CN217780804U - Ion type mine effluent treatment plant - Google Patents
Ion type mine effluent treatment plant Download PDFInfo
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- CN217780804U CN217780804U CN202220239269.5U CN202220239269U CN217780804U CN 217780804 U CN217780804 U CN 217780804U CN 202220239269 U CN202220239269 U CN 202220239269U CN 217780804 U CN217780804 U CN 217780804U
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Abstract
The utility model relates to an ion type mine effluent treatment plant, including the combination formula air supporting system that the flocculation cell body unit of four rectangles and the air supporting pond of four rectangles are constituteed, combination formula air supporting system includes the district of intaking, flocculation district, contact zone, air supporting district, play water zone, dissolve gas pitcher and backflow pipeline district that set gradually along the rivers direction. The treatment device of the utility model realizes the neutralization and precipitation and the graded recovery of valuable metals in the whole system by reasonably controlling the sulfide content, the pH value and the air flotation deslagging process in the acid wastewater at different stages; the system has the advantages of simple process, convenient maintenance, low treatment cost and small occupied area, and the treated wastewater reaches the discharge standard of surface water class 3 water bodies. The utility model discloses an even ion type mine effluent treatment plant is under the unstable and higher pollution load condition of the condition of intaking, still can well move, guarantees that sewage is effectively purified, and it is good to go out water quality of water.
Description
Technical Field
The utility model belongs to the technical field of water treatment, especially, relate to an ion type mine effluent treatment plant, concretely relates to waste water treatment plant that still can effectively get rid of heavy metal pollutants in the waste water under lower pH, the higher sulfate content condition.
Background
Mine wastewater discharged out of control without proper treatment poses serious threats to the ecological environment function and public health safety of underground water, and the inorganic pollution of the underground water becomes one of the main problems of water quality safety of water sources in the present stage of China. The iron and manganese elements are common elements causing inorganic pollution to underground water, generally caused by dissolution of iron and manganese in indissolvable compounds of rocks and minerals through microorganism-mediated oxidation reaction, mainly exist in mine wastewater in the form of divalent iron ions and divalent manganese ions, and the mine wastewater generally has the characteristics of low pH, high iron, high manganese and high sulfate.
At present, for mine wastewater treatment, the problems of large sludge production, quick system failure, poor selectivity and secondary pollution caused by the formation of calcium sulfate sludge still exist in a mainstream neutralization and precipitation process, and a sulfide precipitation method has the advantages of good valuable metal separation effect, wide pH application range, small sludge production and the like, and becomes a feasible exploration direction. The biological sulfide precipitation process is a new mine wastewater treatment process based on sulfur reduction and low sludge production. In the process, sulfate in the mine wastewater is firstly reduced into sulfide under the action of sulfate reducing bacteria, and then the sulfide reacts with heavy metal to form an insoluble metal sulfide complex, so that the aim of purifying the water body is fulfilled. The process can meet the water treatment requirements of removing heavy metals, reducing organic matters, improving the biodegradability of water and the like, and solves the problem of generating a large amount of calcium sulfate sludge in conventional treatment of mine wastewater from the source.
However, in the application of the biological sulfide precipitation method, the conventional treatment device is difficult to inhibit the generation of hydrogen sulfide gas while achieving the strict anaerobic environment required by sulfate reducing bacteria, and the requirement on the air tightness of the device is high; and microorganisms directly contacted with the mine wastewater are stressed by heavy metal ions to influence the efficiency of reducing sulfate, and divalent sulfur ions are unstable and cannot be subjected to fractional precipitation according to the difference of solubility products of different insoluble compounds. Moreover, the complex formed by the biological sulfide precipitation method has small particle size and is difficult to clarify and separate; the single-stage bioreactor is not easy to clean, the heavy metal is difficult to recover, and secondary pollution can be caused by improper treatment.
Therefore, how to construct a reaction device and a treatment process for making up for various technical defects based on a biological sulfide precipitation method is an urgent problem to be solved in the application of a biological sulfide precipitation process in mine wastewater treatment.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides an ion type mine waste water physics, chemical combination processing apparatus.
