CN117843107B - A self-renewing high-density sedimentation tank with suspended layer and a water treatment method - Google Patents

A self-renewing high-density sedimentation tank with suspended layer and a water treatment method

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Publication number
CN117843107B
CN117843107B CN202410163060.9A CN202410163060A CN117843107B CN 117843107 B CN117843107 B CN 117843107B CN 202410163060 A CN202410163060 A CN 202410163060A CN 117843107 B CN117843107 B CN 117843107B
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CN
China
Prior art keywords
zone
flocculation
tank
area
mixing
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CN202410163060.9A
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Chinese (zh)
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CN117843107A (en
Inventor
姬晓羽
冯振鹏
朱少华
李志龙
罗可
姜家良
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Wisdri Engineering and Research Incorporation Ltd
Wisdri Urban Construction Engineering Technology Co Ltd
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Wisdri Engineering and Research Incorporation Ltd
Wisdri Urban Construction Engineering Technology Co Ltd
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Priority to CN202410163060.9A priority Critical patent/CN117843107B/en
Publication of CN117843107A publication Critical patent/CN117843107A/en
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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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/0012—Settling tanks making use of filters, e.g. by floating layers of particulate material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/0039—Settling tanks provided with contact surfaces, e.g. baffles, particles
    • B01D21/0045—Plurality of essentially parallel plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2444—Discharge mechanisms for the classified liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2488—Feed or discharge mechanisms for settling tanks bringing about a partial recirculation of the liquid, e.g. for introducing chemical aids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/30—Control equipment
    • B01D21/32—Density control of clear liquid or sediment, e.g. optical control ; Control of physical properties

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

The invention discloses a suspension layer self-updating high-density sedimentation tank which comprises a mixing area, a flocculation area and a sedimentation area, wherein the mixing area comprises a mixing tank and a mixing area stirrer positioned in the mixing tank, the mixing area stirrer comprises a lower turbine blade stirring mechanism and an upper straight blade stirring mechanism, the flocculation area comprises a flocculation tank, a central cylinder and a flocculation area stirrer, the central cylinder is arranged in the flocculation tank, the flocculation area stirrer is arranged in the central cylinder, the lower blade stirring mechanism and the upper blade stirring mechanism of the flocculation area stirrer are arranged in the central cylinder, the sedimentation area comprises a sedimentation tank, the sedimentation tank comprises a mud sedimentation area, a lower inclined plate area, a water distribution area, a suspension interception area, an upper inclined plate area and a water outlet area in sequence from bottom to top, and inclined plates of the lower inclined plate area and the upper inclined plate area are different in inclination direction. The invention also discloses a water treatment method. The invention can improve the removal of the flocs, improve the water outlet quality and reduce the operation and maintenance cost.

Description

Suspension layer self-updating high-density sedimentation tank and water treatment method
Technical Field
The invention belongs to the field of water treatment, and particularly relates to a suspension layer self-updating high-density sedimentation tank and a water treatment method.
Background
The high-density sedimentation tank is also called a sludge circulation sedimentation tank, integrates coagulation, flocculation, sedimentation and sludge concentration, has the advantages of compact tank structure and reduced occupied area of a water treatment system, and can be flexibly applied to primary and deep treatment of raw water of drinking water, industrial and domestic sewage and rainwater. The existing high-density sedimentation tank usually needs to carry out sludge reflux, has high operation and maintenance cost, and the flocculation removal of the existing high-density sedimentation tank is not ideal, so that the water outlet effect needs to be further improved.
Disclosure of Invention
The invention mainly aims to provide a suspension layer self-updating high-density sedimentation tank and a water treatment method, which can improve the removal of flocs, improve the quality of effluent and reduce the operation and maintenance cost.
The technical scheme adopted by the invention is as follows:
A suspension layer self-updating high-density sedimentation tank comprises a mixing zone, a flocculation zone and a sedimentation zone which are sequentially arranged, wherein incoming water and a coagulant are rapidly and fully stirred in the mixing zone, pollutants and medicines in the incoming water are fully mixed and then enter the flocculation zone to react, and formed flocs are intercepted and removed in the sedimentation zone, so that the effluent is ensured to reach the standard;
The mixing zone comprises a mixing pool and a mixing zone stirrer positioned in the mixing pool, and the mixing zone stirrer comprises a lower turbine blade stirring mechanism and an upper straight blade stirring mechanism which are sequentially arranged from bottom to top;
The flocculation zone comprises a flocculation tank, a central cylinder and a flocculation zone stirrer; the water inlet enters the central cylinder through the first water outlet pipe, substances and medicaments in the water react further under the action of the flocculation area stirrer to generate flocs, and the flocs flow downwards to a water outlet of the flocculation tank to flow out of the flocculation area through the central cylinder;
The sedimentation area is provided with an overflow weir, the sedimentation area comprises a sedimentation tank, the sedimentation tank comprises a mud sedimentation area, a lower inclined plate area, a water distribution area, a suspension interception area, an upper inclined plate area and a water outlet area from bottom to top, a water inlet of the sedimentation tank is positioned at the upper part of the sedimentation tank and is communicated with a water outlet of the flocculation tank through the water inlet area, the mud sedimentation area is communicated with the water inlet area through a circulating water pump, an on-line suspended matter concentration measuring instrument is arranged in the suspension interception area, inclined plates of the lower inclined plate area and the upper inclined plate area are different in inclination direction, the circulating water pump circulates mud sediment in the mud sedimentation area to the water inlet area in a starting period, the mud sediment enters the sedimentation area, a suspension layer in the suspension interception area is cultivated, and after the suspended matter concentration in the suspension interception area reaches 3-10g/L, the circulating water pump is stopped, and the mud enters a normal treatment period after the specified concentration is reached.
