Electrochemical destabilizer and low-power high-efficiency precipitation device

Abstract

The application provides an electrochemical destabilizer and a low-power high-efficiency precipitation device, wherein the electrochemical destabilizer comprises a barrel and a plurality of metal separators; the metal separators are arranged in the barrel at intervals, used for separating the space between the liquid inlet and the liquid outlet of the barrel into a plurality of flow sections, and the metal separators are provided with communication holes; the communication holes are used for communicating adjacent flow sections; and the material of the metal separators at least comprises zinc, copper, nickel and chromium. The application is based on the following: a plurality of metal separators made of nickel-chromium-zinc-copper alloy are arranged in the barrel, and the metal separators are provided with communication holes to form flow channels, so that the fluid to be destabilized is completed after flowing through each metal separator, and no external energy is needed, which is more energy-saving; the working condition is not affected by pressure and temperature, and no maintenance is needed during use, which is easier to operate; and the service life is long.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of mine water purification equipment, and particularly relates to an electrochemical destabilizer and a low-power efficient precipitation device. BACKGROUND

[0002] In the process of coal mining, mine water is usually accompanied by gushing, which has the characteristics of large discharge and high suspended solids. According to the relevant requirements of the environmental protection policy, coal production enterprises should preferentially use it for coal washing, underground production, fire fighting and dust spraying, etc., and the water quality of the discharged water must reach the Class III water quality standard in the surface water environmental quality standard.

[0003] The main pollutant of mine water is suspended solids (SS), which is mainly composed of fine particles such as coal dust, rock dust and clay. If it is to be reused or discharged, the suspended solids need to be treated. In the treatment, the mine water needs to be destabilized first, and then flocculation, sedimentation and other operations are performed. The current destabilizer mostly adopts a chemical destabilization method, that is, a coagulant such as aluminum sulfate or polyaluminum chloride is added to realize destabilization in water and form small flocs by cooperating with mechanical stirring. However, this destabilization method has the following problems: on the one hand, a coagulant needs to be added and mechanical stirring is needed, which has high energy consumption and operation cost; on the other hand, stable operating conditions such as water temperature and pH value need to be maintained during the destabilization operation, which has high operation requirement and is difficult to implement. The above problems need to be solved urgently. SUMMARY

[0004] In order to solve the problems in the background art, the present application provides an electrochemical destabilizer and a low-power efficient precipitation device.

[0005] In a first aspect, the present application provides an electrochemical destabilizer, which comprises a cylinder and a plurality of metal separators; the metal separators are arranged in the cylinder at intervals, used to divide the space between the liquid inlet and the liquid outlet of the cylinder into a plurality of flow sections, and the metal separators are provided with communication holes; the communication holes are used to communicate adjacent flow sections; the metal separators are made of zinc, copper, nickel and chromium.

[0006] Further, the mass percentage of nickel in the metal separator is 10-14%, the mass percentage of chromium is 16-22%, the mass percentage of zinc is 4-20%, and the balance is copper.

[0007] Further, the metal separator further comprises aluminum and / or magnesium, and the mass percentage of each component is: aluminum: 1%-2%, and magnesium: 2%-2.8%.

[0008] Further, the metal separator comprises a plurality of communication holes; the sum of the areas of the plurality of communication holes is greater than or equal to 92% of the area of the metal separator.

[0009] Further, the communication hole diameter comprises 5mm, and / or 12mm, and / or 27mm.

[0010] Further, the distance between adjacent metal separators is greater than or equal to 6 times the thickness of the metal separator.

[0011] Further, the cylinder axis is horizontally arranged; the metal separator is arranged perpendicularly to the cylinder axis.

[0012] Further, at least two of the electrochemical destabilizers are arranged in parallel.

[0013] Further, the cylinder is of split structure and detachably connected through flanges.

[0014] In the second aspect, the present application further provides a low-power high-efficiency precipitation device comprising any of the above-mentioned electrochemical destabilizers, flocculation equipment, precipitation equipment and sludge hopper; the electrochemical destabilizer, the flocculation equipment, the precipitation equipment and the sludge hopper are sequentially communicated and sequentially lowered along the vertical height.