In order to realize the above-mentioned purpose, the utility model provides an ion type mine effluent treatment plant, including the combination formula air supporting system that the flocculation cell body unit of four rectangles and the air supporting pond of four rectangles are constituteed, combination formula air supporting system includes water inlet area, flocculation district, contact zone, air supporting district, play water receptacle, dissolves gas pitcher and backward flow pipeline district that sets gradually along the rivers direction, the water inlet area includes inlet tube, solution tank, inlet opening, the flocculation district includes flocculation tank, mechanical coagulation unit, crosses water hole, overflow wall, evacuation groove, blow-down pipe, mechanical coagulation unit is including thoughtlessly congealing the brush and accuse fast unit, the contact zone includes the contact chamber, dissolves gas release unit and crosses the water board, the air supporting district includes disengagement chamber, scum machine, slag runner, wash pipe, scum pipe, tubular water collector and mud discharging structure, the play water receptacle includes water sluice, catch basin and outlet pipe, dissolve gas pitcher and backward flow pipeline district including dissolving gas reflux pipe, pressure dissolve gas pitcher and storage tank.
Preferably, sewage is alternately distributed into the solution tank by an automatic control water inlet pump equipped with the water inlet distribution well, and the sewage enters from a jet flow spray head arranged at the bottom of the water inlet distribution well; the water inlet hole is positioned at the bottom of the wall of the solution tank separated from the flocculation tank; the flocculation tank comprises a first flocculation chamber, a second flocculation chamber and a third flocculation chamber which are arranged along the water flow direction, and water flow enters the contact area through the water holes and the overflow wall; the water passing holes are respectively positioned below the first flocculation chamber and the second flocculation chamber and below the connecting pool wall of the third flocculation chamber and the contact area; the overflow wall is positioned on the walls of the second flocculation chamber and the third flocculation chamber and has a height of 80% of the height of the flocculation tank wall; emptying grooves are formed in the bottom of the flocculation tank along the long edge direction and the short edge of the water inlet side; the emptying pipes are positioned at two corners of the emptying groove and below the groove body; the mechanical coagulation unit is provided with two groups of coagulation rotating brushes, a partition plate used for fixing a rotating shaft is arranged between the two groups of coagulation rotating brushes, the height of the partition plate is 40% -45% of the depth of the flocculation chamber, the thickness of the partition plate is equivalent to that of the tank wall, the length of the coagulation rotating brush is not higher than 0.8 time of the effective water depth of the flocculation chamber, the length of each blade is 0.75-0.85 time of the width of the flocculation tank, and the width of each blade is not less than 0.25m.
Preferably, the length-width ratio of the contact chamber is 1-1, the width of the contact chamber is the same as that of the flocculation chamber, the effective water depth is not less than 3.0m, the bottom gradient is greater than 0.1, and the hydraulic retention time is not higher than 8min; the dissolved air releasing unit adopts a TV type dissolved air releaser, the specification is that the diameter of a connector is 25mm, two groups are arranged in one group, and seven groups are arranged in two rows.
Preferably, the length-to-width ratio of the separation chamber is 2.25; the slag discharging groove is positioned on the water outlet side of the air flotation zone, the length of the slag discharging groove is not less than 0.4m, the width of the slag discharging groove is equivalent to that of the air flotation zone, the height of the slag discharging groove is not less than 0.6m, and the slag discharging groove slopes to one end of the slag discharging pipe at a gradient of 1%; the slag discharge pipe is positioned at the bottom of the slag discharge groove on the outer side of the tank body; the tubular water collector is positioned at the bottom of the separation chamber, the length of the tubular water collector is 45-55 percent of that of the separation chamber, the diameter of the tubular water collector is 250mm, and the flow velocity of effluent is 0.1-1.0 m/s; the separation chamber bottom of the pool sets up the sludge discharging structure, the sludge discharging structure includes six groups of sludge hoppers, sets up perforation sludge discharge pipe, connection under the sludge hopper the sludge discharge ditch of perforation sludge discharge pipe, the sludge discharge communicating pipe and the setting of two groups of separation district sludge discharge ditch of intercommunication are in the final sludge discharge main pipe of sludge discharge ditch.
Preferably, the water outlet gates are provided with electric rising stem type gate opening and closing machines for controlling opening and closing, and each separation chamber is provided with three water outlet gates; the length of the water collecting channel is 1.8-3.2 m, the wall thickness is 0.2-0.5 m, the height is 75-85% of the height of the pool body, and the water collecting channel is provided with an adjustable weir gate; the water outlet pipe is positioned at the bottom of the water collecting ditch.
Preferably, the dissolved air backflow pipe starts from a water collecting channel of the water outlet area, and backflow water is pumped to the pressure dissolved air tank through the dissolved air pump; and air in the air storage tank is conveyed to the pressure dissolved air tank by the air compressor unit.
