CN109133409B - High-hardness water hardness removal process and device - Google Patents
High-hardness water hardness removal process and device Download PDFInfo
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- CN109133409B CN109133409B CN201810926570.1A CN201810926570A CN109133409B CN 109133409 B CN109133409 B CN 109133409B CN 201810926570 A CN201810926570 A CN 201810926570A CN 109133409 B CN109133409 B CN 109133409B
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/05—Conductivity or salinity
- C02F2209/055—Hardness
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
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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
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
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Abstract
The invention discloses a high-hardness water hardness removal process and a device, wherein the high-hardness water hardness removal process mainly comprises the steps of mixing crystal nucleus-containing liquid which flows back from a high-hardness water, a sodium hydroxide solution and a calcium salt crystal slurry collecting tank with a certain volume with a mother liquor of a filter press through a tangential mixer, then feeding the mixture into a self-circulation lifting tank, fully lifting the liquid from the tangential mixer by utilizing lifting and stirring equipment, fully and uniformly mixing carbon dioxide and a flocculating agent of the liquid, reacting to generate calcium salt, gradually growing the calcium salt into settleable particles under the action of the flocculating agent, collecting the particles into crystal slurry, recycling the mother liquor to a system after the crystal slurry is subjected to filter pressing, and conveying soft water to a subsequent process for use through a soft water pipeline. A high-hardness water hardness removal device mainly comprises a tangent mixer, a self-circulation lifting tank, a calcium salt crystallization settling tank, a calcium salt crystal slurry collecting tank and a filter press.
Description
Technical Field
The invention relates to the field of water quality treatment, in particular to a process and a device for removing hardness of high-hardness water.
Technical Field
The problem that a water unit faces is always a serious system structure caused by high hardness in a high-hardness water system, and in order to reduce the influence on the water system, the hardness in the water system needs to be reduced and the water quality of the water system needs to be improved, and the traditional high-hardness water hardness removal system has the following problems: firstly, a tangent mixer is not arranged, so that the primary mixing effect of liquid is poor; secondly, the lifting equipment in the self-circulation lifting tank has no guide cylinder, so that the mixing time of the sodium hydroxide solution, the carbon dioxide, the flocculating agent and the high-hardness water is longer; thirdly, crystal nucleus backflow does not exist, so that the sedimentation effect is poor, the calcium salt recovery takes longer time, namely 5-6 hours, and the recovery rate is 90-93%; fourthly, the mother liquor after filter pressing is directly discharged out of the system and is not recycled, which has certain influence on the environment.
Disclosure of Invention
In order to overcome the defects, the invention aims to provide a hardness removal process for high-hardness water, which utilizes a tangential mixer, a self-circulation lifting tank, a calcium salt crystallization settling tank, a calcium salt crystal slurry collecting tank and filter press equipment, and utilizes carbon dioxide, sodium hydroxide, a flocculating agent and the like to form a hardness removal process so as to obtain soft water.
The invention provides a high-hardness water hardness removal process, which comprises the following specific steps:
(1) a premixing stage: the method comprises the following steps of enabling high hard water with a certain volume, a sodium hydroxide solution and calcium salt crystal slurry collecting tank to flow back to contain crystal nucleus liquid and filter press mother liquor along the tangential direction of the wall of a tangential mixer, enabling four materials to enter the tangential mixer and then automatically mixing uniformly in a self-rotating mode, and enabling the materials after mixing uniformly to enter a self-circulation lifting tank from the bottom by utilizing potential difference.
Further, the tangential mixer has a cylindrical upper part and a conical lower part, the height of the cylindrical body is 1500-.
Furthermore, four material feed pipelines are arranged in sequence along the annular direction and are respectively a high hard water tangential mixer feed pipeline, a sodium hydroxide solution tangential mixer feed pipeline, a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feed pipeline and a filter press mother liquor tangential mixer feed pipeline. The four material feeding pipelines are welded with the tangential line mixer.
Furthermore, the welding point of the feeding line of the high-hardness water tangential mixer and the wall of the tangential mixer is located at a distance of 500mm, preferably 300mm and 400mm from the uppermost end of the tangential mixer, and the tangential angle of the feeding line of the high-hardness water tangential mixer and the wall of the tangential mixer is 20-40 degrees, preferably 25-35 degrees.