Preferably, the hydraulic retention time of the suspension layer self-updating high-density sedimentation tank is 40-60 min, wherein the hydraulic retention time of the mixing zone is not more than 2min, the hydraulic retention time of the flocculation zone is 15-20 min, and the hydraulic retention time of the sedimentation zone is 30-45 min, so that the water outlet quality is ensured.
Preferably, two partition boards are arranged in parallel in the mixing tank to divide the mixing tank into 3 areas, the upper ends of the partition boards are connected with the top of the mixing tank, and the lower ends of the partition boards are provided with gaps with the bottom of the mixing tank;
the water enters a mixing area between the 2 partition plates through a water inlet of the mixing tank, and under the stirring action of a stirrer in the mixing area, the medicament is fully diffused and uniformly mixed, and then flows upwards to a water outlet at the upper part of the mixing tank through a gap between the partition plates and the bottom of the mixing tank and flows out of the mixing tank.
Preferably, the distance between the two separation plates is d 1;
The upper straight blade stirring mechanism is 2/3~3/5 of the height of the mixing tank from the tank bottom of the mixing tank and comprises two straight blade, wherein the diameter of the straight blade is 0.6d 1~0.7d1;
The lower turbine blade stirring mechanism has a height of 1/3-2/5 of the mixing tank from the bottom of the mixing tank, and comprises a disc and a plurality of turbine blades embedded around the disc, wherein the total diameter of the lower turbine blade stirring mechanism is 0.8d 1, the diameter of the disc is 0.5d 1~0.6d1, and the length of the blades is 0.5d 1~0.6d1. Preferably, the turbine blade is 45 ° six-bladed. The mixing of the incoming water and the medicament is generally better achieved.
Preferably, the flocculation area adopts a lower inlet and lower outlet mode, water inlet adopts a pipeline for water inlet and water outlet adopts a submerged hole for water outlet, namely, a water inlet of the flocculation tank is arranged at the bottom of the central cylinder and is communicated with a water outlet of the mixing tank through a first water outlet pipe, a water outlet of the flocculation tank is arranged at the lower part of the flocculation tank and is arranged outside the central cylinder, and the structure can better generate flocs.
Preferably, the diameter d 2 of the central cylinder is 0.5-0.7 times that of flocculation Chi Bianchang;
The height of the lower-layer blade stirring mechanism from the bottom of the flocculation tank is 1/2-3/5 of the height of the flocculation tank, the height of the upper-layer blade stirring mechanism from the bottom of the flocculation tank is 3/4~4/5 of the height of the flocculation tank, the lower-layer blade stirring mechanism and the upper-layer blade stirring mechanism both adopt 45-degree four-oblique-blade blades, the total diameter is 0.9d 2, and the structure can better generate flocs.
Preferably, the height of the water outlet area is not less than 0.8m;
The height of the water distribution area is not less than 1.5m, and the suspension interception area is controlled to form a suspension layer through the change of the flow velocity;
The height of the suspension interception area is not smaller than 1.0m, the ratio of the water passing area of the lower layer to the water passing area of the upper layer of the suspension interception area is 1:1.2-1:1.5, and the structure can better precipitate flocs and improve the water outlet quality.
Preferably, the upper inclined plate area is formed by obliquely arranging a plurality of flat plates, wherein the inclination angle of each flat plate is 50-70 degrees, preferably 60 degrees, the distance between every two adjacent flat plates is 80-100 mm, and the height of the upper inclined plate area is 0.8-1.0 m;
the lower inclined plate area is formed by obliquely arranging a plurality of corrugated plates, the wavelength of each corrugated plate is 400-500 mm, the wave height is 80-100 mm, the inclination angle of each corrugated plate is 50-70 degrees, preferably 60 degrees, the distance between every two adjacent corrugated plates is 150-300 mm, and the height of the lower inclined plate area is 0.8-1.0 m;
The inclination directions of the flat plate and the corrugated plate are different, namely the installation directions of the upper inclined plate area and the lower inclined plate area are not the same, and the structure can better precipitate flocs and improve the water outlet quality.
The method comprises the steps of mixing incoming water and a medicament in a mixing area through mechanical stirring, entering a flocculation area, enabling the incoming water in the mixing area to pass through a central cylinder, stirring at a low speed by a flocculation area stirrer, enabling the incoming water to undergo further reaction, enabling the flocs to gradually increase, enabling the incoming water to pass through the central cylinder, enabling the incoming water to have smaller water flow disturbance outside the central cylinder, enabling the flocs to further increase, and enabling the incoming water to enter a sedimentation area, enabling a suspension interception area of the sedimentation area to form a dynamic suspension layer capable of being automatically updated through flow speed change, and enabling the flocs to be intercepted and removed after the incoming water in the flocculation area passes through the sedimentation area.
The invention also provides a water treatment method, which adopts the suspension layer self-updating high-density sedimentation tank and comprises the following steps:
the incoming water and the coagulant are stirred rapidly and fully in a mixing area, pollutants and medicaments in the incoming water are mixed fully and then enter a flocculation area for reaction to generate flocs, and the flocs enter a precipitation area;
The suspension layer of the suspension interception area in the precipitation area is required to be cultivated in the starting period; the method comprises the steps of circulating the precipitated sludge in a sludge settling zone to a water outlet of a flocculation zone by a circulating water pump in a starting period, stopping the circulating water pump when the concentration of suspended matters in a suspension interception zone reaches 3-10g/L, and entering a treatment period;
The flocs enter the sedimentation area and then flow upwards to the lower sloping plate area, part of suspended matters with larger particle size are precipitated in the lower sloping plate area, and the suspended matters are precipitated and compressed at the trough position of the corrugated plate to form a floc structure with larger particle size and compacter particle size, and then slide downwards to the sedimentation area at the bottom of the sedimentation tank after being accumulated and compressed to a certain extent;
because of the existence of the suspension layer in the suspension interception area, part of suspended matters are intercepted and adsorbed to generate contact flocculation, the particle size and the density are increased, and then the suspended matters are opposite to the water flow direction and slide downwards to the lower inclined plate area to be removed;
The sedimentation tank has the advantages that the sedimentation tank can be used for effectively playing the role of intercepting suspended matters due to the existence of the suspending layers of the lower inclined plate area and the suspending interception area, the effect of contact flocculation is effectively exerted, the existence of carrier flocculation and the dynamic updating of the sludge suspending layer are realized under the condition that no external sludge flows back, the sludge is finally precipitated in the sludge settling area of the sedimentation area, and the treated water flows out from the water outlet area at the top of the sedimentation tank.