[0015] Further, the flocculation equipment comprises a first box body, a plurality of heterogeneous wave folded plates, a plurality of homogeneous wave folded plates and a plurality of parallel straight plates; the plurality of heterogeneous wave folded plates, the plurality of homogeneous wave folded plates and the plurality of parallel straight plates are respectively arranged vertically and spaced apart to form a continuous flow channel connected head to tail; the first box body is provided with a discharge port at a position corresponding to the bottom of the continuous flow channel and is provided with a liquid inlet and a liquid outlet communicated with the continuous flow channel at the top.

[0016] Further, the liquid inlet is communicated with the liquid outlet of the electrochemical destabilizer, and the liquid outlet is communicated with the liquid inlet of the precipitation equipment.

[0017] Further, the cross-sectional area of the flow channel formed between the heterogeneous wave folded plates, the cross-sectional area of the flow channel formed between the homogeneous wave folded plates and the cross-sectional area of the flow channel formed between the parallel straight plates are sequentially increased.

[0018] Further, the precipitation equipment comprises a second box body, a fluid distribution member, a filler layer and a cofferdam; the filler layer is arranged in the second box body and divides the space in the second box body into a clear water area above the filler layer and a precipitation area below the filler layer; the fluid distribution member is arranged in the precipitation area and adjacent to the feed inlet of the second box body for shunting the fluid flowing into the feed inlet; the cofferdam is arranged on the discharge side of the filler layer, and the top height of the cofferdam is higher than the discharge port of the second box body, so that the fluid overflows via the top edge of the cofferdam and then flows out through the discharge port of the second box body; the sludge outlet at the bottom of the second box body is vertically above the sludge hopper.

[0019] Further, the cofferdam top edge distance from the second box inner wall top surface is H1, H1≥0.5m; and / or, the cofferdam height H2≥0.3m; and / or, the filler layer height H3 is 0.866m; and / or, the height of the precipitation zone H4≥2m.

[0020] Further, the filler layer is inclined pipe or inclined plate filler, the inclination is 60°.

[0021] Further, the fluid distribution member is a distribution baffle, the height is 1.5m, the two side edges are connected to the second box inner wall, the fluid distribution member is provided with a through hole, and the opening ratio is 2-3%.

[0022] Further, the sludge hopper is a square hopper, and the inclination angle of each hopper wall is 60°.

[0023] The beneficial effects of the present application are as follows: the electrochemical destabilizer of the present application is based on setting a plurality of nickel-chromium-zinc-copper alloy metal separators in the barrel, and setting communication holes on the metal separators to form flow channels, and the fluid to be destabilized flows through each metal separator to complete the destabilization process, without the need for external energy, and is more energy-saving; and the working conditions are not affected by pressure and temperature, and do not need maintenance during use, and are easier to operate; and have a long service life. BRIEF DESCRIPTION OF DRAWINGS

[0024] Figure 1 is a structural schematic view of the electrochemical destabilizer of the present application;

[0025] Figure 2 is a structural schematic view of the metal separator of the present application;

[0026] Figure 3 is a structural schematic view of the low-power high-efficiency precipitation device of the present application.

[0027] Legend: 1. electrochemical destabilizer; 11. barrel; 12. metal separator; 121. communication hole; 13. flow section; 2. flocculation equipment; 21. first box; 211. liquid inlet; 212. liquid outlet; 22. different wave folded plate; 23. same wave folded plate; 24. parallel straight plate; 25. discharge port; 3. precipitation equipment; 31. second box; 311. clear water zone; 312. precipitation zone; 313. feed inlet; 314. discharge outlet; 32. fluid distribution member; 33. filler layer; 34. cofferdam; 4. sludge hopper. DETAILED DESCRIPTION

[0028] In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the following will be combined with the accompanying drawings for the embodiments of the present application to make a clear and complete description of the technical solutions of the embodiments of the present application. Obviously, the described embodiments are only some of the embodiments of the present application, but not all the embodiments of the present application.

[0029] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs; the terminology used in the description herein is for describing the specific embodiments of the application only and is not intended to be limiting of the application; the terms "including", "comprising" and "having" as used in the specification herein and in the claims herein and the above description are intended to be inclusive of a wide variety of embodiments and are intended to be open-ended terms. The terms "comprises", "comprising", "includes", "including" and "have" or "has" as used herein and in the claims herein and the above description are intended to be open-ended terms that specify the presence of stated features, elements, components, members, integers, steps, or the like, but do not preclude the presence or addition of one or more other features, elements, components, members, integers, steps, or the like.