Furthermore, the distance between the feeding line of the sodium hydroxide solution tangential mixer and the uppermost end of the welding point of the wall of the tangential mixer is 400-800mm, preferably 600-700mm from the uppermost end of the tangential mixer, and the included angle between the feeding line of the sodium hydroxide solution tangential mixer and the tangential line of the wall of the tangential mixer is 20-40 degrees, preferably 25-35 degrees.
Furthermore, the feeding line of the tangential mixer for the reflux liquid of the calcium salt crystal slurry collecting tank is 1100mm away from the uppermost end of the tangential mixer at the uppermost end of the welding point of the wall of the tangential mixer, preferably 1000mm away from the uppermost end of the tangential mixer, and the included angle between the feeding line of the tangential mixer and the tangential mixer is 20-40 degrees, preferably 25-35 degrees.
Furthermore, the welding point of the feeding line of the tangential mixer of the mother liquor of the filter press and the wall of the tangential mixer is 1000-1400mm, preferably 1200-1300mm away from the uppermost end of the tangential mixer, and the included angle of the feeding line of the tangential mixer and the wall of the tangential mixer is 20-40 degrees, preferably 25-35 degrees.
Furthermore, the flow of the feed pipe line of the return liquid tangential mixer of the calcium salt crystal slurry collecting tank is 0.1-0.15 time of the flow of the feed pipe line of the high hard water tangential mixer.
Further, the sodium hydroxide solution concentration ranges from 10 to 30 wt.%.
(2) Self-circulation lifting and strengthening mixing stage: and (3) sufficiently lifting the liquid from the outlet pipeline of the tangential mixer by utilizing a lifting stirring device so as to ensure that the liquid is sufficiently and uniformly mixed with the carbon dioxide from the carbon dioxide pipeline and the flocculating agent from the flocculating agent pipeline.
Further, the self-circulation lifting groove is a square groove, the length is 5000-.
Furthermore, a lifting stirring device is arranged on a bracket in the middle of the self-circulation lifting tank and is driven by a motor.
Furthermore, promote the agitated vessel outside installation draft tube, the draft tube welding is on middle support, and the draft tube is the cylinder, highly is 3600 and supplyes 6000mm, prefers 4500 and supplyes 5500mm, and the diameter is 2000 and supplyes 3000mm, prefers 2300 and supplyes 2500 mm.
Furthermore, a semicircular conical reducing port is welded and installed on the lower side of the guide cylinder to serve as a water inlet of the self-circulation lifting groove, liquid from a water outlet pipeline of the tangent mixer firstly enters the semicircular conical reducing port and then enters the guide cylinder, and further circular mixing is carried out from bottom to top under the lifting driving of the lifting stirring equipment.
Furthermore, the diameter of the lowest side of the semi-conical reducing pipe is 3000-4000mm, preferably 3300-3600mm, and the height is 300-1000mm, preferably 500-800 mm.
Furthermore, the stirring speed is increased to 40-80r/min, preferably 55-65 r/min.
Furthermore, a carbon dioxide pipeline and a flocculant pipeline are arranged at the top of the self-circulation lifting tank, and the pipelines extend to the lowest end of the guide shell.
Further, a PH on-line analyzer is arranged at an overflow port at the upper part of the self-circulation lifting tank, the PH value is controlled to be 11.5-12 by adjusting the adding amount of sodium hydroxide solution and carbon dioxide, and the carbon dioxide reacts with calcium ions to generate calcium salt under the environment.
Further, the flocculating agent is polyacrylamide with the concentration of 10-50mg/L, preferably 20-40mg/L and the flow rate of 0.5-3m3H, preferably 1.5 to 2.5m3/h。
(3) Calcium salt crystallization stage: the calcium salt-containing liquid after being intensively mixed by the self-circulation lifting tank overflows to the calcium salt crystallization settling tank from an overflow pipeline at the top of the self-circulation lifting tank, fully contacts with crystal nuclei from a feed pipeline of a reflux liquid tangential mixer of the calcium salt crystallization settling tank and a flocculating agent from a flocculating agent pipeline for growth, and gradually grows into settleable particles.
Further, the upper part of the calcium salt crystallization settling tank is a cylinder, and the height is 2500-. Set up calcium salt magma collecting vat in calcium salt crystallization settling tank bottom, calcium salt magma collecting vat is the cone, highly is 800 types of cake 1200mm, preferred 1000 types of cake 1200 mm.