Based on the technical scheme, the utility model has the advantages that:
the utility model discloses an ion type mine effluent treatment plant, according to four process stage cycle operation, effectively solved conventional processing apparatus and difficult production that suppresses the hydrogen sulfide gas when reaching the required strict anaerobic environment of sulfate reducing bacteria, the microorganism receives heavy metal ion to coerce can influence the efficiency of reduction sulfate, can't carry out the fractional precipitation according to the difference of different indissolvable compound solubility products, the problem of valuable metal recovery difficulty.
The combined air floatation system of the treatment device of the utility model has the operation method that the neutralization sedimentation and the grading recovery of valuable metals in the whole system are realized by reasonably controlling the sulfide content, the pH value and the air floatation deslagging process in the acid wastewater at different stages; the system has the advantages of simple process, convenient maintenance, low treatment cost and small occupied area, and the treated wastewater reaches the discharge standard of surface water class 3 water bodies. The utility model discloses an even ion type mine effluent treatment plant is under the unstable and higher pollution load condition of the condition of intaking, still can well move, guarantees that sewage is effectively purified, and it is good to go out water quality of water.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the invention and together with the description serve to explain the invention without undue limitation to the invention. In the drawings:
FIG. 1 is a schematic plan view of an ionic mine wastewater treatment apparatus;
FIG. 2 is a sectional view of the ionic mine wastewater treatment apparatus 1-1;
FIG. 3 is a sectional view of an ionic mine wastewater treatment apparatus 2-2;
FIG. 4 is a sectional view of an ionic mine wastewater treatment apparatus 3-3;
FIG. 5 is a sectional view of the ionic mine wastewater treatment apparatus 4-4.
Detailed Description
The technical solution of the present invention is further described in detail by the accompanying drawings and examples.
The utility model provides an ion type mine wastewater treatment device, as shown in figures 1-5, wherein the utility model discloses a preferred embodiment.
The utility model discloses a solve conventional processing apparatus and be difficult to restrain the production of hydrogen sulfide gas when reaching the required strict anaerobic environment of sulfate reducing bacteria, the microorganism receives heavy metal ion to coerce the efficiency that can influence reduction sulfate, can't carry out hierarchical the sediment according to the difference of different indissolvable compound solubility products, the reactor is not clear up well, the problem of valuable metal recovery difficulty, a three unit formula fractional precipitation device and supporting processing technology according to pH, the different workshop section solubility balanced states of sulphide concentration alternative control are proposed, in order to improve the recovery efficiency of valuable metal.
As shown in fig. 1, the ionic mine wastewater treatment device comprises a combined air floatation system composed of four rectangular flocculation tank units and four rectangular air floatation tanks, wherein the combined air floatation system comprises a water inlet area, a flocculation area, a contact area, an air floatation area, a water outlet area, a dissolved air tank and a return pipeline area which are sequentially arranged along the water flow direction.
The combined air flotation system main body is composed of 4 rectangular flocculation tank body units with the same size and 4 rectangular air flotation tanks with the same size, the length-width ratio of a single flocculation tank body is about 2, the length-width ratio of a single air flotation tank body is about 3, the specific specification is determined according to the incoming water condition, the width is not less than 5m, and the height is about 2.75-3.25 m. The wall thickness of the tank is 0.2-0.3 m, and the water inlet pipe and the water outlet pipe respectively penetrate through the tank walls and the water pipes at the two ends of the tank bodyThe height is positioned at the lower part of the tank body, is coaxial with the tank body and is 50-80 cm away from the device; the water flow enters the flocculation area through the water inlet hole. The bottom of the pool body is provided with an anti-seepage geomembrane which adopts two cloths and one membrane (400 g/m) 2 ～700g/m 2 ) The bottom base layer of the membrane is flat, the interfaces of the membrane, the partition wall and the outer wall edge are provided with anchoring ditches, the depth of the ditches is more than or equal to 0.6m, and the anchoring ditches are anchored by adopting clay or plain concrete. The top of the device is integrally provided with a waterproof ceiling and an I-shaped steel structure which is 0.8 to 1m higher than the top. The ceiling can be added with a photovoltaic panel to compensate part of the power consumption.
As shown in fig. 2, the water inlet area includes a water inlet pipe 1, a solution tank 2, and a water inlet hole 3. The sewage of the water inlet pipe 1 is alternately distributed into the water inlet to the solution pool 2 by an automatic control water inlet pump equipped with a water inlet distribution well, the diameter of the water inlet pipe is 400-600 mm, and the model is selected according to the actual situation. The mine wastewater contains a large amount of suspended particles, a grid storage tank pretreatment unit is arranged in front of the water inlet distribution well, and SS is controlled to be less than 500mg/L when the mine wastewater enters the combined air floatation device. The water inlet pipe 1 is arranged at the bottom of the solution tank 2 and is controlled by a water distribution pump to enter the solution tank 2 in a jet flow mode according to the water condition.
