CN115259326A - Grid flocculation tank for reinforcing removal of pollutants by inducing formation of coral reef-shaped flocs - Google Patents
Grid flocculation tank for reinforcing removal of pollutants by inducing formation of coral reef-shaped flocs Download PDFInfo
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- CN115259326A CN115259326A CN202211079202.0A CN202211079202A CN115259326A CN 115259326 A CN115259326 A CN 115259326A CN 202211079202 A CN202211079202 A CN 202211079202A CN 115259326 A CN115259326 A CN 115259326A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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Abstract
一种诱导形成珊瑚礁状絮体强化污染物去除的网格絮凝池，沿水流方向，池中依次分为投药区、絮凝区、过渡区和沉淀区；投药区和絮凝区均划分为呈网格状分布的若干分区；在投药区和絮凝区中，沿水流方向，各分区为串联关系，且本级分区与其上游紧邻分区之间在顶部或底部连通，本级分区与其下游紧邻分区之间在底部或顶部连通；在投药区选择某几个分区分别作为酸投加点、碱投加点和混凝剂投加点；其中酸投加点位于所有碱投加点和混凝剂投加点的上游；在投药区选择某几个分区设置pH计，酸和碱的投加使得上游分区的pH计示数常为6，下游分区的pH计示数常为7。本发明具有效率高，成本低，易应用的优点。
A grid flocculation tank for inducing the formation of coral reef-like flocs to enhance the removal of pollutants. Along the direction of water flow, the tank is divided into a dosing area, a flocculation area, a transition area and a sedimentation area in turn; the dosing area and the flocculation area are divided into grids. In the dosing area and the flocculation area, along the water flow direction, the partitions are connected in series, and the current-level partition and its immediate upstream partition are connected at the top or bottom, and the current-level partition and its immediate downstream partition are connected at the top or bottom. Connected at the bottom or top; select certain partitions in the dosing area as acid dosing points, alkali dosing points and coagulant dosing points; acid dosing points are located upstream of all alkali dosing points and coagulant dosing points; in the dosing area Select a few partitions to set up pH meters. The addition of acid and alkali will make the pH meter of the upstream partition always show 6 and the pH meter of the downstream partition to always be 7. The invention has the advantages of high efficiency, low cost and easy application.
Description
Technical Field
The invention belongs to the technical field of water purification, and particularly relates to a grid flocculation tank for inducing formation of coral reef-shaped flocs to enhance removal of pollutants.
Background
Currently, the sewage discharge standard is increasingly strict, most sewage plants execute the primary standard of integrated sewage discharge standard (GB 8978-1996) or the primary standard B of pollutant discharge standard (GB 18918-2002) of urban sewage treatment plants, and in recent years, the standard is improved to the primary standard A and is even similar to the III and IV standards of surface water environment quality standard (GB 3838-2002), such as the integrated water pollutant discharge standard (DB 11/307-2013) of Beijing local standard, and the integrated yellow river drainage standard of Shaanxi province (DB 61 224-2018) of local standard of Shaanxi province. The total phosphorus and COD emission standards are further reduced to 0.3mg/L and 30mg/L. Therefore, sewage plants must be upgraded to meet the emission requirements.
As a traditional water treatment process, the coagulation process is widely applied to advanced sewage treatment and has a certain effect of removing suspended matters, organic matters, phosphorus pollutants and the like. However, in the face of more stringent discharge standards, the coagulant dosage must be increased, which not only increases the direct cost of the chemicals, but also increases the cost of subsequent sludge disposal. The traditional flocculation tank is used as a structure for floc growth after coagulant addition, and the medicament is added in the mixing tank once and is stirred and mixed by a mechanical device. Under such conditions, the metal salt coagulant is rapidly hydrolyzed under neutral or alkaline conditions to generate hydroxide, and the net trapping and sweeping and adsorbing capabilities of the hydroxide are not fully exerted.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a grid flocculation tank for inducing the formation of coral reef-shaped flocs to strengthen the removal of pollutants, which creates favorable hydrolysis conditions through pre-acidification, optimizes the adding mode of a metal salt coagulant and alkali, realizes the induced formation of the coral reef-shaped flocs, provides more binding point positions for the pollutants so as to improve the coagulation removal effect, and has the advantages of high efficiency, low cost and easy application.