Furthermore, a groove harrow device is arranged on the support of the calcium salt crystallization settling tank, the rotation speed of the groove harrow device is 5-20r/min, preferably 10-15r/min through the driving of a motor, and the settled calcium salt crystal slurry is collected to a calcium salt crystal slurry collecting tank in the rotation process of the groove harrow device.
Furthermore, a calcium salt crystal slurry outlet pipeline is arranged in the calcium salt crystal slurry tank, calcium salt crystal slurry is conveyed through a screw pump, one part of the calcium salt crystal slurry is conveyed to a feeding pipeline of a reflux liquid tangent mixer of the calcium salt crystal slurry tank, and the other part of the calcium salt crystal slurry is conveyed to a filter press.
(4) A filter pressing stage: conveying the calcium salt crystal slurry from the calcium salt crystal slurry collecting tank to a filter press by a screw pump, wherein the dry material after filter pressing is calcium salt, and the mother liquor flows back to a tangential mixer through a feeding pipeline of the tangential mixer of the mother liquor of the filter press and enters a system for recycling; the soft water is transported to the post-process for use through a soft water pipeline.
Further, the filter press is provided with a mother liquor recovery line and a soft water line.
The invention also provides a device for realizing the process, which comprises a tangential mixer, a self-circulation lifting tank, a calcium salt crystallization settling tank, a calcium salt crystal slurry collecting tank and a filter press, wherein the tangential mixer is provided with a high-hardness water tangential mixer feeding pipeline, a sodium hydroxide solution tangential mixer feeding pipeline, a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline and a filter press mother liquor tangential mixer feeding pipeline; the outlet pipeline of the tangential mixer is connected with the lower part of the self-circulation lifting tank; the overflow pipeline at the top of the self-circulation lifting tank is connected with the upper part of the calcium salt crystallization settling tank; the lower part of the calcium salt crystallization settling tank is provided with a calcium salt crystal slurry collecting tank; the calcium salt crystal slurry collecting tank is provided with a calcium salt crystal slurry outlet pipeline; the calcium salt crystal slurry outlet pipeline is respectively connected with a feeding pipeline of a reflux liquid tangent mixer of a calcium salt crystal slurry collecting tank and a filter press; the filter press is provided with a filter press mother liquor recovery pipeline and a soft water pipeline, the filter press mother liquor recovery pipeline is connected with a filter press mother liquor tangential mixer feeding pipeline, and the soft water pipeline is connected with a post-process.
The invention has the beneficial effects that:
1. through the preliminary mixed liquid of tangent line blender, improved preliminary mixed effect.
2. The self-circulation lifting tank realizes the up-and-down circulation of the mixed liquid by using the guide cylinder, and shortens the mixing time of the sodium hydroxide solution, the carbon dioxide, the flocculating agent and the high hard water.
3. And a part of crystal slurry in the calcium salt crystal slurry collecting tank is used as a crystal nucleus to flow back to the system, so that the sedimentation effect is improved.
4. The mother liquor after filter pressing is recycled to the system, thereby protecting the environment.
The implementation of the invention consumes 3-4h in the whole process of hardness removal, and the recovery rate reaches 96-99%.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the application and, together with the description, serve to explain the application and are not intended to limit the application.
FIG. 1 is a schematic diagram of a process and apparatus for removing hardness from high hardness water.
Wherein, 1, tangent mixer, 2, self-loopa promotes groove, 3, calcium salt crystallization settling tank, 4, calcium salt magma collecting vat, 5, the pressure filter, 6, high hard water tangent mixer inlet line, 7, sodium hydroxide solution tangent mixer inlet line, 8, calcium salt magma collecting vat backward flow liquid tangent mixer inlet line, 9, pressure filter mother liquor tangent mixer inlet line, 10, tangent mixer outlet line, 11, the carbon dioxide pipeline, 12, the flocculating agent pipeline, 13, promote agitated vessel, 14, the draft tube, 15, self-loopa promotes groove top overflow line, 16, the groove harrow equipment, 17, the water hose line
See in particular the examples below.
