the hydrogen peroxide is 1000: 5, adding hydrogen peroxide.
4061mg/L medical phosphorus-containing sewage (calculated by P) containing organic phosphorus enters a primary coagulation reaction tank 20 through a water inlet 9 for aeration and uniform mixing, the phosphorus-containing sewage after aeration and uniform mixing enters a secondary coagulation reaction tank 21, a dosing system is started simultaneously, sulfuric acid and hydrogen peroxide are fed into the secondary coagulation reaction tank 21, the pH value of the sewage is adjusted to 3, and the mixture is stirred and uniformly mixed; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electrolytic dephosphorization of the electrode plates flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air flotation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the content of inorganic phosphorus (counted by P) in the effluent sewage is 3.5mg/L, and the effluent sewage reaches the three-level total phosphorus discharge standard in the Integrated wastewater discharge Standard GB 8978-1996.
Example 5:
the controlled process parameters are as follows: the space between the electrode plates is 1cm, the working voltage between the electrode plates is 1v, the electrolysis time is 10min, and the polar water ratio is 28m2：1m3The power supply is a high-frequency pulse direct-current power supply with the current density of 200A/m2The pulse frequency is 20000Hz, the duty ratio is 100%, the aeration rate of the second aeration opening 24 is 10L/(L.min), the aeration rate of the first aeration opening 23 is 40L/(L.min), the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 4, the concentration of the hydrogen peroxide in the added medicament is 30%, and the flow rate of the hydrogen peroxide is adjustedAccording to the volume ratio of sewage to hydrogen peroxide of 1000: adding hydrogen peroxide in the proportion of 40.
4061mg/L medical phosphorus-containing sewage (calculated by P) containing organic phosphorus enters a primary coagulation reaction tank 20 through a water inlet 9 for aeration and uniform mixing, the phosphorus-containing sewage after aeration and uniform mixing enters a secondary coagulation reaction tank 21, a dosing system is started simultaneously, sulfuric acid and hydrogen peroxide are fed into the secondary coagulation reaction tank 21, the pH value of the sewage is adjusted to 4, and the mixture is stirred and uniformly mixed; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electrolytic dephosphorization of the electrode plates flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air flotation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the content of inorganic phosphorus (counted by P) in the effluent sewage is 1.5mg/L, and the effluent sewage reaches the three-level total phosphorus discharge standard in the Integrated wastewater discharge Standard GB 8978-1996.
Example 6:
the controlled process parameters are as follows: the space between the electrode plates is 4cm, the working voltage between the electrode plates is 5v, the electrolysis time is 20min, and the polar water ratio is 28m2：1m3The power supply is a high-frequency pulse direct-current power supply with the current density of 100A/m2The pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the second aeration opening 24 is 15L/(L.min), the aeration rate of the first aeration opening 23 is 30L/(L.min), the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 5, the concentration of the hydrogen peroxide in the added medicament is 30%, the flow rate of the hydrogen peroxide is adjusted, and the volume ratio of the sewage to the hydrogen peroxide is 1000: hydrogen peroxide is added in the proportion of 20.
4061mg/L medical phosphorus-containing sewage (calculated by P) containing organic phosphorus enters a primary coagulation reaction tank 20 through a water inlet 9 for aeration and uniform mixing, the phosphorus-containing sewage after aeration and uniform mixing enters a secondary coagulation reaction tank 21, a dosing system is started simultaneously, sulfuric acid and hydrogen peroxide are fed into the secondary coagulation reaction tank 21, the pH value of the sewage is adjusted to be 5, and the mixture is stirred and uniformly mixed; the phosphorus-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electrolytic dephosphorization of the electrode plates flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air flotation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the content of inorganic phosphorus (counted by P) in the effluent sewage is 6.5mg/L, and the effluent sewage reaches the three-level total phosphorus discharge standard in the Integrated wastewater discharge Standard GB 8978-1996.