The sewage enters the room from a jet nozzle at the bottom, the solution pool 2 is square, the volume of the solution pool is 20-30 percent of the flocculation area, and the gradient of the bottom is not less than 0.02. The thickness of the tank wall is 0.2-0.25 m, and the height of the tank wall is 0.2m, so that the overflow of the solution during stirring is prevented. The sulfide saturated solution (prepared from separated and recycled elemental sulfur by the mass ratio of sodium sulfide to potassium sulfide powder of 1-1.
The water inlet hole 3 is positioned at the bottom of the tank wall of the solution tank 2 and the flocculation tank, has the same width as the solution tank 2, has the height of not less than 0.2m, and is controlled by a numerical control device to open and close up and down.
As shown in the figure and figure 3, the flocculation area comprises a flocculation tank 4, a mechanical coagulation unit 5, a water through hole 6, an overflow wall 7, an emptying groove 8 and an emptying pipe 9, and the mechanical coagulation unit 5 comprises a coagulation rotary brush and a speed control unit. The length-width ratio of a single tank of the flocculation tank 4 is 1.75-2.25, the width is not less than 5.0m, the effective water depth is not less than 2.5m, and the tank wall and the solution tank are as high as each other. Each flocculation tank is divided into three flocculation chambers, and water flows into the contact area through the water holes and the overflow wall. Each flocculation chamber is provided with a group of coagulation rotating brushes and a matched speed control device.
Specifically, sewage is alternately distributed into the solution pool 2 by an automatic control water inlet pump equipped with the water inlet distribution well, and the sewage enters from a jet flow nozzle arranged at the bottom of the water inlet distribution well; the water inlet hole 3 is positioned at the bottom of the wall of the solution tank 2 separated from the flocculation tank 4; the flocculation tank 4 comprises a first flocculation chamber, a second flocculation chamber and a third flocculation chamber which are arranged along the water flow direction, and water flow enters a contact zone through a water hole 6 and an overflow wall 7; the water passing holes 6 are respectively positioned below the first flocculation chamber and the second flocculation chamber and below the connecting pool wall of the third flocculation chamber and the contact area; the overflow wall 7 is positioned on the walls of the second flocculation chamber and the third flocculation chamber, and the height of the overflow wall is 80% of the height of the flocculation chamber wall; the bottom of the flocculation tank 4 is provided with emptying grooves 8 along the long edge direction and the short edges of the water inlet side for emptying the tank body during maintenance. And the emptying pipe 9 is positioned at two corners of the emptying groove 8 and below the groove body, has the diameter of 100mm and is an anti-corrosion pipe.
The mechanical coagulation unit 5 is equipped with two sets of coagulation rotating brushes for facilitating flocs and assisting in mixing circulation. The device is characterized in that a partition plate for fixing the rotating shaft is arranged between the two groups of coagulation rotating brushes, the height of the partition plate is 40% -45% of the depth of the flocculation chamber, the thickness of the partition plate is equivalent to the thickness of the tank wall, the length of each coagulation rotating brush is not higher than 0.8 time of the effective water depth of the flocculation chamber, the length of each blade is 0.75-0.85 time of the width of the flocculation tank, and the width of each blade is not less than 0.25m. The speed control unit controls the rotating brush to stir at a constant speed, so that the flocculation time is maintained at 5-30 min, and micro flocs are formed.
As shown in fig. 2, the contact zone includes a contact chamber 10, a dissolved air releasing unit 11, and a water passing plate 12. Preferably, the length-width ratio of the contact chamber 10 is 1. The dissolved air releasing unit 11 is a TV type dissolved air releaser, and the specification is that the diameter of a connector is 25mm, two groups are arranged in two rows, and the total number of the two groups is seven. And aiming at the condition that the air dissolving membrane is possibly blocked, a pulse sweeping mode is adopted for cleaning. The operation parameters of the dissolved gas release unit are that the pressure of 8-40% backflow pressurized water is 2-10 bar, and the power consumption per ton of water is 0.02-0.08 kWh. The specification and the hole distribution form of the water passing plate 12 are determined by a hydraulic optimization test, and the height of the water passing plate is 45-55% of the contact chamber inner wall. The water flow passes through the water plate 12, the ascending flow velocity reaches 30-40 m/h (the water temperature is more than 15 ℃), and the Reynolds number ranges from 800 to 1500. The water passing plate 12 is used for promoting the combination of bubble flocs, inducing the bubble bed to reversely rotate to form stratified flow and vertical laminar flow, increasing the rising possibility of bubbles and ensuring the uniform flow state.
