CN214571316U - Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method - Google Patents
Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method Download PDFInfo
- Publication number
- CN214571316U CN214571316U CN202022896656.XU CN202022896656U CN214571316U CN 214571316 U CN214571316 U CN 214571316U CN 202022896656 U CN202022896656 U CN 202022896656U CN 214571316 U CN214571316 U CN 214571316U
- Authority
- CN
- China
- Prior art keywords
- softening
- unit
- water
- crystallization
- reverse osmosis
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 167
- 238000002425 crystallisation Methods 0.000 title claims abstract description 78
- 230000008025 crystallization Effects 0.000 title claims abstract description 78
- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000005469 granulation Methods 0.000 title claims abstract description 32
- 230000003179 granulation Effects 0.000 title claims abstract description 32
- 230000008878 coupling Effects 0.000 title claims abstract description 28
- 238000010168 coupling process Methods 0.000 title claims abstract description 28
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 28
- 239000012528 membrane Substances 0.000 title claims description 29
- 150000003839 salts Chemical group 0.000 claims abstract description 49
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 42
- 238000005243 fluidization Methods 0.000 claims abstract description 37
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229920005989 resin Polymers 0.000 claims abstract description 24
- 239000011347 resin Substances 0.000 claims abstract description 24
- 230000006698 induction Effects 0.000 claims abstract description 22
- 238000001728 nano-filtration Methods 0.000 claims description 42
- 239000013078 crystal Substances 0.000 claims description 36
- 150000002500 ions Chemical class 0.000 claims description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 24
- 239000002245 particle Substances 0.000 claims description 23
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 18
- 238000000926 separation method Methods 0.000 claims description 18
- 239000003814 drug Substances 0.000 claims description 16
- 239000012452 mother liquor Substances 0.000 claims description 16
- 238000000108 ultra-filtration Methods 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 230000008014 freezing Effects 0.000 claims description 8
- 238000007710 freezing Methods 0.000 claims description 8
- 238000005342 ion exchange Methods 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- 229910002651 NO3 Inorganic materials 0.000 claims description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 4
- 239000002455 scale inhibitor Substances 0.000 claims description 4
- 238000004062 sedimentation Methods 0.000 claims description 4
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 3
- 239000003638 chemical reducing agent Substances 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 3
- 238000011033 desalting Methods 0.000 claims description 2
- 230000003472 neutralizing effect Effects 0.000 claims description 2
- 229920001429 chelating resin Polymers 0.000 claims 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 8
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 8
- 238000009434 installation Methods 0.000 abstract description 5
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 4
- 239000011780 sodium chloride Substances 0.000 abstract description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 4
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 abstract description 3
- 238000007781 pre-processing Methods 0.000 abstract description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 18
- 230000008569 process Effects 0.000 description 10
- 229910000019 calcium carbonate Inorganic materials 0.000 description 9
- 235000010216 calcium carbonate Nutrition 0.000 description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 8
- 239000003513 alkali Substances 0.000 description 8
- 239000011575 calcium Substances 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 5
- 229910001425 magnesium ion Inorganic materials 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 229910021532 Calcite Inorganic materials 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 239000006004 Quartz sand Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000002223 garnet Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 230000033558 biomineral tissue development Effects 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 239000013522 chelant Substances 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- 239000011435 rock Substances 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000007726 management method Methods 0.000 description 2
- 239000013081 microcrystal Substances 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
Images
Abstract
The utility model provides a crystallization granulation softens zero discharge system that hard mine water of negative water was handled to coupling embrane method, including consecutive concentrated preprocessing unit, circulation fluidization induction crystallization softening unit, resin softening unit, the concentrated unit of second grade, ammonia nitrogen get rid of unit, COD get rid of unit and receive and strain the salt unit. The utility model discloses a to circulate induced crystallization softening installation of fluidization and reverse osmosis unit ingenious combination, use one-level reverse osmosis unit earlier and make the concentrated decrement of the hard mine water of burden, recycle circulation fluidization induced crystallization softening installation and get rid of calcium ion, then get rid of ammonia nitrogen and COD in the mine aquatic, receive through the two-stage and strain the salt and obtain sodium chloride crystallization and sodium sulfate crystallization to the miscellaneous salt that will obtain dissolves back, this method can effectively reduce the running cost, improves the treatment effeciency.
Description
Technical Field
The utility model relates to a water treatment technical field, concretely relates to crystallization granulation softens zero discharge system that hard mine water of negative was handled to coupling embrane method.