The invention has the beneficial effects that:
the mixing area stirrer is composed of a lower turbine blade stirring mechanism and an upper straight blade stirring mechanism after being modified, so that the medicaments can be quickly and uniformly mixed, and the problem that water flow integrally rotates along with the stirrer and the medicaments cannot be quickly and uniformly mixed when the stirring speed of a mixing area of a common high-density sedimentation tank is high is solved. According to experiments and simulation, the mixing efficiency of the invention is improved by 10% -20% compared with that of a common sedimentation tank, and the mixing time can be reduced by 10% -20%.
The flocculation area stirrer of the flocculation area is combined with the central cylinder, so that an environment with larger internal G value and smaller external G value can be created, water flow enters from the water inlet and then rises to the vicinity of the stirring blades of the flocculation area stirrer of the central cylinder against the action of gravity, flocculation reaction and flocculation growth occur under the dual action of the gravity and the stirring blades, and the flocculation enters the outside of the central cylinder along with the water flow after the central cylinder grows to a certain particle size, so that the G value is smaller, the flocculation can be effectively prevented from being broken, and a good environment is provided for the growth and the further increase of the particle size of the flocculation, so that the generated flocculation is more compact than that of a common high-density sedimentation tank, and a precondition is provided for the generation and sedimentation of a subsequent suspension layer.
The lower inclined plate area, the upper inclined plate area and the suspension interception area (variable speed area) are arranged in the sedimentation tank to form a stable suspension layer, so that the removal rate of the flocs is further improved. After the flocs generated in the flocculation area enter the sedimentation area, the flocs pass through the lower inclined plate area, part of the flocs with larger particle size are intercepted to be directly sedimented, and meanwhile, the wave crests and the wave troughs of the corrugated plates in the lower inclined plate area promote the further growth and the aggregation of the flocs, are beneficial to the sedimentation, and reduce the disadvantage that the sedimentation in the lower inclined plate area is not easy to clean. The floccules with proper particle size enter the variable speed area through the lower inclined plate area, the speed is slowed down, meanwhile, because the upper inclined plate area has a certain blocking effect on the floccules, part of the floccules can suspend in the area under the action of rising water flow to form a suspension layer, the suspension layer is used as a crystal nucleus of the subsequent floccules, larger floccules are formed after collision, the effect of rising water flow can be resisted when the particle size of the floccules is increased to a certain degree, the floccules are precipitated in the lower inclined plate area, and finally the floccules are sunk to the bottom of the precipitation area to be removed. The existence of the suspension layer can effectively intercept the flocs which are difficult to precipitate and have smaller particle diameters in the water flow, so that the flocs are removed after the flocs continue to grow to a certain extent, the sludge reflux is not needed, and the stability of the suspension layer is promoted only by virtue of the improvement of hydraulic conditions. Under the action of the water flow, the suspended layer can be self-updated, namely, the floccules with larger particle size and fewer effective flocculation points are collided and combined and then deposited and removed, and the floccules with smaller particle size and more effective flocculation points are partially and directly remained in the variable speed area under the action of the water flow, and partially ascended to the upper inclined plate area along with the water flow, and the deposited and deposited floccules downwards slide to the variable speed area after being used as 'crystal nuclei' of the follow-up floccules, so that the process is repeated. According to experiments and simulation, the removal rate of the effluent suspended matters can be improved by 35-45% compared with that of a common high-density sedimentation tank.
The lower inclined plate area and the upper inclined plate area (double-layer inclined plate) are arranged to ensure the stability of the suspension layer and the improvement of the treatment effect. The lower inclined plate area adopts a wave-shaped inclined plate to prevent sludge accumulation and blockage in the lower inclined plate area and negatively affect the water outlet effect in the later period.
The invention rationalizes the flow state of each stage of the high-density sedimentation tank, improves the effective volume to the maximum extent, reduces the generation of a dead water area and a backflow area, fully exerts the treatment potential of the tank body, and improves the actual effective volume. After entering the high-density sedimentation tank, the incoming water is mixed and flocculated to provide a foundation for the subsequent sedimentation stage, and the design of the tank body can ensure the reaction process to be full and is helpful for the growth of the flocs, so that the flocs obtained by the reaction are more superior to the existing high-density sedimentation tank in terms of compactness and size.
Compared with the existing high-density sedimentation tank, the sedimentation zone is provided with the double-layer inclined plates, and the installation angles are different, so that the water flow can fully play a sedimentation role in the two-layer inclined plates. The suspended interception area is formed through the speed change of water flow, the advantage of contact flocculation is fully exerted, the suspended layer can be kept stable due to the double-layer inclined plate, the flocs precipitated on the upper-layer inclined plate can slide down to the suspended layer to be used as the supplement of the suspended layer, the flocs with overlarge grain size in the suspended layer can be precipitated on the lower-layer inclined plate, the dynamic update of the suspended layer can be realized, and external force is not used, so that the treatment effect is improved, and the cost of external circulation is saved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions of the prior art, the following description will briefly explain the drawings used in the embodiments or the description of the prior art, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a suspension layer self-updating high density sedimentation tank;
FIG. 2 is a schematic structural view of a mixing zone;
FIG. 3 is a schematic structural view of a flocculation zone;
FIG. 4 is a schematic diagram of the structure of the precipitation zone;
FIG. 5 is a graph comparing the treatment effect of a common high-density sedimentation tank with that of the invention at different moments.