The air flotation zone comprises a separation chamber 13, a foam scraper 14, a slag discharge groove 15, a flushing water pipe 16, a slag discharge pipe 17, a tubular water collector 18 and a sludge discharge structure. The length-width ratio of the separation chamber 13 is 2.25-3.75, the width is the same as that of the contact chamber 10, the effective water depth is not less than 2.5m, and the hydraulic retention time is 9-16 min; in the separation chamber 13, bubbles are concentrated to form a bubble bed (40-70 nm) near the water passing plate 12, and the flotation effect is enhanced by laminar flow in the tank.
The foam scraper 14 is an XSD foam scraper for scraping off a fine bubble scum layer (bubble bed) formed in the separation chamber. The track and the laying requirement are as follows, the top surface of the pool platform is flat when the pool platform is installed, the longitudinal straight line deviation of the track is not more than +/-3 mm, the longitudinal levelness of the track is not more than 1/1000, and the relative height of the two parallel tracks is not more than 3mm. The joints of the two parallel tracks are arranged in a staggered mode, and the staggered distance is larger than the wheel track.
Preferably, the slag discharging groove 15 is positioned on the water outlet side of the air flotation zone, has the length of not less than 0.4m, the width equivalent to that of the air flotation zone and the height of not less than 0.6m, and slopes to one end of the slag discharging pipe 17 by 1 percent of slope. The flushing water pipe 16 is a branch of the dissolved air backflow water pipe, has a pipe diameter of 70mm, and is used for flushing the slag discharge groove and accelerating the slag discharge process. The deslagging pipe 17 is positioned at the bottom of the deslagging groove 15 outside the tank body, and the pipe diameter is 200mm. The tubular water collector 18 is positioned at the bottom of the separation chamber 13, above the sludge discharge structure and next to the water outlet area, the length of the tubular water collector is 45-55% of that of the separation chamber, the diameter of the tubular water collector is 250mm, and the water outlet flow rate is 0.1-1.0 m/s.
Further, the bottom of the separation chamber 13 pool sets up the sludge discharging structure, the sludge discharging structure includes six sets of sludge bucket 19, sets up perforation sludge discharge pipe 20, connection under the sludge bucket 19 the sludge discharge ditch 21 of perforation sludge discharge pipe 20, the sludge discharge communicating pipe 30 and the setting of two sets of separation district sludge discharge ditch 21 are in the final sludge discharge main pipe 22 of sludge discharge ditch 21. The width of the bottom of the mud discharging hopper 19 is 0.25-0.5 m, the inclination angle of the hopper wall and the horizontal plane is 60 degrees, and the height of the hopper is 0.4-0.8 m; the perforated sludge discharge pipe 20 is arranged at the center of the bucket bottom, has the pipe diameter of 0.4-0.6 m and is 0.1-0.2 m away from the pool bottom, and periodically discharges magnetic flocs and residual sludge through a numerical control valve under the action of gravity. The sludge discharge ditch 21 is located below the separation chamber 13 and is used for collecting sludge collected by the perforated sludge discharge pipe 20 and the sludge discharge communicating pipe 30. The sludge discharge communicating pipe 30 is positioned below the bottom of the separation chamber 13 and is communicated with the sludge discharge ditches 21 of the two adjacent separation areas, so that the residual sludge is discharged from the sludge discharge main pipe 22 at one side, and the pipe diameter is 200mm. The mud discharging main pipe 22 is positioned at the tail end of the mud discharging ditch 21 and has a pipe diameter of 200mm. The sludge discharge period is 4-5 min, the head loss is 2-3%, and the hydraulic sludge discharge concentration is 1-5 g/L (the mechanical sludge discharge concentration is 15-25 g/L).
As shown in fig. 1 and 4, the water outlet area includes a water outlet gate 23, a water collecting channel 24 and a water outlet pipe 25. The water outlet gate 23 is controlled to open and close by an electric rising stem type gate hoist so as to lead the water flow of the tubular water collector to pass through. Each separation chamber is provided with three water outlet gates 23 with the specification of 400mm in diameter. The water collecting channel 24 is positioned in the water outlet area of the tank body, the length is 1.8-3.2 m, the wall thickness is 0.2-0.5 m, the height is 75-85% of the height of the tank body, and the water collecting channel is provided with an adjustable weir 26 for controlling the water outlet condition. The water outlet pipe 25 is positioned at the bottom of the water collecting ditch 24.