Background
The high-salinity mine water generally refers to mine water with the salt content of more than 1000mg/L, and the water quality is neutral or slightly alkaline. With the optimization of coal production and development layout, the national energy supply strategy moves to the west, so that the proportion of mine water with high mineralization of coal mines is greatly increased. According to statistics, about 30 percent of mine water in China is high-salinity mine water, and the proportion of the high-salinity mine water in the northwest area exceeds 50 percent, so that the problem that the development of the northwest coal mine is the most prominent problem is solved. Because the mine water with high mineralization is harmful, the mine water is lack of receiving water, and the drainage can cause soil and water loss, salinization, vegetation withering and the like on the earth surface. In the last two years, the inner Mongolia autonomous region is fully provided with a bivalve water guard war, and ecological civilization construction such as water quality improvement of a real drainage basin, urban environment protection, mining area environment treatment and restoration, ecological construction, pollution prevention and control, forest planting in spring, grassland fire prevention, mine water zero discharge, strong brine resource utilization and the like is firmly achieved. In 2018, the original drainage port of the Wulanmulun basin where the Shendong group mining area is located is closed, zero waste water discharge is realized, and the water quality of the centralized drinking water source above cities and towns reaches or is superior to that of the III-class embodiment and is stabilized at 100%. However, the existing mine water treatment plants of Shendong group still operate according to the design of the emission standard of pollutants in coal industry, the emission limit value of the original standard is 100 times of the emission limit value required at present to the maximum extent, the risk of environmental penalty is faced, and the mine water zero emission treatment in mine areas under the flag becomes a necessary route.
The implementation of the membrane method zero-emission technology has higher requirements on the front-end hardness removal pretreatment, and the hardness, suspended matters and SiO of mine water after the underground clarification treatment of the mine2、Fe、HCO3 -The concentration of (a) is still high, and therefore the softening pretreatment needs to be enhanced. The softening effect directly influences scaling and service life of the membrane material, and reasonable pretreatment process and standard operation management are the key for stable implementation of the mine water zero-discharge technology. The main softening pretreatment in the zero-emission system mainly adopts two schemes of dosing hardness removal and ion exchange: (1) adding double alkali for softening: the lime (or caustic soda-sodium carbonate) softening method is widely applied to the softening treatment of wastewater, the process has the advantages of good stability and reliability, the total hardness after two-stage chemical softening treatment is reduced to less than 100mg/L, the process has the disadvantages of large consumption of chemicals, generation of a large amount of sludge in the softening process, high medicament cost and sludge treatment cost, and high HCO (hydrogen chloride oxide) treatment cost3 -In the case of mine water with high concentration, decarburization treatment is also required. In the coal-fired power plant desulfurization wastewater zero discharge system, the double-alkali dosing softening process is improved, and calcium and magnesium ions are separated by using a tubular microfiltration or ultrafiltration membrane between double-alkali dosing reactors and using the critical pH value and the oxidation-reduction potential of calcium carbonate and magnesium hydroxide precipitation, so that the improvement on calcium and magnesium ions can be realizedThe pretreatment efficiency is improved, the softening time of the medicament is shortened, the dosage is reduced to a certain extent, but a large amount of alkaline medicament is still required to be used and the risk of membrane blockage is accompanied. (2) The ion exchange softening process is stable and reliable, and the hardness of the effluent after ion exchange can be reduced to be within 10 mg/L. However, the problems of excessive equipment investment, excessive regenerated wastewater yield and the like exist for the inflow water with high hardness. Therefore, in practical applications, ion exchange softening after chemical softening is usually considered to further reduce the hardness of the wastewater so as to ensure stable operation of subsequent systems. The small amount of regeneration waste water that can be returned to the original chemical softening system ensures that the system does not produce new contaminants. Compared with the desulfurization wastewater of a coal-fired power plant with wide application of a zero discharge system, the highly mineralized mine water has the advantages of unobvious concentration of calcium and magnesium ions and HCO3 -The characteristics of high concentration and low COD concentration require urgent development of softening pretreatment technology suitable for the water quality characteristics of mine water and the treatment requirement of large water amount, and aims to reduce the medicament cost, improve the operation stability of a mine water zero-discharge system, save the operation cost and reduce the operation and maintenance management difficulty.
Disclosure of Invention
The utility model relates to a solve the problem that the hard mine water treatment method working costs of current burden is high, poor stability, provide a crystallization granulation softening coupling embrane method and handle the zero discharge system of the hard mine water of burden, including consecutive concentrated preprocessing unit, circulation fluidization induction crystallization softening unit, resin softening unit, the concentrated unit of second grade, ammonia nitrogen removal unit, COD get rid of unit and receive and divide the salt unit. The utility model discloses a to circulate induced crystallization softening installation of fluidization and reverse osmosis unit ingenious combination, use one-level reverse osmosis unit earlier and make the concentrated decrement of the hard mine water of burden, recycle circulation fluidization induced crystallization softening installation and get rid of calcium ion, then get rid of ammonia nitrogen and COD in the mine aquatic, receive through the two-stage and strain the salt and obtain sodium chloride crystallization and sodium sulfate crystallization to the miscellaneous salt that will obtain dissolves back, this method can effectively reduce the running cost, improves the treatment effeciency.
The utility model provides a zero discharge system for treating negative hard mine water by a crystallization granulation softening coupling membrane method, which comprises a concentration pretreatment unit, a circulating fluidization induced crystallization softening unit, a resin softening unit, a second-stage concentration unit, an ammonia nitrogen removal unit, a COD removal unit and a nanofiltration salt separation unit which are connected in sequence;
the concentration pretreatment unit is used for adjusting and filtering negative hard mine water and performing primary concentration pretreatment, the circulating fluidization induction crystallization softening unit is used for softening and removing hardness through induction crystallization, the resin softening unit is used for further removing hardness through ion exchange softening, the secondary concentration unit is used for performing secondary concentration, the ammonia nitrogen removal unit is used for removing ammonia nitrogen, the COD removal unit is used for removing COD through an ozone-activated carbon filtration process, and the nanofiltration salt separation unit is used for separating monovalent ions and divalent ions to obtain monovalent ion crystal finished products and divalent ion crystal finished products;
the water inlet of the circulating fluidization induced crystallization softening unit is connected with the concentrated water outlet of the concentration pretreatment unit, and the water inlet of the ammonia nitrogen removal unit is connected with the concentrated water outlet of the second-stage concentration unit.