In order to achieve the purpose, the invention adopts the technical scheme that:
a mesh flocculation tank for inducing the formation of coral reef-shaped flocs to enhance pollutant removal is characterized in that the tank is sequentially divided into a dosing area, a flocculation area, a transition area and a precipitation area along the water flow direction; the drug feeding area and the flocculation area are divided into a plurality of subareas which are in grid distribution;
in the dosing zone and the flocculation zone, the zones are in series connection along the water flow direction, the zone of the stage is communicated with the adjacent zone at the upstream of the zone at the top or the bottom, and the zone of the stage is communicated with the adjacent zone at the downstream of the zone at the bottom or the top;
selecting a plurality of subareas in the dosing area as an acid dosing point, an alkali dosing point and a coagulant dosing point respectively; wherein the acid addition point is positioned at the upstream of all alkali addition points and coagulant addition points;
and selecting a plurality of subareas in the drug feeding area to be provided with pH meters, wherein the pH meters are at least arranged in an upstream subarea of a first coagulant feeding point and a downstream subarea of a last coagulant feeding point, the acid and alkali are fed so that the pH meter reading number of the upstream subarea is always 6, and the pH meter reading number of the downstream subarea is always 7.
In one embodiment, the dosing zone has a zoned cross-sectional area that is less than a zoned cross-sectional area of the flocculation zone such that the flow rate and turbulence of the water flow in the zoned of the dosing zone is substantially greater than the flow rate and turbulence in the zoned of the flocculation zone.
In one embodiment, the vertical flow velocity of water in each partition of the dosing zone is 0.25-0.4m/s; in each subarea of the flocculation area, the vertical flow velocity of water flow is 0.1-0.15m/s, and each subarea of the flocculation area is provided with grids or grid bars.
In one embodiment, the acid dosing point is located in the most upstream zone of the dosing zone.
In one embodiment, the alkali adding points and the coagulant adding points are multiple and are arranged at intervals along the water flow direction, the coagulant adding rate of each coagulant adding point is constant, the pH meters are multiple and are arranged along the water flow direction, the alkali adding rate of the upstream alkali adding point is controlled according to the indication number of the pH meter, so that the indication number of each pH meter along the water flow direction is gradually increased, and the indication number of the downstream pH meter is 7.
In one embodiment, one alkali addition point is provided upstream of each coagulant addition point.
In one embodiment, the most upstream pH meter has a reading of 6, the most downstream pH meter has a reading of 7, and the remaining pH meters have readings between 6 and 7.
In one embodiment, the single-pond processing capacity of the grid flocculation pond is 1-3.5 ten thousand meters 3 D, the water depth is 2-4m, the water passing holes among the subareas are staggered up and down, and all the water passing holes are in a submerged state.
In one embodiment, the effective volume of the flocculation zone is:
V 2 ＝m 2 ×t 2
the total area of the plane is:
the area of a single partition is:
the number of partitions is:
m 2 flow rate of flocculation zone, t 2 Is the hydraulic retention time of the flocculation zone; h is a total of 2 Is the average water depth of the flocculation zone; r is 2 Is the shaft flow velocity of the flocculation zone;
the total area of the plane of the drug delivery area is as follows:
the area of each partition is:
the number of partitions is:
V 1 is the effective volume of the administration area, V 1 ＝V 2 ，h 1 The average water depth of the drug delivery area; m is a unit of 1 Flow rate of drug administration area, m 1 ＝m 2 ，r 1 Is the shaft flow rate of the dosing area.
Compared with the prior art, the invention has the beneficial effects that:
1. the invention has higher treatment efficiency under the condition of the same coagulant adding amount; the coagulant required by the invention is only half of that of the traditional coagulation process to achieve the same treatment target.
2. The coral reef-like flocs induced by the method provide more binding sites for pollutants, and the capturing capability of the coagulant is fully exerted.
3. The adopted acid, alkali and coagulant have sufficient sources and low price, and the cost of the whole treatment process can be effectively controlled.
Drawings
Fig. 1 is a schematic plan view of a grid flocculation basin of the present invention.
Detailed Description
The embodiments of the present invention will be described in detail below with reference to the drawings and examples.
The invention relates to a grid flocculation tank for inducing and forming coral reef-shaped flocs to enhance removal of pollutants, which utilizes the hydrolytic polymerization characteristic of metal salt ions to build proper conditions, so that the coral reef-shaped flocs are induced and formed in a small and large process to enhance removal of pollutants, thereby realizing quality improvement and efficiency enhancement of water treatment.
The contaminants referred to in the present invention may preferably be small molecule organic substances.
As shown in figure 1, along the water flow direction, the grid flocculation tank is sequentially divided into a dosing area 1, a flocculation area 2, a transition area 3 and a sedimentation area 4. For convenience of description, the medicine feeding area 1 is divided into a first division area, and the flocculation area 2 is divided into a second division area.
In the direction of water flow, in the dosing zone 1, the first sections are connected in series, the first section of the current stage is communicated with the first section of the immediately adjacent section upstream at the top or bottom, and the first section of the current stage is communicated with the first section of the immediately adjacent section downstream at the bottom or top, namely, the water flow flows in an up-and-down staggered mode among the first sections.