As shown in fig. 1 and 5, the dissolved air tank and the return pipeline section include a dissolved air return pipe 27, a pressure dissolved air tank 28, and an air tank 29. Preferably, the dissolved air return pipe 27 starts from the water collecting channel 24 of the water outlet area, and return water is lifted to the pressure dissolved air tank 28 through the dissolved air water pump 31, and the pipe diameter is 200mm. The pressure dissolved air tank 28 is a filling dissolved air tank with a diameter of 1200mm and a height of 3-4 m, and has the function of realizing sufficient contact between return water and air and accelerating air dissolution. The filling type gas dissolving tank adopts a step ring as a filler, the gas dissolving efficiency reaches 90 percent, the thickness of the filler layer is more than 0.8m, and the surface load is 1500-2000 m 3 /(m 2 D). The air storage tank 29 is 2000mm in diameter, 3-3.5 m in height and hollowThe air is delivered to the pressure dissolved air tank 28 by the air compressor unit 32, the installed power of the pressure dissolved air tank is 500-800 kW, and the rated working pressure is 40bar.
The utility model also provides an operation method of the ion type mine wastewater treatment device, the operation method comprises adjusting the negative logarithm pL of the solubility product of sulfide MS Controlling the grain diameter of the floc by pH, and controlling the grain diameter of the microbubbles to be 20-100 mu m by adjusting the reflux quantity and the dissolved gas pressure to be 3-10 bar and the rising flow rate; the nanometer-level micro-bubble release head is used, and the grain diameter of the micro-bubbles is controlled to be 100 nm-10 mu m.
Preferably, the first stage copper treatment step comprises: under the action of a lift pump, water flows through a flowmeter and enters a flocculation area, a first flocculation-air flotation stage operates under the condition that the pH is = 3-4, saturated biological sodium sulfide/potassium sulfide solution is added according to the quality of inlet water, the negative logarithm of sulfide solubility product reaches 30-35, after the water enters a contact area, the dissolved air pressure is 4bar under the action of a dissolved air releaser, the dissolved air water with 30% of reflux quantity is uniformly mixed with the water, the ascending flow rate is adjusted to be 25m/h, the particle size range of the generated nano-scale copper sulfide floc is 2-15nm, the floc is supported by a nano-scale micro-bubble layer with the particle size of 100 nm-5000 nm to float upwards and enters the air flotation area and is separated from the water through a foam scraper, and the hydraulic retention time of the stage is 20-30 min.
The second stage of lead and cadmium treatment comprises the following steps: under the action of a lift pump, water flows through a flowmeter and enters a flocculation zone, a second flocculation-air flotation stage operates under the condition that the pH is = 4-5, and a saturated biological sodium sulfide/potassium sulfide solution is added according to the quality of inlet water, so that the negative logarithm of the sulfide solubility product pL MS When the flotation of cadmium sulfide floc reaches 25-30, adding a lead sulfide dispersing agent, enabling the dissolved gas pressure to be 5bar after the water body enters the contact zone under the action of a dissolved gas releaser, uniformly mixing the dissolved gas water with the reflux quantity of 20% with the water body, and adjusting the rising flow rate to be 12-25m/h; after the cadmium sulfide is collected, adding 20-50 g/t of lead sulfide trapping agent sodium hexametaphosphate, and separating from the water body according to the same air flotation parameters.
Preferably, the third stage nickel and iron treatment step comprises: under the action of the lift pump, water flows through the flowmeter and enters the flocculation area, and the third flocculation areaThe air floatation stage is operated under the condition that the pH = 5-6.5, and a saturated biological sodium sulfide/potassium sulfide solution is added according to the quality of inlet water, so that the negative logarithm of the sulfide solubility product reaches 15-25; after the water body enters the contact zone, the dissolved gas pressure is 5-8 bar under the action of a dissolved gas releaser, the dissolved gas water with 20% of reflux quantity is uniformly mixed with the water body, and the ascending flow rate is adjusted to be 10-15 m/h; adding the additive in an amount of 5-10 x 10 -4 Discharging the sodium oleate serving as a nickel sulfide trapping agent in mol/L and a magnetic flocculant in an adding amount of 5-20 mg/L from the lower part of the tank body through a sludge discharge structure and separating the sodium oleate from a water body; the particle size range of the generated ferrous sulfide floc is 60-200 mu m, the floc is supported to float upwards by utilizing a micro-bubble layer with the particle size of 20-70 mu m, enters an air flotation area and is separated from a water body by a foam scraper.
