CN111233219A - Treatment method for recycling strong brine of metallurgical enterprise - Google Patents
Treatment method for recycling strong brine of metallurgical enterprise Download PDFInfo
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- 239000012267 brine Substances 0.000 title claims abstract description 37
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000004064 recycling Methods 0.000 title claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000002351 wastewater Substances 0.000 claims abstract description 49
- 230000001105 regulatory effect Effects 0.000 claims abstract description 30
- 238000005189 flocculation Methods 0.000 claims abstract description 28
- 230000016615 flocculation Effects 0.000 claims abstract description 28
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 25
- 238000001179 sorption measurement Methods 0.000 claims abstract description 24
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 18
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 18
- 229910000831 Steel Inorganic materials 0.000 claims abstract description 15
- 239000010959 steel Substances 0.000 claims abstract description 15
- 150000003839 salts Chemical class 0.000 claims abstract description 12
- 239000012528 membrane Substances 0.000 claims abstract description 10
- 238000009287 sand filtration Methods 0.000 claims abstract description 7
- 230000008929 regeneration Effects 0.000 claims abstract description 6
- 238000011069 regeneration method Methods 0.000 claims abstract description 6
- 239000010802 sludge Substances 0.000 claims abstract description 6
- 239000013522 chelant Substances 0.000 claims abstract description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 53
- 239000013505 freshwater Substances 0.000 claims description 25
- 230000001276 controlling effect Effects 0.000 claims description 22
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 12
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 11
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 10
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 10
- 229910052791 calcium Inorganic materials 0.000 claims description 10
- 239000011575 calcium Substances 0.000 claims description 10
- 229910021645 metal ion Inorganic materials 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 8
- 229910052742 iron Inorganic materials 0.000 claims description 6
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims description 5
- 239000006004 Quartz sand Substances 0.000 claims description 5
- 229910052782 aluminium Inorganic materials 0.000 claims description 5
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000007772 electrode material Substances 0.000 claims description 5
- 238000011010 flushing procedure Methods 0.000 claims description 5
- 229910052748 manganese Inorganic materials 0.000 claims description 5
- 239000011572 manganese Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 230000000737 periodic effect Effects 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 239000011347 resin Substances 0.000 claims description 5
- 229920005989 resin Polymers 0.000 claims description 5
- 239000002356 single layer Substances 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 5
- 238000009297 electrocoagulation Methods 0.000 claims description 4
- 239000003344 environmental pollutant Substances 0.000 claims description 2
- 150000002500 ions Chemical class 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims description 2
- 231100000719 pollutant Toxicity 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 238000011001 backwashing Methods 0.000 abstract 1
- 238000003672 processing method Methods 0.000 abstract 1
- 229910052749 magnesium Inorganic materials 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
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- 238000010612 desalination reaction Methods 0.000 description 4
- 238000009292 forward osmosis Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 239000008235 industrial water Substances 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- 238000011033 desalting Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
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- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
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- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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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
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4691—Capacitive deionisation
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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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
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a processing method for recycling strong brine of a metallurgical enterprise, wherein the strong brine of the steel industry enters an adjusting tank and enters electric flocculation equipment, and sludge discharged by an electric flocculation device enters a sludge treatment system for treatment; the effluent of the electric flocculation enters a primary electric adsorption device, and secondary electric adsorption concentrated water returns to a front-end regulating reservoir; and the produced water after the secondary electro-adsorption treatment enters a sand filtration device, sand filtration backwashing water enters a front end regulating reservoir, effluent enters an ultrafiltration device, ultrafiltration produced water enters chelate ion exchange resin, regeneration wastewater of the ion exchange resin flows back to the regulating reservoir for circulation treatment, and the effluent enters a membrane concentration unit. The advantages are that: the electric flocculation and electric adsorption technology selected in the pretreatment process fully utilizes the characteristic of high salt content of metallurgical strong brine, the energy consumption of the process is low, the cost is low, the equipment is simple, the operation is easy, the treatment effect is stable, and good water inlet conditions are created for subsequent membrane concentration.