[0030] Reference herein to "an embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment can be included in at least one embodiment of the application. The appearances of the phrase in various places in the specification are not necessarily all referring to the same embodiment, nor are they necessarily mutually exclusive of one another. As will be apparent to those of ordinary skill in the art, embodiments described herein can be combined with other embodiments.

[0031] An electrochemical destabilizer and a low-power high-efficiency precipitation device are described in detail below with reference to the accompanying drawings.

[0032] As shown in FIGS. Figure 1 and 2 An electrochemical destabilizer includes a cylinder 11 and a plurality of metal separators 12; the metal separators 12 are arranged at intervals in the cylinder 11 to divide the space between the liquid inlet and the liquid outlet of the cylinder 11 into a plurality of flow sections 13, and the metal separators 12 are provided with communication holes 121; the communication holes 121 are used to communicate adjacent flow sections 13; and the metal separators 12 are made of at least zinc, copper, nickel and chromium.

[0033] The electrochemical destabilizer of the present application is based on setting multiple metal separators of nickel-chromium alloy in the barrel, and setting communication holes on the metal separators to form flow channels. The destabilization process is completed after the fluid to be destabilized flows through each metal separator. The electrochemical reaction between zinc, copper, nickel and chromium destroys the colloid charge balance in the fluid, thereby realizing destabilization. In the experimental water sample, the colloid Zeta potential is reduced from-30 mV to the minimum-3 mV (close to the critical value), which realizes destabilization without external energy and is more energy-saving. The working conditions are not affected by pressure and temperature, and the pH value of the fluid to be destabilized can be adjusted, so that maintenance is not required during use, operation is easier, and the service life is long. No medicament needs to be added, and the sludge amount can be reduced by 30-40%.

[0034] In some preferred embodiments, the mass percentage of nickel in the metal separator 12 is 10-14%, the mass percentage of chromium is 16-22%, the mass percentage of zinc is 4-20%, and the balance is copper. Based on this, the self-corrosion rate of the metal separator is reduced while ensuring the destabilization rate. Within this range, the destabilization rate, the self-corrosion rate and the potential difference (mV) of the micro-battery are all better. The destabilization rate is 40-80%, the self-corrosion rate is 0.1-0.5 mm / a, the potential difference (mV) of the micro-battery is 200-400, and the pH adjustment range is 5-9.

[0035] In the coagulation and sedimentation experiment, the destabilization rate is a key indicator for measuring the loss of stability of colloidal particles and the beginning of aggregation due to the action of coagulants, which is usually defined and calculated by the following two methods:

[0036] 1. Based on the change of surface charge of colloidal particles

[0037] The stability of colloidal particles mainly depends on the electrostatic repulsion force formed by the surface charge (such as Zeta potential). The destabilization rate can be characterized by the decrease of Zeta potential. The higher the destabilization rate, the better the surface destabilization effect:

[0038] Destabilization rate = (ζ0-ζ final ) / ζ0x100%;

[0039] ζ0: initial Zeta potential (mV) of colloids at the inlet of the electrochemical destabilizer 1;

[0040] ζ final : Zeta potential (mV) at the outlet of the electrochemical destabilizer 1.

[0041] Critical value: when the Zeta potential is close to the isoelectric point (such as <5 mV), it is considered that the colloids are fully destabilized, and the destabilization rate tends to 100%. The Zeta potential is measured by the Zeta potential method.

[0042] 2. Based on turbidity or particle concentration

[0043] By testing the change of oil degree or particle concentration before and after coagulation, the destabilization effect is indirectly reflected:

[0044] Destabilization rate = (Co-Ct) / Co x 100%

[0045] Co: oil degree (NTU) or particle concentration (mg / L) of raw water, i.e. oil degree (NTU) or particle concentration (mg / L) at the inlet of the electrochemical destabilizer 1;

[0046] Ct: turbidity or particle concentration after a certain time of coagulation reaction, i.e. turbidity or particle concentration at the outlet of the electrochemical destabilizer 1.

[0047] The turbidity measurement method can adopt a scattering turbidimetry method, a spectrophotometry method, a visual turbidimetry method or a transmission method. The present application adopts the spectrophotometry method.