Preferably, the fourth stage manganese treating step comprises: under the action of a lift pump, water flows through a flowmeter and enters a flocculation zone, a fourth flocculation-air flotation stage operates under the condition that the pH is = 7.5-8, and a saturated biological sodium sulfide/potassium sulfide solution is added according to the quality of inlet water, so that the negative logarithm of the sulfide solubility product reaches 10-15; after the water body enters the contact zone, under the action of a dissolved gas releaser, the dissolved gas pressure is 10bar, the dissolved gas water with 10 percent of reflux quantity is uniformly mixed with the water body, and the ascending flow velocity is adjusted to be 8m/h; the particle size range of the generated manganese sulfide floc is more than 200 mu m, the floc is supported to float upwards by utilizing a micro-bubble layer of 40-100 mu m, enters an air flotation zone and is separated from a water body by a foam scraper.
The utilization way of the valuable metal sulfide after recovery is as follows: after the heavy metal is removed and recovered as a precipitate by using a sulfuration biological reaction process, the precipitate mainly contains nano-scale metal sulfide, and the application fields of the precipitate include but are not limited to solar cells, electrode catalytic materials, medical antibacterial coating research and development and agricultural plant pathogenic fungi inactivation.
The utility model discloses an ion type mine effluent treatment plant and operation method thereof, according to four process stage cycle operation, effectively solved conventional processing apparatus and difficult production that suppresses the hydrogen sulfide gas when reaching the required strict anaerobic environment of sulfate reducing bacteria, the microorganism receives heavy metal ion to coerce can influence the efficiency of reduction sulfate, can't carry out the fractional precipitation according to the difference of different indissolvable compound solubility products, the problem of valuable metal recovery difficulty.
The combined air floatation system of the treatment device of the utility model has the operation method that the neutralization sedimentation and the grading recovery of valuable metals in the whole system are realized by reasonably controlling the sulfide content, the pH value and the air floatation deslagging process in the acid wastewater at different stages; the system has the advantages of simple process, convenient maintenance, low treatment cost and small occupied area, and the treated wastewater reaches the discharge standard of surface water class 3 water bodies. The utility model discloses an ion type mine effluent treatment plant is even under the unstable and higher pollution load condition of the condition of intaking, still can well move, guarantees that sewage obtains effective purification, and it is good to go out water quality of water.
It should be finally noted that the above examples are only intended to illustrate the technical solution of the present invention and not to limit it; although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that: the invention can be modified or equivalent substituted for some technical features; without departing from the spirit of the technical solution of the present invention, the present invention should be covered by the technical solution of the present invention.
Claims (6)
1. The utility model provides an ion type mine effluent treatment plant which characterized in that: the combined type air flotation system comprises four rectangular flocculation tank body units and four rectangular air flotation tanks, and comprises a water inlet area, a flocculation area, a contact area, an air flotation area, a water outlet area, a dissolved air tank and a backflow pipeline area which are sequentially arranged along the water flow direction, wherein the water inlet area comprises a water inlet pipe (1), a solution tank (2) and a water inlet hole (3), the flocculation area comprises a flocculation tank (4), a mechanical coagulation unit (5), a water passing hole (6), an overflow wall (7), an emptying groove (8) and an emptying pipe (9), the mechanical coagulation unit (5) comprises a coagulation brush and a speed control unit, the contact area comprises a contact chamber (10), a dissolved air release unit (11) and a water passing plate (12), the air flotation area comprises a separation chamber (13), a foam scraping machine (14), a slag discharging groove (15), a flushing water pipe (16), a slag discharging pipe (17), a tubular water collector (18) and a mud discharging structure, and the water outlet area comprises a water outlet sluice (23), a water collecting pipe (24) and a backflow pipe (25), and the dissolved air tank (27), a pressure and a pressure gas tank (29).