Similarly, in the flocculation zone 2, the second partitions are connected in series along the water flow direction, the second partition is communicated with the second partition immediately upstream thereof at the top or bottom, and the second partition is communicated with the second partition immediately downstream thereof at the bottom or top, that is, the water flows between the second partitions in an up-and-down staggered manner.
Selecting a plurality of subareas I as an acid feeding point, an alkali feeding point and a coagulant feeding point respectively; wherein the acid addition point is located upstream of all the alkali addition points and the coagulant addition point. The acidifying agent used in the present invention may be sulfuric acid (H) 2 SO 4 ) Or hydrochloric acid (HCl), the coagulant can be crystalline aluminum chloride (AlCl) 3 ·6H 2 O) or crystalline aluminium sulphate (Al) 2 SO 4 ·18H 2 O), the base can be sodium hydroxide (NaOH) or calcium hydroxide (Ca (OH) 2 )。
And selecting a certain number of subareas and arranging a pH meter, wherein the pH meter is at least arranged in an upstream subarea of a first coagulant feeding point and a downstream subarea of a last coagulant feeding point. In the present invention, the acid and base are added so that the pH reading in the upstream zone is usually 6 and the pH reading in the downstream zone is usually 7. Illustratively, the acid addition point is located in the most upstream zone of dosing zone 1.
According to the above structure, the present invention performs the administration phase in the administration zone 1 and the flocculation phase in the flocculation zone 2.
In the dosing stage, the raw water to be treated is acidified to a pH value of 6 by adding acid through an acid adding point. Then respectively adding alkali and coagulant through an alkali adding point and a coagulant adding point. In order to fully mix the coagulant with the water body, the flow velocity of the water body is high at this stage, and the mixing is violent. Illustratively, the vertical flow velocity of the water flow of each zone I is controlled to be 0.25-0.4m/s through the pump piece, the size of the zone I and the like.
The alkali adding point and the coagulant adding point are both provided with a plurality of alkali adding points, 10-20 alkali adding points are arranged in the embodiment at intervals along the water flow direction, and preferably, one alkali adding point can be arranged at the upstream of each coagulant adding point. The coagulant adding at each coagulant adding point adopts a metering pump, the adding speed is constant and is generally 2-3 mg/(L.min), the adding amount is generally 15-30 mg/L (calculated by aluminum), therefore, the adding time is generally 5-10min, namely, the hydraulic retention time in the adding stage is 5-10min.
The alkali adding equipment is also a metering pump, a plurality of pH meters are arranged along the water flow direction, 5 pH meters are averagely arranged along the process in the embodiment, the alkali adding speed of the downstream alkali adding points is adjusted and controlled according to the readings of the pH meters, so that the readings of the downstream pH meters along the water flow direction are gradually increased, namely the pH value of the water body rises along the process, and the reading of the most downstream pH meter is 7, namely the pH value of the water body just rises to be neutral after the coagulant adding is finished at the last coagulant adding point. It is understood that the most upstream pH meter has a reading of 6, the most downstream pH meter has a reading of 7, and the remaining pH meters have a reading between 6 and 7.
In the process that the pH value and the coagulant concentration are increased along the process in the dosing stage, coral reef-shaped flocs grow gradually to form, a large number of binding sites are provided for small molecular organic matters, and the removal rate of the small molecular organic matters is enhanced.
In the flocculation stage, the growth and coagulation of flocs are performed. In the stage, the flow rate of the water body is far slower than that of the dosing stage, the disturbance is far smaller than that of the dosing stage, so that the growth and the agglomeration of flocs are facilitated, and the size of the flocs gradually grows up in the stage. Illustratively, the vertical flow rate of the water flow of each second subarea is controlled to be 0.1-0.15m/s through the pump piece, the size of the second subarea and the like, and the hydraulic retention time of the stage is 10-20min.
After buffer transition in a transition zone 3, the solid-liquid separation is realized by precipitation in a precipitation zone 4.
In one embodiment of the invention, the water flow velocity and disturbance control are realizedThe sectional area of the first partition is smaller than that of the second partition, namely, the density of the first partition is larger than that of the second partition, and the volume of the first partition is smaller than that of the second partition. Illustratively, the section of the subarea I is square or square-like, and a sludge hopper is not arranged. The section of the partition II is square, and a sludge hopper is arranged. And arranging grids or grids in the second subarea. When passing through the pores of the grid or the grid bars, the water flow shrinks and expands after passing through the meshes, so that a good flocculation condition is formed. Thus, the dosing stage maintains a rapid mixing (100 s) with the same width and flow rate of the dosing zone 1 and the flocculation zone 2 -1 ＜G＜300s -1 ) And the flocculation stage is changed from a rapid mixing state to a slow mixing state (30 < G < 60 s) -1 )。
In order to adapt to general industrial treatment, the single-tank treatment capacity of the grid flocculation tank is 1-3.5 ten thousand meters 3 And d, the water depth is 2-4m, the water passing holes among the subareas are arranged in a vertically staggered manner, and all the water passing holes are always submerged. The dosing area 1 and the flocculation area 2 are adjacently arranged and have the same width.