Example 7:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 1.5v, the electrolysis time of the sewage is 20min, and the electrode-water ratio is 28m2：1m3Current density of 100A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the aeration port II 24 is 10L/(L.min), the aeration rate of the aeration port I23 is 30L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Sewage containing 76.5mg/L chromium enters a primary coagulation reaction tank 20 through a water inlet 9 for aeration and uniform mixing, the sewage containing chromium after aeration and uniform mixing enters a secondary coagulation reaction tank 21, and meanwhile, a dosing system is started, the pH value of the sewage is adjusted to 8, and the sewage is stirred and uniformly mixed; the evenly mixed chromium-containing sewage flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the phosphorus-containing sewage after water distribution and aeration flows through the electrode plate from bottom to top; the sewage after the electric flocculation flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air floatation device through a water outlet 4 for solid-liquid separation, and after stable operation, sampling detection is carried out, the total chromium content in the effluent sewage is 0.01mg/L, and the effluent sewage reaches the first-level discharge standard in Integrated wastewater discharge Standard GB 8978-1996.
Example 8:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 3v, the electrolysis time of the sewage is 20min, and the polar water ratio is 28m2：1m3Current density of 100A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the aeration port II 24 is 10L/(L.min), the aeration rate of the aeration port I23 is 30L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Sewage containing 84.7mg/L of copper coke enters a primary coagulation reaction tank 20 through a water inlet 9 for aeration and uniform mixing, the copper-containing sewage after aeration and uniform mixing enters a secondary coagulation reaction tank 21, and meanwhile, a dosing system is started to adjust the pH value of the sewage to 8, and the sewage is stirred and uniformly mixed; the copper-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the copper-containing sewage subjected to water distribution and aeration flows through the electrode plates from bottom to top; the sewage after the electrochemical reaction flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air floatation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the total copper content in the effluent sewage is 0.084mg/L, and reaches the first-level discharge standard in Integrated wastewater discharge Standard GB 8978-1996.
Example 9:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 2.8v, the electrolysis time of the sewage is 20min, and the electrode-water ratio is 28m2：1m3Current density of 100A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the aeration port II 24 is 10L/(L.min), the aeration rate of the aeration port I23 is 30L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Introducing 160mg/L nickel-containing sewage into a primary coagulation reaction tank 20 through a water inlet 9 for uniformly aerating, introducing the uniformly aerated nickel-containing sewage into a secondary coagulation reaction tank 21, starting a dosing system, adjusting the pH value of the sewage to 8, and uniformly stirring; the nickel-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the nickel-containing sewage subjected to water distribution and aeration flows through the electrode plates from bottom to top; the sewage after the electrochemical reaction flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air floatation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the total nickel content in the effluent sewage is 0.168mg/L, and reaches the first-level discharge standard in Integrated wastewater discharge Standard GB 8978-1996.
Example 10:
the controlled process parameters are as follows: the space between the electrode plates is 2cm, the working voltage between the electrode plates is 2v, the electrolysis time of the sewage is 20min, and the polar water ratio is 28m2：1m3Current density of 100A/m2The power supply is a high-frequency pulse direct-current power supply, the pulse frequency is 10000Hz, the duty ratio is 50%, the aeration rate of the aeration port II 24 is 10L/(L.min), the aeration rate of the aeration port I23 is 30L/(L.min), and the pH value of the sewage in the secondary coagulation reaction tank is adjusted to be 8.
Introducing 130mg/L zinc-containing sewage into a primary coagulation reaction tank 20 through a water inlet 9, uniformly aerating, introducing the uniformly aerated zinc-containing sewage into a secondary coagulation reaction tank 21, starting a dosing system, adjusting the pH value of the sewage to 8, and uniformly stirring; the zinc-containing sewage after being stirred and uniformly mixed flows into the perforated pipe 17 through the communicating pipe 7 and reaches the water distribution area 16 for water distribution and aeration; the zinc-containing sewage after water distribution and aeration flows through the electrode plates from bottom to top; the sewage after the electrochemical reaction flows into an overflow groove 14 through an overflow weir 13, then flows into a coagulating sedimentation device or an air floatation device through a water outlet 4 for solid-liquid separation, and is sampled and detected after stable operation, the total zinc content in the effluent sewage is 0.125mg/L, and reaches the first-level discharge standard in Integrated wastewater discharge Standard GB 8978-1996.
The embodiments of the present invention have been described in detail with reference to the drawings, but the present invention is not limited to the above embodiments, and those skilled in the art can make modifications and improvements without departing from the scope of the present invention.