Example 1:
400m3/h high hardness water (1100-3The flow rate is fed into the tangential mixer 1 through a feeding pipeline 6 of the tangential mixer for high hard water, 20 wt.% of sodium hydroxide solution is fed into the tangential mixer 1 through a feeding pipeline 7 of the tangential mixer for sodium hydroxide solution, and the reflux of the calcium salt crystal slurry collecting tank is 40m3The flow rate of the liquid enters a tangential mixer 1 through a feeding pipeline 8 of a calcium salt crystal slurry collecting tank backflow liquid tangential mixer, a filter press mother liquid enters the tangential mixer 1 through a feeding pipeline 9 of the filter press mother liquid tangential mixer, high hard water, 20 wt.% of sodium hydroxide solution, calcium salt crystal slurry collecting tank backflow liquid and four kinds of liquid of the filter press mother liquid enter the tangential mixer 1 in a tangential mode, the liquid is automatically and uniformly mixed in a self-rotating mode, the uniformly mixed liquid enters a semi-conical reducing cylinder below a flow guide cylinder 14 of a self-circulation lifting tank 2 from an outlet pipeline 10 of the tangential mixer by utilizing potential difference, meanwhile, carbon dioxide is conveyed to the lowest part of the flow guide cylinder 14 through a carbon dioxide pipeline 11, the PH value is controlled to be 11.5 by adjusting the adding amount of the sodium hydroxide solution and the carbon dioxide, and 10mg/L polyacrylamide flocculant solution is 0.5m3The flow of the solution/h is conveyed to the lowest part of a guide cylinder 14 through a flocculating agent pipeline 12, the liquid from an outlet pipeline 10 of a tangential mixer and the carbon dioxide of a carbon dioxide pipeline 11 are further self-circularly mixed along the guide cylinder 14 from bottom to top to generate calcium salt under the action of lifting and stirring of a lifting and stirring device 13 (the lifting and stirring rotating speed is 40r/min), the calcium salt-containing liquid overflows to a calcium salt crystallization settling tank 3 from an overflow pipeline 15 at the top of the self-circulating lifting tank, crystal nuclei from a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline 8 are fully contacted with the calcium salt solution from a self-circulating lifting tank 2 and the polyacrylamide solution from the flocculating agent pipeline 12 in the calcium salt crystallization settling tank 3 to gradually grow into settleable particles, and under the rotating action of a rake device 16 in the calcium salt crystallization settling tank 3 (the rake device rotating speed is 5r/min), gradually collecting the precipitated calcium salt crystal slurry into a calcium salt crystal slurry collecting tank 4, conveying the calcium salt crystal slurry from the calcium salt crystal slurry collecting tank 4 to a filter press 5 by a screw pump, and pressingThe filtered dry material is calcium salt, and the mother liquor flows back to the tangential mixer through a feeding pipeline 9 of the tangential mixer of the mother liquor of the filter press and enters a system for recycling; the soft water is supplied to the post-process through a soft water line 17. After the hardness of the alloy is removed by the process, the analysis result is as follows:
remarking: the hardness removing time is the interval time between water inlet and water outlet sampling.
Example 2:
400m3The/h high-hardness water (1100-1500ppm) treatment device comprises a tangential mixer 1, a self-circulation lifting tank 2, a calcium salt crystallization settling tank 3, a calcium salt crystal slurry collecting tank 4, a filter press 5, a high-hardness water tangential mixer feeding pipeline 6, a sodium hydroxide solution tangential mixer feeding pipeline 7, a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline 8, a filter press mother liquor tangential mixer feeding pipeline 9, a tangential mixer outlet pipeline 10, a carbon dioxide pipeline 11, a flocculating agent pipeline 12, a lifting stirring device 13, a guide cylinder 14, a self-circulation lifting tank top overflow pipeline 15, a tank rake device 16 and a water softening pipeline 17.