[0048] In some preferred embodiments, the metal separator 12 further comprises aluminum and / or magnesium. The simultaneous presence of magnesium and zinc produces a synergistic effect, improving the potential difference of the micro-battery; especially, the simultaneous increase of aluminum and magnesium is more optimal for improving the destabilization rate. The mass percentage of each component is aluminum: 1%-2%, magnesium: 2%-2.8%; thereby, the destabilization rate can be improved by 15-30%; the destabilization rate is 68-98%; the self-corrosion rate is 0.1-0.5 mm / a; and the potential difference (mV) of the micro-battery is 280-680.

[0049] Preferably, the mass percentage of nickel in the metal separator 12 is 12-13%, the mass percentage of chromium is 19-20%, the mass percentage of zinc is 12-16%, and the mass percentage of magnesium is 2.4%-2.8%; at this time, the destabilization rate can achieve the optimal effect of the self-corrosion rate; the destabilization rate is 90-95%, the self-corrosion rate is 0.18-0.25 mm / a, and the pH can be adjusted within the range of 6.3-8.5.

[0050] In some preferred embodiments, the metal separator 12 further comprises manganese and titanium. The mass percentage of each component is manganese: 1%-2%, titanium: 1%-2%; based on the addition of manganese and titanium, the strength of the metal separator 12 can be improved, and the corrosion resistance is improved, thereby improving the service life; preferably, the mass percentage of manganese in the metal separator 12 is manganese: 1.5%-1.8%, and the mass percentage of titanium is 1.3%-1.8%.

[0051] In some preferred embodiments, the metal separator 12 further comprises iron and carbon, and the mass percentage of each component is as follows: iron: 0.1-5%, carbon: ≤0.05%. If the content of iron is too high, the processability of the alloy will be reduced, and if the content of carbon is too high, the grain boundary brittleness will be increased. Preferably, the mass percentage of iron and carbon is as follows: iron: 2-3%, carbon: ≤0.03%.

[0052] The preparation steps of the metal separator 12 are as follows: the raw materials are added in two batches. The first batch is zinc, magnesium, aluminum, and copper. The metal materials are melted at a high temperature, and the furnace opening temperature is controlled at 900-1100°C. After all the metals are melted, the molten metal is degassed for 5-10 min to reduce the content of impurities and gases. Then the remaining metal raw materials are added, and the furnace temperature is controlled at 1800-2000°C. Slow stirring is performed to remove dross. When the furnace temperature decreases to about 1300°C, the molten alloy is poured into a mold to form a metal disc with the desired shape. Further cold working is performed to further refine the grains and improve the strength and surface quality of the alloy. Finally, polishing and cleaning are performed to improve the surface finish, remove the oxide layer, and remove contaminants.

[0053] In some preferred embodiments, the metal separator 12 comprises a plurality of communication holes 121, and the sum of the areas of the plurality of communication holes 121 is greater than or equal to 92% of the area of the metal separator 12. In this way, the destabilization rate can be greater than 90%.

[0054] Preferably, the diameter of the communication hole 121 includes 5mm, and / or 12mm, and / or 27mm. Further preferably, the diameters of the communication holes 121 of adjacent two metal separators 12 are different. Further preferably, the diameter of the metal separator 12 includes 5mm, 12mm, and 27mm. In this way, the turbulent effect of the flow is increased, thereby improving the destabilization effect.

[0055] Further preferably, the spacing between adjacent metal separators 12 is greater than or equal to 6 times the thickness of the metal separator 12. If the spacing is too large, the destabilization rate will decrease, especially when the spacing is greater than 8 times the thickness, the destabilization rate will decrease by 15%. If the spacing is too small, the pressure drop will increase, affecting the subsequent flocculation and sedimentation process. Preferably, the spacing between adjacent metal separators 12 is greater than or equal to 6 times the thickness of the metal separator 12 and less than or equal to 8 times the thickness.

[0056] When the sum of the areas of the plurality of communication holes 121 is greater than or equal to 92% of the area of the metal separator 12, the diameter of the communication hole 121 includes 5mm, and / or 12mm, and / or 27mm, and the spacing between adjacent metal separators 12 is greater than or equal to 6 times the thickness of the metal separator 12, the water quality can be observed by the naked eye to have flocculation, and the colloidal Zeta potential in the effluent is detected to be less than -10mV, indicating that the colloidal particles have been destabilized and are easy to coagulate.