In the figure, a 1-mixing area, a 2-flocculation area, a 3-sedimentation area, a 4-circulating water pump, a 5-first water outlet pipe, a water inlet of a 101-mixing area, a 102-partition plate, a 103-mixing area stirrer, a water outlet of a 104-mixing area, a 10301-upper straight blade stirring mechanism, a 10302-lower turbine blade stirring mechanism, a 105-mixing tank, a water inlet of a 201-flocculation area, a water outlet of a 202-flocculation area, a 203-central cylinder, a 204-flocculation area stirrer, a 20401-upper blade stirring mechanism, a 20402-lower blade stirring mechanism, a 205-flocculation tank, a 301-water inlet area, a 302-sludge sedimentation area, a 303-lower inclined plate area, a 304-water distribution area, a 305-suspension interception area, a 306-upper inclined plate area, a 307-water outlet area, a 308-online suspended matter concentration measuring instrument and a 309-sedimentation tank are shown.
Detailed Description
The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
Example 1
Referring to fig. 1-4, the suspension layer self-updating high-density sedimentation tank comprises a mixing zone 1, a flocculation zone 2 and a sedimentation zone 3 which are sequentially arranged, incoming water and coagulant are rapidly and fully stirred in the mixing zone 1, pollutants and medicines in the incoming water are fully mixed and then enter the flocculation zone 2 to react to form flocs, and the flocs are intercepted and removed in the sedimentation zone 3 to ensure that the effluent reaches the standard.
Mixing zone 1 comprises mixing tank 105, mixing zone stirrer 103. Two partition plates 102 are arranged in parallel in the mixing tank 105 to divide the mixing tank into 3 areas. The upper end of the partition plate 102 is connected with the top of the mixing tank 105, and the lower end of the partition plate has a gap with the bottom of the mixing tank 105. The mixing zone 1 adopts an upper inlet and upper outlet weir flow mode to prevent the water coming from the mixing zone 1 from generating integral rotational flow under the action of the mixing zone stirrer 103, namely, a water inlet 101 of the mixing tank is arranged at the upper part of the mixing tank 105 and is positioned between two partition plates 102, two water outlets 104 of the mixing tank are arranged at the upper part of the mixing tank 105 and are positioned outside the two partition plates 102. The mixing zone stirrer 103 is interposed between the two partition plates 102, and includes a lower turbine blade stirring mechanism 10302 and an upper straight blade stirring mechanism 10301 which are disposed in this order from bottom to top. The distance between the two separation plates 102 is d 1, and the height of the upper straight blade stirring mechanism 10301 from the bottom 2/3~3/5 of the mixing tank 105 is equal to the height of the mixing tank 105, and the distance between the two separation plates is equal to two straight blades, wherein the diameter of each straight blade is 0.6d 1~0.7d1. The lower turbine blade stirring mechanism 10302 is 1/3-2/5 of the height of the mixing tank 105 from the bottom of the mixing tank 105, and comprises a disc and a plurality of turbine blades embedded around the disc. The overall diameter of the lower turbine blade agitation mechanism 10302 is 0.8d 1, with a disk diameter of 0.5d 1~0.6d1 and a blade length of 0.5d 1~0.6d1. Preferably, the turbine blades of the lower turbine blade agitation mechanism 10302 are 45 ° six-bladed. The turbine blade of lower floor turbine blade rabbling mechanism 10302 has the axial to rivers to promote, and two straight leaf blades of upper straight leaf blade rabbling mechanism 10301 have radial effect to rivers, and when rivers take place vertical motion under turbine blade's effect, two straight leaf blades carry out radial diffusion to rivers again, make rivers and medicament can spread, fuse fast.
The incoming water enters a mixing area between 2 partition plates 102 through a water inlet 101 of the mixing tank, and under the stirring action of a stirrer 103 in the mixing area, the chemical is fully diffused and uniformly mixed, and then flows upwards to a water outlet at the upper part of the mixing tank 105 through a gap between the partition plates 102 and the bottom of the mixing tank 105 and flows out of the mixing tank 105.
Flocculation zone 2 includes flocculation basin 205, central cylinder 203, and flocculation zone agitator 204. The central cylinder 203 is placed in the flocculation basin 205 (in the latter stage of flocculation reaction, the overall turbulence of the water flow is not too high to avoid the breaking of the formed flocs, so the central cylinder 203 is arranged in the flocculation zone 2), and the flocculation zone stirrer 204 is placed in the central cylinder 203. The flocculation zone 2 adopts a lower inlet and lower outlet mode, water inlet adopts a pipeline for water inlet, and water outlet adopts a submerged hole for water outlet, namely, a water inlet 201 of the flocculation tank is arranged at the bottom of a central cylinder 203 and is communicated with a water outlet 104 of the mixing tank through a first water outlet pipe 5, and a water outlet 202 of the flocculation tank is positioned at the lower part of a flocculation tank 205 and is positioned outside the central cylinder 203. The inflow water enters the central cylinder 203 through the first water outlet pipe 5, substances and medicines in the inflow water further react under the action of the flocculation area stirrer 204 to generate flocs, the outer side of the central cylinder 203 has no action of the flocculation area stirrer 204, the turbulence of the water flow is reduced, the environment is provided for the further growth of the flocs, and the flocs flow out of the flocculation area 2 through the central cylinder 203 and then downwards turn to the water outlet 202 of the flocculation tank. Flocculation zone agitator 204 includes a lower blade agitation mechanism 20402 and an upper blade agitation mechanism 20401 that are sequentially provided from bottom to top. The diameter d 2 of the central cylinder 203 is 0.5-0.7 times the side length of the flocculation tank 205. The height of the lower-layer blade stirring mechanism 20402 from the bottom of the flocculation tank 205 is 1/2-3/5 of the height of the flocculation tank 205, and the height of the upper-layer blade stirring mechanism 20401 from the bottom of the flocculation tank 205 is 3/4~4/5 of the height of the flocculation tank 205. The lower blade stirring mechanism 20402 and the upper blade stirring mechanism 20401 both adopt 45-degree four-oblique-blade blades, and the total diameter is 0.9d 2.