The tangential mixer 1 is provided with a high hard water tangential mixer feeding pipeline 6, a sodium hydroxide solution tangential mixer feeding pipeline 7, a calcium salt crystal slurry collecting tank reflux liquid tangential mixer feeding pipeline 8 and a filter press mother liquor tangential mixer feeding pipeline 9; the outlet pipeline 10 of the tangent mixer is connected with the lower part of the self-circulation lifting tank 2; the overflow pipeline 15 at the top of the self-circulation lifting tank is connected with the upper part of the calcium salt crystallization settling tank 3; the lower part of the calcium salt crystallization settling tank 3 is provided with a calcium salt crystal slurry collecting tank 4; the calcium salt crystal slurry collecting tank 4 is provided with a calcium salt crystal slurry outlet pipeline; the calcium salt crystal slurry outlet pipeline is respectively connected with a feeding pipeline 8 of a reflux liquid tangent mixer of a calcium salt crystal slurry collecting tank and the filter press 5; the filter press 5 is provided with a filter press mother liquor recovery pipeline and a soft water pipeline 17, the filter press mother liquor outlet pipeline is connected with a filter press mother liquor tangential mixer feeding pipeline 9, and the soft water pipeline 17 is connected with a post-process.
The upper part of the tangent mixer 1 is a cylinder, the lower part of the tangent mixer is a cone, the height of the cylinder is 1500mm, and the height of the cone is 3000 mm; high hard water tangent mixer feed line 6 and tangent mixer 1 wall welding point the top is 100mm from tangent mixer 1 the top, be 20 with tangent mixer 1 wall tangent angle, sodium hydroxide solution tangent mixer feed line 7 and tangent mixer 1 wall welding point the top is 400mm from tangent mixer 1 the top, be 20 with tangent mixer 1 wall tangent included angle, calcium salt magma collecting vat backflow liquid tangent mixer feed line 8 and tangent mixer 1 wall welding point the top is 700mm from tangent mixer 1 the top, be 20 with tangent mixer wall tangent included angle, pressure filter mother liquor tangent mixer feed line 9 and tangent mixer 1 wall welding point the top is 1000mm from tangent mixer 1 the top, be 20 with tangent mixer 1 wall tangent included angle.
From circulation lifting groove 2 for square groove, length is 5000mm, the width is 5000mm, highly be 5000mm, install promotion agitated vessel 13 in the middle of self-circulation lifting groove 2 on the support, promote agitated vessel 13 through motor drive, at promotion agitated vessel 13 outside installation draft tube 14, draft tube 14 welds on the middle support, draft tube 14 is the cylinder, highly be 3600mm, the diameter is 2000mm, at 14 downside welding installations semicircle toper reducing of draft tube as self-circulation lifting groove 2 water inlet, the downside diameter of semicircle toper reducing is 3000mm, highly be 300 mm. A carbon dioxide pipeline 11 and a flocculating agent pipeline 12 are arranged at the top of the self-circulation lifting tank 2, and the pipelines extend to the lowest end of a guide shell 14; a PH on-line analyzer is installed on the overflow line 15 at the top of the self-circulation lift tank.
3 upper portions of calcium salt crystallization subsider are the cylinder, highly are 2500mm, set up calcium salt crystal thick liquid collecting vat 4 in 3 bottoms of calcium salt crystallization subsider, and calcium salt crystal thick liquid collecting vat 4 is the cone, highly is 800mm, and mounting groove harrow equipment 16 promotes groove harrow equipment 16 through motor drive in calcium salt crystallization subsider 3. And a calcium salt crystal slurry outlet pipeline is arranged on the calcium salt crystal slurry collecting tank 4. The filter press 5 is provided with a mother liquor recovery line and a soft water line 17.