[0057] In some preferred embodiments, the water flow velocity within the electrochemical destabilizer is controlled between 0.8 and 2.5 m / s (this requirement applies to both pore and non-pore areas) to prevent excessive residence time leading to sedimentation of suspended solids and insufficient reaction due to insufficient residence time. The optimal flow velocity is 1.2 m / s.

[0058] In some preferred embodiments, the cylinder 11 is arranged horizontally along its axis; the metal partition 12 is arranged perpendicular to the axis of the cylinder 11.

[0059] In some preferred embodiments, the cylinder 11 is a split structure, detachably connected by flanges, thereby facilitating internal maintenance and replacement.

[0060] The following verifies the effect of different materials of the metal partition 12 on the destabilization efficiency, and the results are shown in the table below:

[0061]

[0062]

[0063] As can be seen from the table above, compositions numbered 2, 8, and 9 all exhibited good destabilization and self-corrosion rates, with composition number 2 being the best.

[0064] Example 2

[0065] This embodiment provides a low-power, high-efficiency sedimentation device, such as... Figure 3 As shown, it includes the electrochemical destabilizer 1, flocculation device 2, sedimentation device 3 and sludge hopper 4 in the above embodiment 1; the electrochemical destabilizer 1, flocculation device 2, sedimentation device 3 and sludge hopper 4 are connected in sequence and decrease in height in sequence.

[0066] The low-power, high-efficiency sedimentation device of the present invention has no internal power equipment. It only needs to lift the mine water into the electrochemical destabilizer and then rely on gravity to achieve the flow process, resulting in low operating costs and investment. Moreover, the electrochemical destabilizer, flocculation equipment, sedimentation equipment and sludge hopper are arranged vertically, which reduces the footprint. The low-power, high-efficiency sedimentation device of the present invention is internally enclosed and is not affected by the external environment. It is not easy for algae to grow and produces good water quality.

[0067] In some preferred embodiments, the flocculation device 2 comprises a first tank 21, a plurality of wave-shaped baffles 22, a plurality of straight baffles 23, and a plurality of parallel straight plates 24, i.e. the parallel straight plates form straight flow channels; the plurality of wave-shaped baffles 22, the plurality of straight baffles 23, and the plurality of parallel straight plates 24 are arranged vertically and spaced apart to form a continuous flow channel connected at the head and tail; the first tank 21 is provided with a discharge port 25 at a position corresponding to the bottom of the continuous flow channel, and is provided with a liquid inlet port 211 and a liquid outlet port 212 at the top and in communication with the continuous flow channel, so that the fluid flows from top to bottom and then from bottom to top; based on this structure, stirring is not required during flocculation, and energy saving is achieved.

[0068] Preferably, the first tank 21 is square, and further preferably, the horizontal cross section of the first tank 21 is square.

[0069] Preferably, the residence time of the fluid in the flocculation device 2 is 15-20 minutes, and most preferably, the residence time is 18 minutes. Further preferably, the flocculation time of the first wave-shaped baffles and the second wave-shaped baffles is greater than 5 minutes.

[0070] Preferably, the included angle of the wave-shaped baffles 22 and the straight baffles 23 is 90-120°, based on which, the hydraulic conditions can be optimized and the cost of the device can be controlled; when the included angle is less than 90° (e.g. 60°), the baffles are prone to cracking due to stress concentration; when the included angle exceeds 120°, the structural strength may be reduced, affecting the long-term operation stability.

[0071] Further preferably, the included angle of the wave-shaped baffles 22 increases from the inflow side to the outflow side, e.g. the included angle of the inflow side is 90° and the included angle of the outflow side is 120°, thereby improving the turbulence effect, promoting the rapid formation of flocs in the initial flocculation stage, and increasing the contact time of the water flow, promoting the combination of small particles into large particles, and reducing energy consumption.

[0072] Preferably, the material of the baffles is the same as that of the device, and the maintenance process is omitted.

[0073] Preferably, the distance between the discharge port 25 and the bottom surface of the first tank 21 is less than 0.2 m.

[0074] In some preferred embodiments, the liquid inlet port is in communication with the liquid outlet port of the electrochemical destabilizer 1, and the liquid outlet port is in communication with the liquid inlet port of the sedimentation device 3.

[0075] In some preferred embodiments, the cross-sectional area of the flow channel formed between the wave-shaped baffles 22, the cross-sectional area of the flow channel formed between the straight baffles 23, and the cross-sectional area of the flow channel formed between the parallel straight plates 24 increase in sequence.