In one embodiment of the invention, the secondary effluent of a sewage plant is taken as a treatment object, and the treatment scale is designed as follows: 31500m 3 And d, the hydraulic retention time of the dosing stage and the flocculation stage is 10min.
Firstly, a flocculation stage is designed, and the flow rate is 31500m 3 /d＝0.365m 3 /s
Flocculation time is 10min, and effective volume is obtained
V＝0.365×10×60＝219.0m 3
The average water depth is 3.0m, and the total plane area of the flocculation zone 2 is
The flow rate of the vertical shaft is 0.12m/s, and the area of a single subarea is obtained as
Each grid is square, the side length is 1.73m, and the area of each partition is 3.0m 2 The number of the second partition is
In order to match the size of the sedimentation tank, 25 grids are adopted.
The actual flocculation time is
The average water depth in the pond is 3.0m, the height of the pond is 0.45m, the depth of the mud bucket is 0.5m, and the total height of the pond is obtained
H＝3.0+0.45+0.5＝3.95m
The size of the flocculation area 2 is 8.65 multiplied by 4.10, so the width of the drug feeding area 1 is 8.65m, the flow and the hydraulic retention time are the same as the flocculation area 2, and the effective volume is 219m 3 . The average water depth was 3.5m, and the total planar area was:
the flow rate of the vertical shaft is 0.285m/s, and the area of each single partition is obtained
Each grid is similar to a square, the size of each grid is 1.03m multiplied by 1.24m, and the area of each grid is 1.28m 2 The number of the partitions one is
For matching with flocculation stage, 49 grids are adopted
The actual hydraulic retention time is
The average water depth in the pond is 3.5m, the height of the pond is 0.45m, and the total height of the pond is obtained
H＝3.5+0.45＝3.95m
The operation of the above embodiment is as follows:
the method comprises the following steps: adding a certain amount of sulfuric acid into raw water to reduce the pH value of the water body to 6. The water body then enters the first part of the grid flocculation tank: and (4) an administration phase. The hydraulic retention time of the section is 10min. Illustratively, the point of addition of sulfuric acid is located in the most upstream zone one.
Step two: the prepared crystalline aluminum chloride solution is continuously added into the water body by a metering pump, the concentration is 4g/L (calculated by aluminum, the same applies below), and the adding dose is 24mg/L. And 12 coagulant adding points (shown in figure 1) are arranged along the process, and the coagulant adding rate of each point is 0.1825L/s. When the coagulant is continuously added, 6 pH meters are arranged along the process, the pH change of the water body is monitored in the whole process, a prepared sodium hydroxide solution is continuously added into the water body by using a metering pump, the concentration is 0.4mol/L, and the adding rate control principle is that the pH of each pH meter arrangement point is slowly increased from the original pH, and finally, when the coagulant is added, the pH of the water body is just neutral (pH = 7.0). The water body then enters the second part of the grid flocculation tank: the conventional flocculation stage. The hydraulic retention time of the section is 10min.
Step three: in the traditional flocculation stage, the water flow speed is low, flocs pass through grids and grow by continuous collision, and the size of the flocs is enlarged. And finally, the water body passes through the transition area, passes through the water distribution pattern wall and enters the precipitation area to finish the sedimentation and separation of the flocs.
In the embodiment of the invention, the incoming water is the secondary effluent of a sewage plant, the concentration of organic matters is DOC =5.71mg/L, and the addition of a coagulant is 24mg/L, for example, after the treatment of the flocculation tank, the concentration of the organic matters is detected and reduced to DOC =4.30mg/L, and the corresponding removal rate is about 24.69 percent, so that the flocculation tank can realize advanced treatment. And the conventional flocculation tank is utilized to treat the secondary effluent of the sewage plant, and the addition amount of the coagulant is 24mg/L, so that the concentration of the treated organic matters is DOC =5.03mg/L, and the corresponding removal rate is only 11.91 percent. If the removal rate is about 25%, the coagulant addition amount required by the conventional flocculation tank is at least 48mg/L.
Claims (9)
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Cited By (1)
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| CN119080170A (en) * | 2024-07-31 | 2024-12-06 | 西安西热水务环保有限公司 | A system and method for removing small molecular organic matter based on field energy granulation and agglomeration |
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