Description
Technical Field
The invention belongs to the technical field of industrial wastewater treatment, and particularly relates to a treatment method for recycling strong brine of a metallurgical enterprise.
Background
The unit water consumption of the steel enterprises in China is still higher than the level of the advanced steel enterprises in China, so that the new water consumption per ton of steel of the steel enterprises is further reduced, the cyclic utilization rate of water of the steel enterprises is improved, and the comprehensive treatment and recycling of wastewater of the steel enterprises are enhanced, which is one of the keys for realizing sustainable development of the steel enterprises.
The reuse of wastewater is the final target of wastewater treatment, but after the wastewater is subjected to reverse osmosis treatment, most of primary pure water is obtained, and simultaneously, a large proportion of high-salinity concentrated water is also produced, the concentrated water is an inevitable product of a reverse osmosis desalination process, contains high organic matters and salt concentration, and the concentrated water content is about 25% of the reverse osmosis treatment water content. For the high-salinity concentrated water, the treatment method at the present stage is basically direct discharge, which causes a great deal of resource waste and environmental pollution.
In the prior art, patent application No.: 201010283192.3 discloses a process for desalting strong brine by pervaporation technology and recovering purified water. The process can maximally concentrate the strong brine, and has high desalination rate and low effluent conductivity. Meanwhile, the heat recovery technology is combined, the overall energy consumption of the system is greatly reduced, and the system can be used for desalting wastewater such as reverse osmosis concentrated drainage, circulating cooling sewage and the like. However, the technology has high operation energy consumption, needs to heat the strong brine to more than 60 ℃, and can only remove the salt in the strong brine.
Patent application No.: 200910070804.8, a forward osmosis membrane component is adopted, the seawater desalination strong brine is used as a drawing liquid, fresh water is used as a feeding liquid, part of the fresh water which permeates the seawater desalination strong brine at the permeation side of the forward osmosis membrane component and the feeding liquid side is mixed into diluted standard salt water and then is discharged out of the forward osmosis membrane component, and the rest of the feeding liquid is discharged out of the forward osmosis membrane component. However, the technology can only be used for treating the seawater strong brine, and is not suitable for the strong brine process in the metallurgical industry.
Patent publication No. CN1030773143B discloses a strong brine zero emission treatment process of steel plant, adopts tertiary reverse osmosis process to carry out waste water concentration, then carries out evaporation crystallization. The concentration of the three-stage reverse osmosis has high operation cost, and the process does not consider the problems of organic matter pollution, inorganic matter scaling and the like of the reverse osmosis membrane, so that the popularization and the application are limited.
In conclusion, the existing strong brine treatment process of metallurgical enterprises has the defects of poor treatment effect, serious membrane pollution, low water yield of a system and overhigh process operation cost. Therefore, the method for recycling the concentrated brine of the metallurgical enterprise with low cost and high efficiency is developed, so that a large amount of new water resources can be saved for the metallurgical enterprise, the adverse effect of the waste water discharge on the environment of the surrounding water area can be reduced by greatly reducing the discharge amount of the concentrated brine, and the method has important significance for realizing water saving and emission reduction of the enterprise.
Disclosure of Invention
Aiming at the strong brine discharged by a steel enterprise, the strong brine is sequentially treated by electric flocculation, electric adsorption, sand filtration, ion exchange resin, ultrafiltration and reverse osmosis, so that the aim of reducing and recycling the strong brine of the metallurgical enterprise is fulfilled, the whole process is stable in operation, and the energy consumption is low.