The utility model discloses a crystallization granulation softening coupling membrane method handles zero discharge system of burden hard mine water, as preferred mode, the concentration pretreatment unit includes consecutive raw water equalizing basin, one-level V type filtering pond, one-level ultrafiltration device and one-level reverse osmosis unit;
the circulating fluidization induction crystallization softening unit comprises a circulating fluidization induction crystallization softening system and an adjusting tank which are sequentially connected, and a water inlet of the circulating fluidization induction crystallization softening system is connected with a concentrated water outlet of the primary ultrafiltration device;
the resin softening unit comprises a secondary ultrafiltration device and a resin softening device which are connected in sequence;
the secondary concentration unit comprises a decarbonizer and a secondary reverse osmosis device which are connected in sequence;
the ammonia nitrogen removal unit comprises a first safety filter and an ammonia nitrogen reaction tank which are sequentially connected;
the COD removal unit comprises a high-density sedimentation tank, an ozone reaction tank, an activated carbon filter, a three-stage ultrafiltration device and a second security filter which are sequentially connected;
the nanofiltration salt separation unit comprises a first-stage nanofiltration device connected with an outlet of a second security filter, a nanofiltration water production tank sequentially connected with a water production outlet of the first-stage nanofiltration device, a second-stage nanofiltration device, a third-stage reverse osmosis device connected with a water production outlet of the second-stage nanofiltration device, a first MVR evaporator, a first MVR crystallizer, a first pure salt dryer sequentially connected with a concentrated water outlet of the third-stage reverse osmosis device, a monovalent ion terminal mother liquor tank connected with a mother liquor outlet of the first MVR crystallizer, a concentrated water tank sequentially connected with a concentrated water outlet of the first-stage nanofiltration device, a second MVR evaporator, a nitrate dissolving tank, a second MVR crystallizer and a second pure salt dryer.
A crystallization granulation softens zero discharge system that hard mine water of negative water was handled to coupling embrane method, as preferred mode, receive and strain salt unit and still include freezing crystallizer, third pure salt desicator that links to each other in proper order with the mother liquor export of second MVR crystallizer, with freezing crystallizer mother liquor export continuous divalent ion terminal mother liquor jar.
A crystallization granulation softens zero discharge system that coupling embrane method was handled hard mine water of burden, as preferred mode, the export of third pure salt desicator links to each other with one-level nanofiltration device's water inlet.
A crystallization granulation softens zero discharge system that coupling embrane method handled burden hard mine water, as preferred mode, circulation fluidization induction crystallization softens the system and includes the vertical hollow circular cylinder barrel of establishhing both ends confined, set up respectively at the softening system water inlet of barrel, add the medicine mouth, set up throw with mouthful and set up throw with the crystalline particles at the barrel top and throw with the delivery port of mouthful relative one side at the barrel top, from the bottom to the top has set gradually water distribution district, cloth medicine district, granulation district and clear water district in the barrel.
A crystallization granulation softens zero discharge system that coupling embrane method was handled hard mine water of burden, as preferred mode, alkali medicament is following one or several kinds: lime, sodium hydroxide, sodium carbonate and sodium metaaluminate; adjusting the pH value of the primary concentrated mine water to be more than 9; the seed crystal feeding pipe is filled with proper 0.1-1 mm seed crystal particles with the size of 0.1-1 mm, and the seed crystal particles are one or more of the following particles: calcium carbonate ore, quartz sand, garnet, calcite, veined rock.
The utility model discloses a zero discharge system of hard mine water of negative is handled to crystallization granulation softening coupling embrane method, as preferred mode, the first order reverse osmosis unit uses SWRO membrane (sea water desalination reverse osmosis membrane), and second grade reverse osmosis unit and tertiary reverse osmosis unit use the RO membrane;
the first-stage reverse osmosis device and the second-stage reverse osmosis device are both a first-stage section and a second-stage section;
and an emergency discharge port is arranged at a concentrated water outlet of the secondary reverse osmosis device.
A crystallization granulation softens zero discharge system that coupling embrane method was handled hard mine water of burden, as preferred mode, still include demineralized water tank, lime device, FeCl3Device, PAM device, MgO device, soda device, H2SO4The device comprises an HCl device, an NaOH device, a scale inhibitor device and a reducing agent device.
A crystallization granulation softens zero discharge system that coupling embrane method was handled burden and is mineed water hard, as preferred mode, still include cleaning system, add medicine storage system, compressed air system, waste water neutralization system, electrical system and instrument control system.
A crystallization granulation softens zero discharge system that coupling embrane method handled hard mine water of burden, as preferred mode, resin softening installation is chelate resin ion exchanger.