The sedimentation zone 3 is filled with water in the form of submerged holes and the outlet water is provided with an overflow weir to avoid negative impact of the water inlet and outlet on the sedimentation process, which includes a sedimentation tank 309. The sedimentation tank 309 is sequentially provided with a sludge sedimentation zone 302, a lower inclined plate zone 303, a water distribution zone 304, a suspension interception zone 305, an upper inclined plate zone 306 and a water outlet zone 307 from bottom to top. The water inlet of the sedimentation tank is positioned at the upper part of the sedimentation tank 309 and is communicated with the water outlet 202 of the flocculation tank through the water inlet area 301. The sludge settling zone 302 is communicated with the water outlet 202 of the flocculation zone through the circulating water pump 4. An in-line suspended matter concentration measuring instrument 308 is provided in the suspension interception area 305. In order to reduce short flow, the swash plate sedimentation function is exerted to the maximum extent, and the swash plate inclination directions of the lower swash plate region 306 and the upper swash plate region 303 are different. In the starting period, the circulating water pump 4 circulates the sludge precipitated in the sludge sedimentation area 302 to the water inlet area 301, then enters the sedimentation area 3, cultures the suspension layer of the suspension interception area 305, stops the circulating water pump 4 when the concentration of the suspended matters in the suspension interception area 305 reaches 3-10g/L, and enters the normal treatment period after the concentration reaches the specified concentration.
In this embodiment, to avoid the negative effect of the water inlet and outlet on the sedimentation process, the height of the water outlet area 307 should not be less than 0.8m. In order to ensure the precipitation effect, the incoming water needs to be uniformly distributed after entering the precipitation zone 3, so the height of the water distribution zone 304 is not less than 1.5m. The suspension interception area 305 is controlled to form a suspension layer through the change of the flow velocity, the ratio of the water passing area of the lower layer to the water passing area of the upper layer of the suspension interception area 305 is 1:1.2-1:1.5, and the height of the suspension interception area 305 is not smaller than 1.0m.
In this embodiment, the upper inclined plate region 306 has a height of 0.8 to 1.0m and is formed by a plurality of flat plates arranged in an inclined manner. The inclination angle of the flat plates is 60 degrees, and the distance between the adjacent flat plates is 80-100 mm. The lower inclined plate region has a height of 0.8-1.0 m and is formed by obliquely arranging a plurality of corrugated plates. The angle of inclination of the corrugated plate is 60 °. The wave length of the corrugated plate is 400-500 mm, wave height is 80-100 mm; the distance between adjacent corrugated plates is 150-300 mm. The inclination direction of the flat plate is different from that of the corrugated plate, that is, the installation directions of the upper inclined plate region 306 and the lower inclined plate region 303 are different.
In the embodiment, the hydraulic retention time of the suspension layer self-updating high-density sedimentation tank is 40-60 min, wherein the hydraulic retention time of the mixing zone 1 is not more than 2min, the hydraulic retention time of the flocculation zone 2 is 15-20 min, and the hydraulic retention time of the sedimentation zone 3 is 30-45 min.
Specific examples:
The common kaolin is used as a water sample of the suspension, the water inlet concentration is 3g/L, the particle phase density is 1010kg/m3, and the average particle size is 100 mu m. By comparing the treatment effect of the common high-density sedimentation tank with the treatment method, the volume, the treatment capacity, the water inlet and outlet speed, the G value of the flocculation zone of the mixing zone, the rising flow rate of the sedimentation zone and other parameters of the common high-density sedimentation tank are consistent with the treatment method.
FIG. 5 is a graph comparing the treatment effect of a common high-density sedimentation tank with that of the invention at different moments. As can be seen from FIG. 5, the outlet suspension concentration of the present invention increases slowly with time compared to a conventional high-density sedimentation tank, and the removal rate decreases slowly with time. The common high-density sedimentation tank has excellent removal performance on suspended matters in the first 2 hours, but the concentration of the suspended matters at the outlet rises rapidly along with the time, because the suspended matters are not accumulated in the sedimentation area at the initial stage of a working period, the suspended matters are easier to sediment and remove in the reactor, but the suspended matters are precipitated in the reaction tank along with the time, the suspended matters can migrate to the outlet to cause the increase of the suspended matters at the outlet, and the interception capability of the high-density sedimentation tank before transformation is limited, so that the initial interception effect on the suspended matters is better, but the limit of the high-density sedimentation tank on the interception of the suspended matters is reached quickly. The high-density sedimentation tank provided by the invention has the advantages that the flow state of the flow field is more reasonable, the interception capability of suspended matters is enhanced, so that the concentration of the suspended matters at the outlet is slower than that of a common high-density sedimentation tank along with the time, and the removal rate of the suspended matters is naturally improved greatly in the same working period.