[0076] Preferably,

[0077] The flow velocity of the flow channel formed between the corrugated plates 22 is 0.25-0.35 m / s at the crest and 0.1-0.15 m / s at the trough;

[0078] The flow velocity of the flow channel formed between the corrugated plates 23 is 0.15-0.25 m / s;

[0079] The flow velocity of the flow channel formed between the parallel straight plates 24 is 0.10-0.15 m / s; thus, the flocculation effect is better, and the flocculation material is prevented from depositing in the flocculation device 2.

[0080] In some preferred embodiments, the precipitation device 3 comprises a second tank 31, a fluid distributor 32, a filler layer 33, and a cofferdam 34; the filler layer 33 is arranged in the second tank 31 and divides the space in the second tank 31 into a clear water area 311 above the filler layer 33 and a precipitation area 312 below the filler layer 33; the fluid distributor 32 is arranged in the precipitation area 312 and is adjacent to a feed inlet 313 of the second tank 31, for distributing the fluid flowing into the feed inlet; the cofferdam 34 is arranged on the discharge side of the filler layer 33, and the top of the cofferdam 34 is higher than the discharge outlet 314 of the second tank 31, i.e., the feed inlet 313 is low and the discharge outlet 314 is high; so that the fluid overflows through the top edge of the cofferdam 34 and then flows out through the discharge outlet of the second tank 31; the sludge outlet at the bottom of the second tank 31 is vertically above the sludge hopper 4; based on this, the larger suspended flocculation material that has been gathered is precipitated, so as to separate the suspended material in the water.

[0081] In some preferred embodiments, the second tank 31 is square, and the liquid surface load is 8 m 3 / (m 2 ·h) to 20 m 3 / (m 2 ·h), and the optimal value is 15 m 3 / (m 2 ·h). The horizontal cross section of the second tank 31 is square, and the length and width are consistent with those of the first tank 21, i.e., the first tank 21 and the second tank 31 can be formed by arranging a partition plate in one tank.

[0082] In some preferred embodiments, a flushing device is further included for flushing the filler layer 33.

[0083] In some preferred embodiments, the distance between the top edge of the cofferdam 34 and the inner wall top surface of the second tank 31 is H1, and H1≥0.5 m; and / or, the height H2 of the cofferdam 34 is≥0.3 m; and / or, the height H3 of the filler layer 33 is 0.866 m; and / or, the height H4 of the precipitation area 312 is≥2 m, so as to reduce the flow velocity in the precipitation area 312, achieve uniform water distribution, and facilitate the sinking of the sludge falling from the filler layer 33, and reduce interference.

[0084] In some preferred embodiments, the filler layer 33 is a sloping tube or plate filler with an inclination angle of 60°.

[0085] In some preferred embodiments, the filler layer 33 is a sloping tube filler with a tube diameter of 80 mm and a length of 1.0 m, and is made of polyvinyl chloride or glass fiber reinforced plastic.

[0086] In some preferred embodiments, the fluid distributor 32 is a distribution baffle with a height of 1.5 m, and the two side edges are connected to the inner wall of the second tank 31. The fluid distributor 32 is provided with through holes, and the opening rate is 2-3%. Based on this, under the premise of meeting the uniformity requirement of water distribution, the flow rate of the incoming water through the through holes is low, which can reduce the disturbance to the sedimentation zone 312, maintain the stability of the flow state in the sedimentation zone 312, reduce the shear damage of high-speed water flow to the formed flocculation body, ensure the sedimentation effect, and prevent short flow.

[0087] Preferably, the through hole flow rate of the through holes is ≤0.15 m / s, and the hole diameter is 50 mm.

[0088] In some preferred embodiments, the sludge hopper 4 is a square hopper, and the inclination angle of each hopper wall is 60°. If the inclination angle of the sludge hopper is too small (e.g., less than 55°), the sludge will adhere to the hopper wall and be difficult to automatically slide down, causing blockage or reducing the sludge discharge efficiency. If the inclination angle is too large, it is not conducive to sedimentation. Selecting an inclination angle of 60° can realize smooth sliding of the sludge by gravity, reducing the frequency of manual cleaning.