And an emergency discharge port is arranged at a concentrated water outlet of the secondary reverse osmosis device.
The main body of the circulating fluidization induced crystallization softening system is a fluidized bed crystallization separator, which comprises: cartridge case, barrel, draft tube, back flow etc. The barrel is a vertically-arranged hollow cylinder with two closed ends, a water distribution area, a medicine distribution area, a granulation area and a clear water area are sequentially arranged in the barrel from the bottom to the top, a water inlet and a medicine feeding opening are formed in the lower portion of the barrel, and a water outlet and a seed crystal feeding opening are formed in the upper portion of the barrel. Filling proper 0.1-1 mm seed crystal particles into the induced crystallization device, wherein the seed crystal particles are any one or combination of the following: calcium carbonate ore, quartz sand, garnet, calcite, veined rock, and the like. Putting crystal nuclei as a trigger through the seed crystal putting port, and forming the fluidization area in the guide shell; adding an alkali agent through the dosing port to enable the mine water with high mineralization degree to be mixed with the alkali agent and react to form calcium carbonate precipitate, enabling crystal nuclei to grow into crystal seeds through calcium carbonate micro crystals generated by adsorption reaction when the mine water flows through the fluidized zone, and continuously attaching the calcium carbonate micro crystals to the surface of the crystal seeds to form multilayer crystal particles; the wastewater continuously enters the separation area upwards, the heavier particles settle down in the static settling area, the mixture of the lighter particles and water continuously rises and forms a sludge layer on the upper part of the separation area, and the clear water after calcium removal gradually enters the clear water area and is discharged through the water outlet. The implementation mode is as follows: the concentrated water of the first-stage reverse osmosis device is used as the inlet water of the induced crystallization device (circulating fluidized bed reactor), and the medicament tank is added with alkali medicament (lime, sodium hydroxide, sodium carbonate, sodium metaaluminate and the like, preferably sodium hydroxide) for fully dissolving to adjust the pH value of the inlet water to be more than 9. And (2) filling proper 0.1-1 mm seed crystal particles (the seed crystal can be calcium carbonate ore, quartz sand, garnet, calcite, veined stone and other minerals) into a seed crystal feeding pipe, pumping the inlet water upwards to maintain the fluidization state flow rate of the particles to be 40-90m/h through the particle bed, preferably, the initial start-up (activation period) flow rate is 60m/h, and increasing the flow rate to 70-80m/h after the operation is stable. The particles act as crystallization sites and the high surface area of the small particles effectively reduces the energy required for precipitation. As the crystals grow and become heavier, they gradually move towards the bottom of the bed layer without interrupting the operation of the reactor, and the crystals with the size of 0.5-2.0 mm are discharged from the bottom. The circulating fluidization induced crystallization softening operation process comprises the following steps: alkaline agent (30% NaOH solution), inlet water pH8.5-10, preferably 9.5, and calcium removal rate greater than 90%. And controlling the addition of the scale inhibitor of the primary RO system to be not more than 2ppm and the flow rate to be 60 m/h.
The water quality of the negative hard mine water is as follows:
| index name | Quality of water |
| pH | 8.3 |
| Soluble Total solids (mg/L) | 3010 |
| Total hardness (mg/L) | 226 |
| Total alkalinity (as CaCO)3Meter) | 570 |
| Sodium (mg/L) | 9.5 |
| Calcium (mg/L) | 52 |
| Magnesium (mg/L) | 13.9 |
| Sulfate (mg/L) | 864 |
| Chloride (mg/L) | 374 |
| Silicon dioxide (mg/L) | 9.53 |
| Suspended substance (mg/L) | 25 |
| CODCr(mg/L) | 16 |
| BOD5(mg/L) | 3 |
| Bicarbonate radical (mg/L) | 727 |
| Carbonate (mg/L) | 5 |
The invention has the following advantages:
(1) in a process system, pre-concentration treatment is adopted, and mine water with large water volume is concentrated and reduced through a first-stage SWRO.
(2) Calcium ions in water are removed by adopting a circulating fluidization induced crystallization softening system, and the negative hardness characteristic of mine water is utilized to induce crystallization to form CaCO3 crystal. The method does not need a filter or other mechanical dehydration equipment, and the dried solid crystal is over 90 percent without dehydration treatment.
(3) The method adopts two-stage nanofiltration, adapts to the characteristic of variable water quality of mine water, improves the purity of sodium chloride crystal salt, improves the pollution resistance and the buffer property of a salt separation membrane system, avoids the risk of influencing the quality of the crystal salt due to the poor salt separation effect in the operation of a conventional one-stage nanofiltration system, and ensures the long-term reliable and stable operation of the system.
(4) The components in the mine water are complex, and the residual components such as calcium and magnesium ions, ammonia nitrogen, COD and the like after concentration influence the quality of the crystallized salt by-product obtained by zero discharge of the tail-end strong brine and influence the sale of the crystallized salt. The system adopts a comprehensive impurity removal treatment process to remove trace impurities in the strong brine, and removes calcium and magnesium ions of second-level and third-level RO inlet water through a chelate resin ion exchanger, wherein the removal rate is as high as 99%; the ammonia nitrogen is removed by adding chlorine at the break point, and the removal rate reaches more than 80 percent; COD is removed by an ozone-activated carbon filtration process, and the removal rate reaches more than 60 percent.