The incoming water and the medicament are rapidly mixed in the mixing zone 1 through the mixing zone stirrer 103 and then enter the flocculation zone 2, the incoming water in the mixing zone 1 passes through the central cylinder 203, the flocculation zone stirrer 204 is used for stirring at a low speed to perform a further reaction, the flocs are gradually increased, the disturbance of the incoming water on the outer side of the central cylinder 203 is small after passing through the central cylinder 203, the flocs are further increased and then enter the sedimentation zone 3, a dynamic suspension layer capable of being automatically updated is formed in the suspension interception zone 305 of the sedimentation zone 3 through the change of the flow velocity, and the flocs are intercepted and removed after the incoming water in the flocculation zone 2 passes through the sedimentation zone 3.
The rapid mixing of the mixing zone, as well as the flocculation zone, provides a good reaction and growth environment for the flocs, providing a basis for the subsequent formation and dynamic renewal of the suspension interception zone 305 (suspension layer). Because the speed change of the suspension interception area 305 and the arrangement of the double-layer inclined plate can realize the dynamic self-updating of the suspension layer, compared with the traditional high-density sedimentation tank, the sludge reflux is not needed, and the removal rate of the flocs can be further improved by the arrangement of the double-layer inclined plate and the suspension interception area, so that the cost is reduced and the water outlet effect is obviously improved.
Example 2
A water treatment method using the suspension layer self-renewal high density sedimentation tank of example 1, comprising the steps of:
The incoming water and the coagulant are stirred rapidly and fully in the mixing zone 1, and pollutants and medicaments in the incoming water are mixed fully and then enter the flocculation zone 2 to react to generate flocs which enter the sedimentation zone 3;
The method comprises the steps of culturing a suspension layer of a suspension interception area 305 in a settling area 3 in a starting period, namely circulating precipitated sludge of a settling area 302 of the settling area to a water outlet 202 (a water inlet area 301) of a flocculation area by a circulating water pump 4 in the starting period, culturing the suspension layer of the suspension interception area 305, stopping the circulating water pump 4 when the concentration of suspended matters in the suspension interception area 305 reaches 3-10g/L, and entering a treatment period, and turning on the circulating water pump 4 when the concentration of the suspension layer in the suspension interception area 305 in the treatment period does not reach the requirement, and turning off the circulating water pump 4 until the concentration reaches the requirement;
the flocs enter the sedimentation area 3 and then flow upwards to the lower inclined plate area 303, part of suspended matters with larger particle size are precipitated in the lower inclined plate area 303, and the suspended matters are precipitated and compressed at the trough positions of the corrugated plates to form a floc structure with larger particle size and compacter particle size because of the aggregation effect of the suspended matters at the trough positions of the corrugated plates;
because of the existence of the suspension layer in the suspension interception area 305, part of suspended matters are intercepted and adsorbed to generate contact flocculation, the particle size and the density are increased, and then the suspended matters are opposite to the water flow direction and slide down to the lower inclined plate area 303 to be removed, and the other part of suspended matters continuously flow upwards along with the water flow to the upper inclined plate area 306;
The sedimentation tank 309 has the advantages that the interception effect of the sedimentation tank 309 on suspended matters is enhanced due to the existence of the lower inclined plate area 303 and the suspension interception area 305, the contact flocculation effect is effectively exerted, the existence of carrier flocculation and the dynamic update of the sludge suspension layer are realized under the condition that no external sludge flows back, the sludge is finally settled in the sludge settling area 302 of the sedimentation area 3, the treated water flows out from the water outlet area 307 at the top of the sedimentation tank 309, the removal efficiency of the sedimentation tank on small particle flocs is greatly improved, the problem of sludge blockage is solved, and the water quality of the produced water is better.
What is not described in detail in this specification is prior art known to those skilled in the art.
It will be understood that modifications and variations will be apparent to those skilled in the art from the foregoing description, and it is intended that all such modifications and variations be included within the scope of the following claims.

Claims (7)