Example 3:
600m3H high hardness water (11)00-1500ppm) treatment process, high hardness water is 600m3The flow rate is fed into a tangential mixer 1 through a feeding pipeline 6 of the tangential mixer for high hard water, 30 wt.% of sodium hydroxide solution is fed into the tangential mixer 1 through a feeding pipeline 7 of the tangential mixer for sodium hydroxide solution, and the reflux of the calcium salt crystal slurry collecting tank is 60m3The flow rate of the liquid enters a tangential mixer 1 through a feeding pipeline 8 of a calcium salt crystal slurry collecting tank backflow liquid tangential mixer, the filter press mother liquid enters the tangential mixer 1 through the feeding pipeline of the filter press mother liquid tangential mixer, high hard water, 30 wt.% of sodium hydroxide solution, calcium salt crystal slurry collecting tank backflow liquid and four kinds of liquid of the filter press mother liquid enter the tangential mixer 1 in a tangential mode, the liquid is automatically and uniformly mixed in a self-rotating mode, the uniformly mixed liquid enters a semi-conical reducing cylinder below a flow guide cylinder 14 of a self-circulation lifting tank 2 from an outlet pipeline 10 of the tangential mixer by utilizing potential difference, meanwhile, carbon dioxide is conveyed to the lowest part of the flow guide cylinder 14 through a carbon dioxide pipeline 11, the PH value is controlled to be 11.5 by adjusting the adding amount of the sodium hydroxide solution and the carbon dioxide, 50mg/L polyacrylamide flocculant solution is 3m3The flow of the solution is conveyed to the lowest part of a guide shell 14 through a flocculating agent pipeline 12, the liquid from an outlet pipeline 10 of a tangential mixer, the carbon dioxide of a carbon dioxide pipeline 11 and the polyacrylamide solution of the flocculating agent pipeline 12 are further mixed from bottom to top along the guide shell 14 under the action of lifting and stirring of a lifting and stirring device 13 (the lifting and stirring speed is 80r/min) to produce calcium salt, the mixed liquid overflows to a calcium salt crystal settling tank 3 from an overflow pipeline 15 at the top of the self-circulation lifting tank, crystal nuclei from a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline 8 are fully contacted with the calcium salt solution from a self-circulation lifting tank 2 and the polyacrylamide solution from the flocculating agent pipeline 12 in the calcium salt crystal settling tank 3 to grow into settleable particles gradually, and under the action of rotation of a tank rake device 16 in the calcium salt crystal settling tank 3 (the rake device rotation speed is 20r/min), gradually collecting the precipitated calcium salt crystal slurry into a calcium salt crystal slurry collecting tank 4, conveying the calcium salt crystal slurry from the calcium salt crystal slurry collecting tank 4 to a filter press 5 by a screw pump, wherein the dry material after filter pressing is calcium salt, and returning the mother liquor to a tangent mixer through a feeding pipeline 9 of a mother liquor tangent mixer of the filter press, and then recycling the mother liquor in a system; soft waterAnd then transported to a post-process for use through a soft water line 17. After the hardness of the alloy is removed by the process, the analysis result is as follows:
remarking: the hardness removing time is the interval time between water inlet and water outlet sampling.
Example 4:
600m3The/h high-hardness water (1100-1500ppm) treatment device comprises a tangential mixer 1, a self-circulation lifting tank 2, a calcium salt crystallization settling tank 3, a calcium salt crystal slurry collecting tank 4, a filter press 5, a high-hardness water tangential mixer feeding pipeline 6, a sodium hydroxide solution tangential mixer feeding pipeline 7, a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline 8, a filter press mother liquor tangential mixer feeding pipeline 9, a tangential mixer outlet pipeline 10, a carbon dioxide pipeline 11, a flocculating agent pipeline 12, a lifting stirring device 13, a guide cylinder 14, a self-circulation lifting tank top overflow pipeline 15, a tank rake device 16 and a water softening pipeline 17.
The tangential mixer 1 is provided with a high hard water tangential mixer feeding pipeline 6, a sodium hydroxide solution tangential mixer feeding pipeline 7, a calcium salt crystal slurry collecting tank reflux liquid tangential mixer feeding pipeline 8 and a filter press mother liquor tangential mixer feeding pipeline 9; the outlet pipeline 10 of the tangent mixer is connected with the lower part of the self-circulation lifting tank 2; the overflow pipeline 15 at the top of the self-circulation lifting tank is connected with the upper part of the calcium salt crystallization settling tank 3; the lower part of the calcium salt crystallization settling tank 3 is provided with a calcium salt crystal slurry collecting tank 4; the calcium salt crystal slurry collecting tank 4 is provided with a calcium salt crystal slurry outlet pipeline; the calcium salt crystal slurry outlet pipeline is respectively connected with a feeding pipeline 8 of a reflux liquid tangent mixer of a calcium salt crystal slurry collecting tank and the filter press 5; the filter press 5 is provided with a filter press mother liquor recovery pipeline and a soft water pipeline 17, the filter press mother liquor recovery pipeline is connected with a filter press mother liquor tangential mixer feeding pipeline 9, and the soft water pipeline 17 is connected with a post-process.