(5) The MVR thermal crystallization and the freezing crystallization are organically combined, the yield of pure salt is improved, the mixed salt of sodium sulfate and sodium chloride is dissolved back to the front of the first-stage nanofiltration, the total mixed salt amount is reduced by more than 30%, and the operation cost and the mixed salt treatment cost are reduced.
(6) The first-stage RO adopts a first-stage and a second-stage, the reflux between the two stages is carried out, and the recovery rate is 80 percent; the second-stage RO adopts a first-stage and a second-stage, and the recovery rate is 75 percent; an emergency discharge port is arranged at the position of the second-stage RO concentrated water, when the third-stage RO scales, the second-stage RO can independently operate, the concentrated water is discharged outside, and meanwhile, the third-stage RO can be maintained; the concentrated water of the second-level RO directly enters the third-level RO through a pump so as to save energy consumption, and the recovery rate of the third-level RO is 50 percent; the recovery rate of the treatment process system of the system is more than 95%.
(7) MVR + is frozen and crystallized to stably obtain I-class first-class sodium sulfate crystal salt, and the market value of byproducts is increased, and the indexes are as follows:
drawings
FIG. 1 is a structural diagram of an embodiment 1 of a zero-emission system for treating negative hard mine water by a crystallization granulation softening coupling membrane method;
fig. 2 is a flow chart of an embodiment 2 of a zero-emission system for treating negative hard mine water by a crystallization granulation softening coupling membrane method.
Reference numerals:
1. a concentration pretreatment unit; 11. a raw water adjusting tank; 12. a first-stage V-shaped filter chamber; 13. a primary ultrafiltration device; 14. a first-stage reverse osmosis device; 2. a circulating fluidization induced crystallization softening unit; 21. a circulating fluidization induced crystallization softening system; 22. a regulating tank; 3. a resin softening unit; 31. a secondary ultrafiltration device; 32. a resin softening device; 4. a secondary concentration unit; 41. a decarbonizer; 42. a secondary reverse osmosis device; 5. an ammonia nitrogen removal unit; 51. a first security filter; 52. an ammonia nitrogen reaction tank; 6. a COD removal unit; 61. a high-density sedimentation tank; 62. an ozone reaction tank; 63. an activated carbon filter; 64. a third stage ultrafiltration device; 65. a second cartridge filter; 7. a nanofiltration salt separation unit; 71. a first-stage nanofiltration device; 72. a nanofiltration water production tank; 73. a secondary nanofiltration device; 74. a third-stage reverse osmosis device; 75. a first MVR evaporator; 76. a first MVR crystallizer; 77. a first pure salt dryer; 78. a monovalent ion terminal mother liquor tank; 79. a nanofiltration concentrated water tank; 7a, a second MVR evaporator; 7b, a nitrate dissolving tank; 7c, a second MVR crystallizer; 7d, a second pure salt dryer; 7e, a freezing crystallizer; 7f, a third pure salt dryer; 7g, divalent ion terminal mother liquor tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments.
Example 1
As shown in fig. 1, a zero discharge system for treating hard mine water by a crystallization granulation softening coupling membrane method comprises a concentration pretreatment unit 1, a circulating fluidization induced crystallization softening unit 2, a resin softening unit 3, a secondary concentration unit 4, an ammonia nitrogen removal unit 5, a COD removal unit 6 and a nanofiltration salt separation unit 7 which are connected in sequence;
the concentration pretreatment unit 1 is used for adjusting and filtering negative hard mine water and performing primary concentration pretreatment, the circulating fluidization induction crystallization softening unit 2 is used for softening and removing hardness through induction crystallization, the resin softening unit 3 is used for further removing hardness through ion exchange softening, the secondary concentration unit 4 is used for performing secondary concentration, the ammonia nitrogen removal unit 5 is used for removing ammonia nitrogen, the COD removal unit 6 is used for removing COD through an ozone-activated carbon filtration process, and the nanofiltration salt separation unit 7 is used for separating monovalent ions and divalent ions to obtain monovalent ion crystal finished products and divalent ion crystal finished products;
the water inlet of the circulating fluidization induced crystallization softening unit 2 is connected with the concentrated water outlet of the concentration pretreatment unit 1, and the water inlet of the ammonia nitrogen removal unit 5 is connected with the concentrated water outlet of the secondary concentration unit 4.