1.一种水处理方法，其特征在于：所述方法采用悬浮层自更新高密度沉淀池；所述悬浮层自更新高密度沉淀池包括依次设置的混合区、絮凝区和沉淀区；1. A water treatment method, characterized in that: the method employs a suspended layer self-renewing high-density sedimentation tank; the suspended layer self-renewing high-density sedimentation tank comprises a mixing zone, a flocculation zone, and a sedimentation zone arranged sequentially; 所述混合区包括混合池和位于混合池内的混合区搅拌器，所述混合区搅拌器包括从下往上依次设置的下层涡轮叶片搅拌机构和上层直叶叶片搅拌机构；The mixing zone includes a mixing tank and a mixing zone agitator located within the mixing tank. The mixing zone agitator includes a lower turbine blade agitation mechanism and an upper straight blade agitation mechanism arranged sequentially from bottom to top. 所述絮凝区包括絮凝池、中心筒、絮凝区搅拌器；所述中心筒置于絮凝池内，所述絮凝区搅拌器置于中心筒内；絮凝区搅拌器包括从下往上依次设置的下层叶片搅拌机构和上层叶片搅拌机构；The flocculation zone includes a flocculation tank, a central cylinder, and a flocculation zone agitator; the central cylinder is placed inside the flocculation tank, and the flocculation zone agitator is placed inside the central cylinder; the flocculation zone agitator includes a lower blade agitator and an upper blade agitator arranged sequentially from bottom to top. 所述沉淀区包括沉淀池；所述沉淀池从下往上依次为沉泥区、布水区、下层斜板区、悬浮拦截区、上层斜板区和出水区；沉淀池的进水口位于沉淀池的上部，且通过进水区与絮凝池的出水口连通；沉泥区通过循环水泵与进水区连通；在悬浮拦截区设置有在线悬浮物浓度测量仪器；下层斜板区和上层斜板区的斜板倾斜方向不同；The sedimentation zone includes a sedimentation tank; the sedimentation tank, from bottom to top, consists of a sludge settling zone, a water distribution zone, a lower inclined plate zone, a suspended solids interception zone, an upper inclined plate zone, and an effluent zone; the inlet of the sedimentation tank is located at the top of the sedimentation tank and is connected to the effluent outlet of the flocculation tank through the inlet zone; the sludge settling zone is connected to the inlet zone via a circulating water pump; an online suspended solids concentration measuring instrument is installed in the suspended solids interception zone; the inclined plates in the lower and upper inclined plate zones have different inclination directions; 所述上层斜板区采用多个平板倾斜安设而成；所述平板的倾斜角度为50-70°；相邻平板的间距为80~100mm；所述上层斜板区的高度为0.8~1.0m；所述下层斜板区采用多个波形板倾斜安设而成；波形板的波长为400~500mm，波高为80~100mm；所述波形板的倾斜角度为50-70°；相邻波形板的间距为150~300mm；所述下层斜板区的高度为0.8~1.0m；平板与波形板的倾斜方向不同；The upper inclined plate area is formed by multiple flat plates installed at an angle; the inclination angle of the flat plates is 50-70°; the spacing between adjacent flat plates is 80-100mm; the height of the upper inclined plate area is 0.8-1.0m. The lower inclined plate area is formed by multiple corrugated plates installed at an angle; the wavelength of the corrugated plates is 400-500mm, and the wave height is 80-100mm; the inclination angle of the corrugated plates is 50-70°; the spacing between adjacent corrugated plates is 150-300mm; the height of the lower inclined plate area is 0.8-1.0m; the flat plates and corrugated plates have different inclination directions. 所述出水区的高度不得小于0.8m；所述布水区的高度不得小于1.5m；通过流速变化控制悬浮拦截区形成悬浮层；悬浮拦截区的高度不得小于1.0m；所述悬浮拦截区的下层过水面积与上层过水面积之比为1:1.2~1:1.5；The height of the outlet zone shall not be less than 0.8m; the height of the distribution zone shall not be less than 1.5m; the suspended interception zone shall be controlled by flow velocity changes to form a suspended layer; the height of the suspended interception zone shall not be less than 1.0m; the ratio of the lower water flow area to the upper water flow area of the suspended interception zone shall be 1:1.2 to 1:1.5. 所述方法包括如下步骤：The method includes the following steps: 来水和混凝剂在混合区快速、充分搅拌；来水中的污染物和药剂充分混合后进入絮凝区进行反应，生成絮体；絮体进入沉淀区；The incoming water and coagulant are rapidly and thoroughly mixed in the mixing zone; after the pollutants and agents in the incoming water are fully mixed, they enter the flocculation zone to react and generate flocs; the flocs then enter the sedimentation zone. 启动期需要对沉淀区中的悬浮拦截区的悬浮层进行培养；具体为：在启动期，循环水泵将沉泥区的沉淀污泥循环至絮凝区的出水口；当悬浮拦截区的悬浮物浓度达到3-10g/L后，停止循环水泵，进入处理期；若处理期，悬浮拦截区的悬浮层浓度达不到要求，开启循环水泵，至浓度达到要求后关闭；During the start-up phase, the suspended layer in the suspended interception zone of the sedimentation zone needs to be cultivated. Specifically, during the start-up phase, the circulating water pump circulates the settled sludge from the sedimentation zone to the outlet of the flocculation zone. When the suspended solids concentration in the suspended interception zone reaches 3-10 g/L, the circulating water pump is stopped, and the treatment phase begins. If the suspended layer concentration in the suspended interception zone does not meet the requirements during the treatment phase, the circulating water pump is turned on until the required concentration is reached, and then turned off. 絮体进入沉淀区后向上流至下层斜板区，部分粒径较大的悬浮物在下层斜板区沉淀，由于波形板的波谷位置对悬浮物有聚集作用，悬浮物在波谷位置沉淀、压缩，形成粒径更大、更为密实的絮体结构；在积聚、压缩到一定程度后下滑至沉淀池底部的沉泥区，这种絮体由于粒径和密度有所提高，其抗向上水流的携卷作用更强，更易快速沉积在沉淀池底部且不易被卷起；粒径较小的悬浮物则通过下层斜板区向上抵达悬浮拦截区；After entering the sedimentation zone, the flocs flow upwards to the lower inclined plate zone. Some of the larger suspended solids settle in the lower inclined plate zone. Due to the aggregation effect of the troughs of the corrugated plates, the suspended solids settle and compress at the troughs, forming a larger and denser floc structure. After accumulating and compressing to a certain extent, they slide down to the sludge zone at the bottom of the sedimentation tank. Because of their increased particle size and density, these flocs have a stronger resistance to being carried up by the upward water flow, making them easier to settle quickly at the bottom of the sedimentation tank and less likely to be rolled up. The smaller suspended solids then move upwards through the lower inclined plate zone to reach the suspension interception zone. 