The upper part of the tangent mixer 1 is a cylinder, the lower part of the tangent mixer is a cone, the height of the cylinder is 2000mm, and the height of the cone is 4000 mm; high hard water tangent mixer feed line 6 and tangent mixer 1 wall welding point the top is 500mm from tangent mixer 1 the top, be 40 with tangent mixer 1 wall tangent angle, sodium hydroxide solution tangent mixer feed line 7 and tangent mixer 1 wall welding point the top is 800mm from tangent mixer 1 the top, be 40 with tangent mixer 1 wall tangent included angle, calcium salt magma collecting vat backflow liquid tangent mixer feed line 8 and tangent mixer 1 wall welding point the top is 1100mm from tangent mixer 1 the top, be 40 with tangent mixer wall tangent included angle, pressure filter mother liquor tangent mixer feed line 9 and tangent mixer 1 wall welding point the top is 1400mm from tangent mixer 1 the top, be 40 with tangent mixer 1 wall tangent included angle.
From circulation lift groove 2 for square groove, length is 7000mm, the width is 7000mm, highly be 8000mm, install lift agitated vessel 13 in the middle of self-circulation lift groove 2 on the support, promote agitated vessel 13 through motor drive, at lift agitated vessel 13 outside installation draft tube 14, draft tube 14 welds on middle support, draft tube 14 is the cylinder, highly be 6000mm, the diameter is 3000mm, at 14 downside welded mounting semicircle toper reducing of draft tube as self-circulation lift groove 2 water inlet, the downside diameter of semicircle toper reducing is 4000mm, highly be 1000 mm. A carbon dioxide pipeline 11 and a flocculating agent pipeline 12 are arranged at the top of the self-circulation lifting tank 2, and the pipelines extend to the lowest end of a guide shell 14; a PH on-line analyzer is installed on the overflow line 15 at the top of the self-circulation lift tank.
3 upper portions of calcium salt crystallization subsider are the cylinder, highly are 3000mm, set up calcium salt crystal thick liquid collecting vat 4 in 3 bottoms of calcium salt crystallization subsider, and calcium salt crystal thick liquid collecting vat 4 is the cone, highly is 1200mm, mounting groove harrow equipment 16 in calcium salt crystallization subsider 3, promote groove harrow equipment 16 through motor drive. And a calcium salt crystal slurry outlet pipeline is arranged on the calcium salt crystal slurry collecting tank 4. The filter press 5 is provided with a mother liquor recovery line and a soft water line 17.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (1)
1. The process for removing hardness of high-hardness water is characterized in that soft water is recovered by utilizing a tangential mixer, a self-circulation lifting tank, a calcium salt crystallization settling tank, a calcium salt crystal slurry collecting tank and filter press equipment, and the process comprises the following steps:
(1) a premixing stage: the method comprises the following steps of (1) enabling high-hardness water, a sodium hydroxide solution and calcium salt crystal slurry collecting tank with a certain volume to flow back to a crystal nucleus-containing liquid and a filter press mother liquor along the tangential direction of the wall of a tangential mixer, enabling four materials to enter the tangential mixer and then be automatically and uniformly mixed in a self-rotating mode, and enabling the uniformly mixed materials to enter a self-circulation lifting tank from the bottom by utilizing a potential difference;
(2) self-circulation lifting and strengthening mixing stage: fully lifting the liquid from the outlet pipeline of the tangential mixer by utilizing lifting and stirring equipment, and fully and uniformly mixing the liquid with the carbon dioxide from the carbon dioxide pipeline and the flocculant from the flocculant pipeline to form calcium salt-containing liquid;
(3) the calcium salt-containing liquid from the self-circulation lifting tank overflows to a calcium salt crystallization settling tank from an overflow pipeline at the top of the self-circulation lifting tank, gradually grows into settleable particles under the action of a flocculating agent, and enters a calcium salt crystal slurry collecting tank;
(4) a filter pressing stage: conveying the calcium salt crystal slurry from the calcium salt crystal slurry collecting tank to a filter press by a screw pump, wherein the dry material after filter pressing is calcium salt, and the mother liquor flows back to a tangential mixer through a feeding pipeline of the tangential mixer of the mother liquor of the filter press and enters a system for recycling; soft water is conveyed to a post-process for use through a soft water pipeline;