Claims (8)
1. An electrochemical phosphorus removal device comprises a water inlet (9) and a water outlet (4), and is characterized in that: a reaction area and an electrolysis area are sequentially arranged between the water inlet (9) and the water outlet (4);
the reaction zone comprises a primary coagulation reaction tank (20), a secondary coagulation reaction tank (21) and a baffle plate (19), the primary coagulation reaction tank (20) and the secondary coagulation reaction tank (21) are separated by the baffle plate (19), the upper edge of the baffle plate (19) is lower than the upper edge of the tank body of the reaction zone, and a water inlet (9) is communicated with the primary coagulation reaction tank (20);
the electrolytic zone is provided with an accommodating groove (15), electrode plates which are the same in distance and parallel to each other are arranged in the accommodating groove (15), and the electrode plates comprise an electric connection electrode plate (11) and an induction electrode plate (10); the material of the electric connecting electrode plate is selected from one or two of iron plate, aluminum plate and graphite, and the material of the induction electrode plate (10) is iron plate or aluminum plate; a water distribution area (16) is arranged below the electrode plate, and the secondary coagulation reaction tank (21) is communicated with the water distribution area (16); the upper part of the accommodating groove (15) is provided with an overflow groove (14), the overflow groove (14) is provided with an overflow weir (13), sewage flows into the overflow groove (14) through the overflow weir (13), and the overflow groove (14) is communicated with the water outlet (4).
2. The electrochemical phosphorus removal device of claim 1, wherein the inner wall of the accommodating groove (15) is provided with a polar plate clamping groove (26), and the polar plates are sequentially inserted into the polar plate clamping groove (26); two electric connecting electrode plates (11) at the outermost side of the electrode plates are respectively connected with the positive and negative electrodes of a power supply, and the induction electrode plates (10) are not connected with the electrodes.
3. An electrochemical phosphorus removal device as claimed in claim 2, wherein the overflow weir (13) is toothed.
4. The electrochemical phosphorus removal device according to claim 3, wherein the water distribution area (16) is provided with perforated pipes (17), water outlet holes are uniformly distributed on the perforated pipes (17), aeration pipes (18) are arranged below the perforated pipes (17), and air outlet holes are uniformly distributed on the aeration pipes (18); a sludge collecting groove is arranged below the water distribution area (16), and a sludge discharge pipe (5) is arranged at the bottom of the sludge collecting groove; the perforated pipe (17) is connected with the secondary coagulation reaction tank (21) through a communicating pipe (7).
5. The electrochemical phosphorus removal device according to any one of claims 1 to 4, wherein the primary coagulation reaction tank (20) is provided with a second aeration opening (24) and/or a mechanical stirring device, and the second aeration opening (24) is arranged below the water inlet (9); the secondary coagulation reaction tank (21) is provided with a mechanical stirring device and/or an aeration port.
6. The electrochemical phosphorus removal device of claim 5, wherein:
the primary coagulation reaction tank (20) is provided with a dosing system, a medicament is selected from acid liquor and alkali liquor, the acid liquor is selected from one of sulfuric acid, hydrochloric acid, ferric sulfate, nitric acid and phosphoric acid, and the alkali liquor is selected from one of potassium hydroxide, calcium hydroxide and sodium hydroxide;
the secondary coagulation reaction tank (21) is provided with a dosing system, a medicament is selected from an oxidant, and the oxidant is selected from one of hydrogen peroxide, persulfate and sodium hypochlorite.
7. The electrochemical phosphorus removal device of claim 6, wherein a first evacuation pipe (25) is arranged at the bottom of the primary coagulation reaction tank (20), and a second evacuation pipe (8) is arranged at the bottom of the secondary coagulation reaction tank (21).
8. The electrochemical phosphorus removal device of any one of claims 1 to 4, wherein the electrode plate spacing is 1cm to 4cm, and the electrode plate current density is 5mA/cm2～50mA/cm2The voltage between the polar plates is 0.1 v-5 v, the power supply is a high-frequency pulse direct current power supply, the pulse frequency is 5000-20000 Hz, the duty ratio is 10-100%, the aeration quantity of the aeration opening I (23) is 20-40L/(L.min), and the aeration quantity of the aeration opening II (24) is 5-15L/(L.min).
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