由于悬浮拦截区悬浮层的存在，部分悬浮物被拦截吸附发生接触絮凝作用，粒径和密度增大，后与水流方向相悖，下滑至下层斜板区被去除；另一部分则继续随水流向上流至上层斜板区；Due to the presence of the suspended layer in the suspended interception zone, some suspended matter is intercepted and adsorbed, resulting in contact flocculation, which increases the particle size and density. Subsequently, it flows against the direction of water flow and slides down to the lower inclined plate zone to be removed; the other part continues to flow upward with the water flow to the upper inclined plate zone. 其中一部分在上层斜板区被沉淀下来，并下滑至悬浮拦截区，促进悬浮拦截区悬浮层的自主动态更新；由于下层斜板区和悬浮拦截区悬浮层的存在，沉淀池对悬浮物的拦截作用增强，接触絮凝作用得到有效发挥，实现在无外部污泥回流的情况下，载体絮凝的存在和污泥悬浮层的动态更新，使污泥最终沉淀在沉淀区的沉泥区；经处理后的水从沉淀池顶部的出水区流出。Some of the sludge settles in the upper inclined plate zone and slides down to the suspended interception zone, promoting the autonomous dynamic renewal of the suspended layer in the suspended interception zone. Due to the presence of the lower inclined plate zone and the suspended layer in the suspended interception zone, the sedimentation tank enhances its interception effect on suspended solids, and the contact flocculation effect is effectively utilized. This allows the sludge to eventually settle in the sedimentation zone without external sludge return, thanks to the presence of carrier flocculation and the dynamic renewal of the sludge suspended layer. The treated water flows out from the effluent zone at the top of the sedimentation tank. 2.根据权利要求1所述的水处理方法，其特征在于：所述悬浮层自更新高密度沉淀池的水力停留时间为40min~60min；其中，混合区水力停留时间不得超过2min，絮凝区水力停留时间为15min~20min，沉淀区水力停留时间为30min~45min。2. The water treatment method according to claim 1, characterized in that: the hydraulic retention time of the self-renewing high-density sedimentation tank of the suspended layer is 40 min to 60 min; wherein, the hydraulic retention time of the mixing zone shall not exceed 2 min, the hydraulic retention time of the flocculation zone is 15 min to 20 min, and the hydraulic retention time of the sedimentation zone is 30 min to 45 min. 3.根据权利要求1所述的水处理方法，其特征在于：所述混合池内平行设置有两个分隔板将混合池分割为3个区域，分隔板的上端与混合池顶部连接，下端与混合池底部有空隙；所述混合区搅拌器置于两个分隔板之间；混合池的进水口置于混合池上部，且位于两个分隔板之间；混合池的出水口有两个，置于混合池上部，且位于两个分隔板外；3. The water treatment method according to claim 1, characterized in that: two partition plates are arranged in parallel inside the mixing tank to divide the mixing tank into three areas, the upper end of the partition plate is connected to the top of the mixing tank, and the lower end has a gap with the bottom of the mixing tank; the agitator of the mixing zone is placed between the two partition plates; the water inlet of the mixing tank is located at the upper part of the mixing tank and between the two partition plates; the water outlet of the mixing tank has two outlets, located at the upper part of the mixing tank and outside the two partition plates; 来水通过混合池的进水口进入2个分隔板之间的混合区，在混合区搅拌器的搅拌作用下，药剂充分扩散、混合均匀后通过分隔板与混合池底部的空隙上翻流至混合池的出水口流出混合池。Water enters the mixing zone between two partition plates through the inlet of the mixing tank. Under the stirring action of the agitator in the mixing zone, the agent is fully diffused and mixed evenly. Then, it flows up through the gap between the partition plate and the bottom of the mixing tank and flows out of the mixing tank through the outlet. 4.根据权利要求3所述的水处理方法，其特征在于：所述两个分隔板之间的间距为d1；4. The water treatment method according to claim 3, wherein the distance between the two partition plates is d1 ; 所述上层直叶叶片搅拌机构距混合池池底2/3~3/5混合池高度，其包括两直叶叶片；所述直叶叶片的直径为0.6d1~0.7d1；The upper straight-blade stirring mechanism is located 2/3 to 3/5 of the mixing tank height from the bottom of the mixing tank, and includes two straight blades; the diameter of the straight blades is 0.6d1 to 0.7d1 . 所述下层涡轮叶片搅拌机构距混合池底1/3~~2/5混合池高度，其包括圆盘和嵌在圆盘四周的多个涡轮叶片；所述下层涡轮叶片搅拌机构的总直径为0.8d1，其中，圆盘直径为0.5d1~0.6d1，叶片长度为0.5d1~0.6d1。The lower turbine blade stirring mechanism is located at 1/3 to 2/5 of the mixing tank height from the bottom of the mixing tank. It includes a disc and multiple turbine blades embedded around the disc. The total diameter of the lower turbine blade stirring mechanism is 0.8d1 , of which the diameter of the disc is 0.5d1 to 0.6d1 , and the blade length is 0.5d1 to 0.6d1 . 5.根据权利要求1所述的水处理方法，其特征在于：所述絮凝池的进水口置于中心筒底部，通过第一出水管与混合池的出水口连通；所述絮凝池的出水口位于絮凝池的下部，且位于中心筒外。5. The water treatment method according to claim 1, characterized in that: the inlet of the flocculation tank is located at the bottom of the central cylinder and is connected to the outlet of the mixing tank through the first outlet pipe; the outlet of the flocculation tank is located at the lower part of the flocculation tank and outside the central cylinder. 6.根据权利要求1所述的水处理方法，其特征在于：中心筒直径d2为絮凝池边长的0.5~0.7倍。6. The water treatment method according to claim 1, characterized in that: the diameter d2 of the central cylinder is 0.5 to 0.7 times the side length of the flocculation tank. 7.根据权利要求6所述的水处理方法，其特征在于：7. The water treatment method according to claim 6, characterized in that: 下层叶片搅拌机构距絮凝池池底1/2~3/5絮凝池高度，上层叶片搅拌机构距絮凝池池底3/4~4/5絮凝池高度；下层叶片搅拌机构和上层叶片搅拌机构均采用45°四斜叶叶片，总直径为0.9d2。The lower blade agitator is positioned 1/2 to 3/5 of the height of the flocculation tank bottom, while the upper blade agitator is positioned 3/4 to 4/5 of the height of the flocculation tank bottom. Both the lower and upper blade agitators use 45° four-bladed blades with a total diameter of 0.9d² .
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