the tangential mixer is provided with a high-hardness water tangential mixer feeding pipeline, a sodium hydroxide solution tangential mixer feeding pipeline, a calcium salt crystal slurry collecting tank backflow liquid tangential mixer feeding pipeline and a filter press mother liquid tangential mixer feeding pipeline; the outlet pipeline of the tangent mixer is connected with the lower part of the self-circulation lifting tank; the overflow pipeline at the top of the self-circulation lifting tank is connected with the upper part of the calcium salt crystallization settling tank; the lower part of the calcium salt crystallization settling tank is provided with a calcium salt crystal slurry collecting tank; the calcium salt crystal slurry collecting tank is provided with a calcium salt crystal slurry outlet pipeline; the calcium salt crystal slurry outlet pipeline is respectively connected with a feeding pipeline of a reflux liquid tangent mixer of the calcium salt crystal slurry collecting tank and a filter press; the filter press is provided with a filter press mother liquor recovery pipeline and a soft water pipeline, the filter press mother liquor recovery pipeline is connected with a filter press mother liquor tangential mixer feeding pipeline, and the soft water pipeline is connected with a post-process;
the line flow of the feeding pipe of the backflow liquid tangential mixer of the calcium salt crystal slurry collecting tank is 0.1-0.15 times of the line flow of the feeding pipe of the high-hardness water tangential mixer, the concentration range of sodium hydroxide solution is 10-30 wt%, the lifting and stirring rotating speed of the self-circulation lifting tank is 40-80r/min, the pH value of an overflow pipeline at the top of the self-circulation lifting tank is controlled to be 11.5-12, the concentration of the flocculating agent is 10-50mg/L, and the flow of the flocculating agent is 0.5-3m3The rotating speed of the raking equipment of the calcium salt crystallization settling tank is 5-20 r/min;
the distance between the feeding pipeline of the high-hardness water tangential mixer and the uppermost end of the welding point of the wall of the tangential mixer is 500mm away from the uppermost end of the tangential mixer, and the tangential angle of the feeding pipeline of the high-hardness water tangential mixer and the wall of the tangential mixer is 20-40 degrees; the distance between the feeding pipeline of the sodium hydroxide solution tangent mixer and the uppermost end of the welding point of the wall of the tangent mixer is 400-800mm away from the uppermost end of the tangent mixer, and the included angle between the feeding pipeline of the sodium hydroxide solution tangent mixer and the tangent line of the wall of the tangent mixer is 20-40 degrees; the distance between the feeding pipeline of the calcium salt crystal slurry collecting tank reflux liquid tangent mixer and the uppermost end of the welding point of the wall of the tangent mixer is 700-1100mm away from the uppermost end of the tangent mixer, and the included angle between the feeding pipeline of the calcium salt crystal slurry collecting tank reflux liquid tangent mixer and the tangent mixer wall is 20-40 degrees; the distance between the uppermost end of the welding point of the feeding pipeline of the mother liquor tangential mixer and the wall of the tangential mixer of the filter press is 1000-1400mm from the uppermost end of the tangential mixer, and the included angle between the feeding pipeline of the mother liquor tangential mixer and the tangential mixer wall is 20-40 degrees;
a guide cylinder is arranged on the outer side of the self-circulation lifting groove lifting stirring equipment, the guide cylinder is welded on the middle support, the guide cylinder is a cylinder, the height is 3600-6000mm, and the diameter is 2000-3000 mm; the lower side of the guide cylinder is welded with a semi-conical reducing cylinder, the diameter of the lowermost side of the semi-conical reducing cylinder is 3000-4000mm, and the height of the lowermost side is
300-1000mm。
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102134129A (en) * | 2010-01-25 | 2011-07-27 | 白连福 | Softening process for industrial raw water |
| CN202465354U (en) * | 2012-03-21 | 2012-10-03 | 中冶赛迪工程技术股份有限公司 | Coagulation device |
| CN104496041A (en) * | 2014-12-22 | 2015-04-08 | 内蒙古久科康瑞环保科技有限公司 | Softening device for treating high-hardness, low-alkalinity salt-containing wastewater |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102134129A (en) * | 2010-01-25 | 2011-07-27 | 白连福 | Softening process for industrial raw water |
| CN202465354U (en) * | 2012-03-21 | 2012-10-03 | 中冶赛迪工程技术股份有限公司 | Coagulation device |
| CN104496041A (en) * | 2014-12-22 | 2015-04-08 | 内蒙古久科康瑞环保科技有限公司 | Softening device for treating high-hardness, low-alkalinity salt-containing wastewater |
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