Example 2
As shown in fig. 2, the zero-emission system for treating negative hard mine water by a crystallization granulation softening coupling membrane method comprises a concentration pretreatment unit 1, a circulating fluidization induced crystallization softening unit 2, a resin softening unit 3, a secondary concentration unit 4, an ammonia nitrogen removal unit 5, a COD removal unit 6 and a nanofiltration salt separation unit 7 which are sequentially connected;
the concentration pretreatment unit 1 is used for adjusting and filtering negative hard mine water and performing primary concentration pretreatment, the circulating fluidization induction crystallization softening unit 2 is used for softening and removing hardness through induction crystallization, the resin softening unit 3 is used for further removing hardness through ion exchange softening, the secondary concentration unit 4 is used for performing secondary concentration, the ammonia nitrogen removal unit 5 is used for removing ammonia nitrogen, the COD removal unit 6 is used for removing COD through an ozone-activated carbon filtration process, and the nanofiltration salt separation unit 7 is used for separating monovalent ions and divalent ions to obtain monovalent ion crystal finished products and divalent ion crystal finished products;
the water inlet of the circulating fluidization induced crystallization softening unit 2 is connected with the concentrated water outlet of the concentration pretreatment unit 1, and the water inlet of the ammonia nitrogen removal unit 5 is connected with the concentrated water outlet of the secondary concentration unit 4;
the concentration pretreatment unit 1 comprises a raw water regulating tank 11, a primary V-shaped filter tank 12, a primary ultrafiltration device 13 and a primary reverse osmosis device 14 which are connected in sequence;
the circulating fluidization induction crystallization softening unit 2 comprises a circulating fluidization induction crystallization softening system 21 and an adjusting tank 22 which are connected in sequence, and a water inlet of the circulating fluidization induction crystallization softening system 21 is connected with a concentrated water outlet of the primary ultrafiltration device 13;
the resin softening unit 3 comprises a secondary ultrafiltration device 31 and a resin softening device 32 which are connected in sequence; the resin softening device 32 is a chelate resin ion exchanger;
the secondary concentration unit 4 comprises a decarbonizer 41 and a secondary reverse osmosis device 42 which are connected in sequence;
the ammonia nitrogen removal unit 5 comprises a first safety filter 51 and an ammonia nitrogen reaction tank 52 which are connected in sequence;
the COD removing unit 6 comprises a high-density sedimentation tank 61, an ozone reaction tank 62, an activated carbon filter 63, a three-stage ultrafiltration device 64 and a second security filter 65 which are connected in sequence;
the nanofiltration salt separation unit 7 comprises a primary nanofiltration device 71 connected with the outlet of the second security filter 65, a nanofiltration water production tank 72 and a secondary nanofiltration device 73 which are sequentially connected with the water production outlet of the primary nanofiltration device 71, a tertiary reverse osmosis device 74 connected with the water production outlet of the secondary nanofiltration device 73, a first MVR evaporator 75, a first MVR crystallizer 76 and a first pure salt dryer 77 which are sequentially connected with the concentrated water outlet of the tertiary reverse osmosis device 74, a monovalent ion terminal mother liquor tank 78 connected with the mother liquor outlet of the first MVR crystallizer 76, a concentrated water tank 79, a second MVR evaporator 7a, a nitrate dissolving tank 7b, a second MVR crystallizer 7c and a second pure salt dryer 7d which are sequentially connected with the concentrated water outlet of the primary nanofiltration device 71;
the nanofiltration salt separation unit 7 also comprises a freezing crystallizer 7e, a third pure salt dryer 7f and a divalent ion terminal mother liquor tank 7g, wherein the freezing crystallizer 7e and the third pure salt dryer 7f are sequentially connected with a mother liquor outlet of the second MVR crystallizer 7 c;
an outlet of the third pure salt dryer 7f is connected with a water inlet of the primary nanofiltration device 71;
the circulating fluidization induction crystallization softening system 21 comprises a hollow cylindrical barrel with two closed ends, a softening system water inlet, a medicine adding port, a crystalline particle adding port and a water outlet, wherein the hollow cylindrical barrel is vertically arranged, the two ends of the hollow cylindrical barrel are respectively arranged on the barrel, the softening system water inlet, the medicine adding port, the crystalline particle adding port and the water outlet are arranged on the top of the barrel, the water outlet is arranged on one side of the top of the barrel opposite to the crystalline particle adding port, and a water distribution area, a medicine distribution area, a granulation area and a clear water area are sequentially arranged in the barrel from bottom to top; the alkali agent is one or more of the following: lime, sodium hydroxide, sodium carbonate and sodium metaaluminate; adjusting the pH value of the primary concentrated mine water to be more than 9; the seed crystal feeding pipe is filled with proper 0.1-1 mm seed crystal particles with the size of 0.1-1 mm, and the seed crystal particles are one or more of the following particles: calcium carbonate ore, quartz sand, garnet, calcite, veined rock;
the first reverse osmosis unit 14 uses SWRO membranes, and the second reverse osmosis unit 42 and the third reverse osmosis unit 52 use RO membranes;
the first-stage reverse osmosis device 14 and the second-stage reverse osmosis device 42 are both a first-stage and a second-stage;
the concentrated water outlet of the second-stage reverse osmosis device 42 is provided with an emergency discharge port;
also comprises a desalting water tank, a lime device and FeCl3Device, PAM device, MgO device, soda device, H2SO4The device comprises a device, an HCl device, a NaOH device, a scale inhibitor device and a reducing agent device;
the system also comprises a cleaning system, a dosing storage system, a compressed air system, a waste water neutralizing system, an electrical system and an instrument control system.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (9)
1. A crystallization granulation softening coupling membrane method is used for treating zero discharge system of negative hard mine water, which is characterized in that: comprises a concentration pretreatment unit (1), a circulating fluidization induced crystallization softening unit (2), a resin softening unit (3), a secondary concentration unit (4), an ammonia nitrogen removal unit (5), a COD removal unit (6) and a nanofiltration salt separation unit (7) which are connected in sequence;
the concentration pretreatment unit (1) is used for adjusting and filtering negative hard mine water and performing primary concentration pretreatment, the circulating fluidization induction crystallization softening unit (2) is used for softening and removing hardness through induction crystallization, the resin softening unit (3) is used for further removing hardness through ion exchange softening, the secondary concentration unit (4) is used for performing secondary concentration, the ammonia nitrogen removal unit (5) is used for removing ammonia nitrogen, the COD removal unit (6) is used for removing COD through an ozone-activated carbon filtration process, and the nanofiltration salt separation unit (7) is used for separating monovalent ions from divalent ions to obtain monovalent ion crystal finished products and divalent ion crystal finished products;
the water inlet of the circulating fluidization induced crystallization softening unit (2) is connected with the concentrated water outlet of the concentration pretreatment unit (1), and the water inlet of the ammonia nitrogen removal unit (5) is connected with the concentrated water outlet of the secondary concentration unit (4).
2. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 1, is characterized in that:
the concentration pretreatment unit (1) comprises a raw water regulating tank (11), a primary V-shaped filter tank (12), a primary ultrafiltration device (13) and a primary reverse osmosis device (14) which are connected in sequence;
the circulating fluidization induction crystallization softening unit (2) comprises a circulating fluidization induction crystallization softening system (21) and an adjusting tank (22) which are sequentially connected, and a water inlet of the circulating fluidization induction crystallization softening system (21) is connected with a concentrated water outlet of the primary ultrafiltration device (13);
the resin softening unit (3) comprises a secondary ultrafiltration device (31) and a resin softening device (32) which are connected in sequence;
the secondary concentration unit (4) comprises a decarbonizer (41) and a secondary reverse osmosis device (42) which are connected in sequence;
the ammonia nitrogen removal unit (5) comprises a first safety filter (51) and an ammonia nitrogen reaction tank (52) which are sequentially connected;
the COD removal unit (6) comprises a high-density sedimentation tank (61), an ozone reaction tank (62), an activated carbon filter (63), a three-stage ultrafiltration device (64) and a second security filter (65) which are connected in sequence;
the nanofiltration salt separation unit (7) comprises a primary nanofiltration device (71) connected with the outlet of the second security filter (65), a nanofiltration water production tank (72) and a secondary nanofiltration device (73) which are connected with the water production outlet of the primary nanofiltration device (71) in turn, a third reverse osmosis device (74) connected with the water outlet of the second nanofiltration device (73), a first MVR evaporator (75), a first MVR crystallizer (76) and a first pure salt dryer (77) which are connected with the concentrated water outlet of the three-stage reverse osmosis device (74) in sequence, a monovalent ion terminal mother liquor tank (78) connected with the mother liquor outlet of the first MVR crystallizer (76), and a concentrated water tank (79), a second MVR evaporator (7a), a nitrate dissolving tank (7b), a second MVR crystallizer (7c) and a second pure salt dryer (7d) are sequentially connected with a concentrated water outlet of the primary nanofiltration device (71).
3. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 2 is characterized in that: the nanofiltration salt separation unit (7) further comprises a freezing crystallizer (7e) and a third pure salt dryer (7f) which are sequentially connected with a mother liquor outlet of the second MVR crystallizer (7c), and a divalent ion terminal mother liquor tank (7g) which is connected with the mother liquor outlet of the freezing crystallizer (7 e).
4. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 3, is characterized in that: the outlet of the third pure salt dryer (7f) is connected with the water inlet of the primary nanofiltration device (71).
5. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 2 is characterized in that: the circulating fluidization induction crystallization softening system (21) comprises a hollow cylindrical barrel with two closed ends, a softening system water inlet, a dosing port, a crystal particle dosing port and a water outlet, wherein the hollow cylindrical barrel is vertically arranged, the softening system water inlet and the dosing port are respectively arranged on the barrel, the crystal particle dosing port is arranged at the top of the barrel, the water outlet is arranged at one side, opposite to the crystal particle dosing port, of the top of the barrel, and a water distribution area, a medicine distribution area, a granulation area and a clear water area are sequentially arranged in the barrel from bottom to top.
6. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 2 is characterized in that: the primary reverse osmosis device (14) uses a SWRO membrane, and the secondary reverse osmosis device (42) and the tertiary reverse osmosis device (74) use a RO membrane;
the first-stage reverse osmosis device (14) and the second-stage reverse osmosis device (42) are both a first-stage reverse osmosis device and a second-stage reverse osmosis device;
and a concentrated water outlet of the secondary reverse osmosis device (42) is provided with an emergency discharge port.
7. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 1, is characterized in that: also comprises a desalting water tank, a lime device and FeCl3Device, PAM device, MgO device, soda device, H2SO4Device, HCl device, NaOH device and scale inhibitor packAnd a reducing agent device.
8. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 1, is characterized in that: the system also comprises a cleaning system, a dosing storage system, a compressed air system, a waste water neutralizing system, an electrical system and an instrument control system.