[0089] In some preferred embodiments, the discharge pipe of the sludge hopper 4 has a diameter of 200 mm or more. When the diameter of the sludge discharge pipe is too small, the frictional resistance of the sludge flow increases significantly, resulting in a decrease in flow rate or even blockage. A larger diameter sludge discharge pipe reduces the frequency of daily cleaning and maintenance, and reduces the risk of failure due to pipe wear or corrosion.

[0090] In some preferred embodiments, at least two electrochemical destabilizers 1 are included, and the two electrochemical destabilizers 1 are arranged in parallel, one in operation and one as a backup, to realize continuous production.

Claims

1. An electrochemical destabilizer characterized by, The cylinder (11) and a plurality of metal separators (12) are included. The metal separators (12) are arranged in the cylinder (11) to divide the space between the liquid inlet and the liquid outlet of the cylinder (11) into a plurality of flow sections (13), and the metal separators (12) are provided with communication holes (121); the communication holes (121) are used to communicate adjacent flow sections (13); the metal separators (12) are made of zinc, copper, nickel and chromium.

2. An electrochemical destabilizer according to claim 1, wherein The mass percentage of nickel in the metal separators (12) is 10-14%, the mass percentage of chromium is 16-22%, the mass percentage of zinc is 4-20%, and the balance is copper.

3. An electrochemical destabilizer according to claim 1 or 2, characterized in that The metal separators (12) also include aluminum and / or magnesium, and the mass percentage of each component is: aluminum: 1%-2%, magnesium: 2%-2.8%.

4. An electrochemical destabilizer according to claim 1, wherein The metal separators (12) include a plurality of communication holes (121). The sum of the areas of the plurality of communication holes (121) is greater than or equal to 92% of the area of the metal separators (12).

5. An electrochemical destabilizer according to claim 1, wherein The diameter of the communication hole (121) is 5mm, and / or 12mm, and / or 27mm.

6. An electrochemical destabilizer according to claim 1, wherein The distance between adjacent metal separators (12) is greater than or equal to 6 times the thickness of the metal separators (12).

7. An electrochemical destabilizer according to claim 1, wherein The axis of the cylinder (11) is arranged horizontally; the metal separators (12) are arranged perpendicular to the axis of the cylinder (11).

8. A low power high efficiency sedimentation device, characterized by, The electrochemical destabilizer (1), the flocculation device (2), the precipitation device (3) and the sludge hopper (4) are sequentially communicated and sequentially lowered in vertical height. The flocculation device (2) includes a first box body (21), a plurality of different wave folded plates (22), a plurality of same wave folded plates (23) and a plurality of parallel straight plates (24).

9. A low power high efficiency sedimentation device according to claim 8, wherein, The plurality of different wave folded plates (22), the plurality of same wave folded plates (23) and the plurality of parallel straight plates (24) are arranged vertically and spaced apart to form a continuous flow channel connected head to tail. The first box body (21) is provided with a discharge port (25) corresponding to the position of the bottom of the continuous flow channel, and the top is provided with a liquid inlet (211) and a liquid outlet (212) communicated with the continuous flow channel. The cross-sectional area of the flow channel formed between the different wave folded plates (22), the cross-sectional area of the flow channel formed between the same wave folded plates (23) and the cross-sectional area of the flow channel formed between the parallel straight plates (24) increase in turn.

10. A low power high efficiency sedimentation device according to claim 9, wherein, The precipitation device (3) includes a second box body (31), a fluid distribution member (32), a filler layer (33) and a cofferdam (34).

11. A low power high efficiency sedimentation device according to claim 8, wherein, The filler layer (33) is arranged in the second box body (31) and divides the space in the second box body (31) into a clear water area (311) above the filler layer (33) and a precipitation area (312) below the filler layer (33). ​ The fluid distributor (32) is arranged in the sedimentation zone (312) and adjacent to the feed inlet (313) of the second tank (31) to distribute the fluid flowing into the feed inlet (313); The cofferdam (34) is arranged at the discharge side of the filler layer (33), and the top of the cofferdam (34) is higher than the discharge outlet (314) of the second tank (31) so that the fluid overflowing from the top edge of the cofferdam (34) flows out through the discharge outlet (314) of the second tank (31); The sludge outlet at the bottom of the second tank (31) is vertically above the sludge hopper (4).

12. A low power high efficiency sedimentation device according to claim 8, wherein, The sludge hopper (4) is a square hopper, and the inclination angle of each hopper wall is 60°.

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