2. The ionic mine wastewater treatment apparatus according to claim 1, characterized in that: sewage is alternately distributed into the solution pool (2) by an automatic control water inlet pump equipped with the water inlet distribution well, and the sewage enters from a jet flow nozzle arranged at the bottom of the water inlet distribution well; the water inlet hole (3) is positioned at the bottom of the wall of the solution tank (2) separated from the flocculation tank (4); the flocculation tank (4) comprises a first flocculation chamber, a second flocculation chamber and a third flocculation chamber which are arranged along the water flow direction, and water flow enters a contact area through a water hole (6) and an overflow wall (7); the water passing holes (6) are respectively positioned below the first flocculation chamber and the second flocculation chamber and below the connecting pool wall of the third flocculation chamber and the contact area; the overflow wall (7) is positioned on the walls of the second flocculation chamber and the third flocculation chamber, and the height of the overflow wall is 80% of the height of the flocculation chamber wall; emptying grooves (8) are formed in the bottom of the flocculation tank (4) along the long edge direction and the short edge of the water inlet side; the emptying pipes (9) are positioned at two corners of the emptying groove (8) and below the groove body; the mechanical coagulation unit (5) is provided with two groups of coagulation rotating brushes, a partition plate used for fixing a rotating shaft is arranged between the two groups of coagulation rotating brushes, the height of the partition plate is 40% -45% of the depth of the flocculation chamber, the thickness of the partition plate is equivalent to that of the tank wall, the length of the coagulation rotating brush is not higher than 0.8 time of the effective water depth of the flocculation chamber, the length of a blade is 0.75-0.85 time of the width of the flocculation tank, and the width of the blade is not less than 0.25m.
3. The ionic mine wastewater treatment apparatus according to claim 1, characterized in that: the length-width ratio of the contact chamber (10) is 1-1, the width is the same as that of the flocculation chamber, the effective water depth is not less than 3.0m, the bottom surface gradient is greater than 0.1, and the hydraulic retention time is not more than 8min; the dissolved air releasing unit (11) is a TV type dissolved air releaser, and the specification is that the diameter of an interface is 25mm, two groups are arranged in two rows, and the total number is seven.
4. The ionic mine wastewater treatment apparatus according to claim 1, characterized in that: the length-width ratio of the separation chamber (13) is 2.25-3.75, the width is the same as that of the contact chamber (10), the effective water depth is not less than 2.5m, and the hydraulic retention time is 9-16 min; the slag discharge groove (15) is positioned on the water outlet side of the air flotation zone, the length is not less than 0.4m, the width is equivalent to that of the air flotation zone, the height is not less than 0.6m, and the slag discharge groove is inclined towards one end of a slag discharge pipe (17) by 1 percent of gradient; the slag discharge pipe (17) is positioned at the bottom of the slag discharge groove (15) at the outer side of the tank body; the tubular water collector (18) is positioned at the bottom of the separation chamber (13), the length of the tubular water collector is 45-55 percent of that of the separation chamber, the diameter of the tubular water collector is 250mm, and the flow velocity of effluent is 0.1-1.0 m/s; separating chamber (13) bottom of the pool sets up the sludge discharging structure, the sludge discharging structure includes six sludge bucket (19), sets up perforation sludge discharge pipe (20), connection under sludge bucket (19) sludge discharge ditch (21), the sludge discharge communicating pipe (30) and the setting of intercommunication two component separation area sludge discharge ditch (21) are in sludge discharge ditch (21) terminal sludge discharge is responsible for (22).
5. The ionic mine wastewater treatment apparatus according to claim 1, characterized in that: the water outlet gates (23) are provided with electric rising stem type gate opening and closing machines for controlling opening and closing, and each separation chamber (13) is provided with three water outlet gates (23); the length of the water collecting ditch (24) is 1.8-3.2 m, the wall thickness is 0.2-0.5 m, the height is 75-85% of the height of the pool body, and the water collecting ditch is provided with an adjustable weir gate (26); the water outlet pipe (25) is positioned at the bottom of the water collecting ditch (24).
6. The ionic mine wastewater treatment apparatus according to claim 1, wherein: the gas dissolving return pipe (27) is arranged in a water collecting channel (24) of the water outlet area, and return water is lifted to a pressure gas dissolving tank (28) through a gas dissolving water pump (31); the air in the air storage tank (29) is conveyed to the pressure dissolved air tank (28) by an air compressor unit (32).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220239269.5U CN217780804U (en) | 2022-01-28 | 2022-01-28 | Ion type mine effluent treatment plant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477353A (en) * | 2022-01-28 | 2022-05-13 | 北京东方利禾景观设计有限公司 | Ion type mine wastewater treatment device and operation method thereof |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477353A (en) * | 2022-01-28 | 2022-05-13 | 北京东方利禾景观设计有限公司 | Ion type mine wastewater treatment device and operation method thereof |
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