9. The zero-emission system for treating negative hard mine water by the crystallization granulation softening coupling membrane method according to claim 2 is characterized in that: the resin softening device (32) is a chelating resin ion exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022896656.XU CN214571316U (en) | 2020-12-04 | 2020-12-04 | Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022896656.XU CN214571316U (en) | 2020-12-04 | 2020-12-04 | Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214571316U true CN214571316U (en) | 2021-11-02 |
Family
ID=78364097
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022896656.XU Active CN214571316U (en) | 2020-12-04 | 2020-12-04 | Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214571316U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114933379A (en) * | 2022-06-15 | 2022-08-23 | 西安洛根科技发展有限公司 | Short-flow reverse osmosis pretreatment system and method |
| CN115340251A (en) * | 2022-07-04 | 2022-11-15 | 哈尔滨工业大学（深圳） | Carbon-neutralized zero-emission industrial water treatment system and treatment method |
| CN116444106A (en) * | 2023-06-14 | 2023-07-18 | 华电电力科学研究院有限公司 | High-hardness high-sulfate type coal mine water treatment method and device |
| CN116655192A (en) * | 2023-08-01 | 2023-08-29 | 金科环境股份有限公司 | High mineral mine drainage water resourceful treatment system |
-
2020
- 2020-12-04 CN CN202022896656.XU patent/CN214571316U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114933379A (en) * | 2022-06-15 | 2022-08-23 | 西安洛根科技发展有限公司 | Short-flow reverse osmosis pretreatment system and method |
| CN115340251A (en) * | 2022-07-04 | 2022-11-15 | 哈尔滨工业大学（深圳） | Carbon-neutralized zero-emission industrial water treatment system and treatment method |
| CN116444106A (en) * | 2023-06-14 | 2023-07-18 | 华电电力科学研究院有限公司 | High-hardness high-sulfate type coal mine water treatment method and device |
| CN116444106B (en) * | 2023-06-14 | 2023-09-12 | 华电电力科学研究院有限公司 | High-hardness high-sulfate type coal mine water treatment method and device |
| CN116655192A (en) * | 2023-08-01 | 2023-08-29 | 金科环境股份有限公司 | High mineral mine drainage water resourceful treatment system |
| CN116655192B (en) * | 2023-08-01 | 2023-10-24 | 金科环境股份有限公司 | High mineral mine drainage water resourceful treatment system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN214571316U (en) | Zero discharge system for treating negative hard mine water by crystallization granulation softening coupling membrane method | |
| CN105565573B (en) | The device and method of desulfurization wastewater zero discharge treatment | |
| CN111362453B (en) | High-salinity coal mine water standard-reaching treatment and resource utilization device and use method thereof | |
| CN112551791A (en) | Zero-emission method for treating negative hard mine water by crystallization granulation softening coupling membrane method | |
| US10011506B2 (en) | System for removing minerals from a brine using electrodialysis | |
| CN109095578B (en) | Method for recovering calcium and magnesium in power plant desulfurization wastewater by oxalic acid precipitation method | |
| CN105502765B (en) | A kind of system and method for handling desulfurization wastewater collaboration Resource recovery | |
| CN112194307A (en) | Coal mine water resource comprehensive utilization system and method | |
| CN112794500B (en) | Coking wastewater strong brine near-zero emission treatment system and treatment method thereof | |
| CN106630350A (en) | Zero-drainage technology of biochemical effluent water deep treatment and resource recycling of coal chemical industry wastewater | |
| CN105084631B (en) | A kind of handling process of resin regeneration waste water | |
| CN214115233U (en) | Negative hard mine water zero-discharge treatment system | |
| CN111777220A (en) | Novel softening treatment method for high-salinity and high-permanent-hardness wastewater | |
| CN104291500B (en) | A kind of lower concentration NH containing Mo 4the recycling treatment system of Cl waste water and method thereof | |
| CN211688666U (en) | Phosphorite wastewater recycling system based on chemical precipitation method and membrane distillation | |
| CN112573720A (en) | Thermal power plant desulfurization wastewater zero-discharge system and method | |
| CN113264605A (en) | Desulfurization wastewater anti-scaling pretreatment method and system | |
| CN209411998U (en) | A kind of processing system of highly mineralized mine water reuse and resource utilization | |
| CN209259867U (en) | Water treatment system with high salt | |
| CN218146261U (en) | Zero release industrial water processing system of carbon neutralization | |
| CN216472672U (en) | Wastewater zero-discharge treatment system | |
| CN105481160A (en) | Method and device for preparing industrial salt with zero emission of concentrated brine | |
| CN111099773A (en) | Desulfurization wastewater treatment method and system | |
| CN110342710A (en) | High chlorine low-sulfur acid group waste water treatment system and its technique | |
| CN215439958U (en) | Softening system suitable for landfill leachate concentrated solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 100039 6th floor, building 1, yard 16, West Fourth Ring Middle Road, Haidian District, Beijing Patentee after: Guoneng Water Environmental Protection Co.,Ltd. Country or region after: China Address before: 100039 501, 502, 5th floor, building 1, yard 16, West Fourth Ring Middle Road, Haidian District, Beijing Patentee before: Guoneng Lang Xinming Environmental Protection Technology Co.,Ltd. Country or region before: China |