In order to achieve the purpose, the invention is realized by the following technical scheme:
a treatment method for recycling strong brine of a metallurgical enterprise comprises the following steps:
1) the method comprises the following steps of (1) enabling strong brine of a metallurgical enterprise to firstly enter a regulating tank to balance water quality and water quantity; the effluent of the regulating reservoir enters an electrocoagulation device, and the high salinity characteristic of the wastewater is utilized to reduce the electric quantity consumption required by the electrocoagulation; selecting an aluminum polar plate as an electrode material of the electric flocculation device, controlling the reaction voltage to be 4V-6V, controlling the distance between the polar plates to be 2cm-4cm, controlling the reaction time to be 20-30min, controlling the pH of the wastewater to be 7.0-8.0, and adopting a periodic reversing power supply to exchange the cathode and the anode of the electric flocculation in a certain period, wherein the reversing period is 6-8 s; sludge discharged by the electric flocculation device enters a sludge treatment system for treatment, and suspended matters and calcium and magnesium metal ions in the wastewater are reduced after the electric flocculation treatment;
2) the effluent of the electric flocculation device enters an electric adsorption device, and ions and charged particles in the water are adsorbed by a charged electrode, so that dissolved salts and other charged substances are enriched and concentrated on the surface of the electrode to realize wastewater purification; controlling the voltage of the polar plates to be 0.8-1.6V, the distance between the polar plates to be 1cm-2cm, the pH value of the wastewater to be 7.0-8.0, and returning the electro-adsorption concentrated water to the front-end regulating tank;
3) the produced water after the electro-adsorption treatment enters a sand filtration device, a single-layer quartz sand homogeneous filter material is adopted, the turbidity and suspended matters of the filtered effluent are further reduced, the sand filtration backwash water enters a front-end regulating reservoir, the effluent enters chelate ion exchange resin, the exchange performance of the resin is utilized to adsorb residual calcium and magnesium metal ions in the wastewater, the regeneration wastewater of the ion exchange resin flows back to a regulating reservoir for circulation treatment, the produced water of the ion exchange resin enters an ultrafiltration device, the pH of the wastewater is controlled to be 6.2-6.6, the suspended matters and colloidal pollutants in the wastewater are further intercepted through an ultrafiltration membrane, the ultrafiltration produced water meets the reverse osmosis water inlet condition that the oil is less than or equal to 0.1mg/L, SDI and less than or equal to 3 and the iron and manganese are less than or equal to 0.05mg/L, and the ultrafiltration concentrated water flows back to the regulating reservoir for circulation; the ultrafiltration product water enters a first reverse osmosis for concentration and separation, most of salt and micromolecule organic matters in the wastewater are intercepted, the first reverse osmosis product water enters a fresh water storage tank for reuse in fresh water users, the first reverse osmosis concentrated water enters a second reverse osmosis for further concentration and separation, the second reverse osmosis product water enters the fresh water storage tank for reuse in the fresh water users, the high-salt water generated by the second reverse osmosis is used for blast furnace slag flushing, and the total RO recovery rate of a two-stage reverse osmosis system is 85% -95%.
The concentrated brine of the metallurgy enterprise is the concentrated brine generated by the reverse osmosis process of the steel enterprise, and has the pH value of 7.0-8.5, the conductivity of 8.0-9.0ms/cm, the COD of 70-100mg/L and the total hardness of 1200-1400 mg/L.
Compared with the prior art, the invention has the beneficial effects that:
the electric flocculation and electric adsorption technology selected in the treatment process fully utilizes the characteristic of high salt content of metallurgical strong brine, the energy consumption of the process is low, the cost is low, the equipment is simple, the operation is easy, the treatment effect is stable, the quality of the reuse water meets the requirement of the quality of the industrial fresh water, the total recovery rate of the system is more than 85 percent, the quality of the reuse water meets the requirement of the quality of the industrial fresh water, the generation amount of the strong brine is reduced, the reuse rate of the production wastewater is greatly improved, and the cost of purchasing the fresh water outside an enterprise is reduced.
Drawings
FIG. 1 is a process flow diagram of the recovery and utilization of concentrated brine in metallurgical enterprises.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings, but it should be noted that the present invention is not limited to the following embodiments.
Example 1
As shown in figure 1, the concentrated brine produced by the reverse osmosis process of the steel enterprises has pH of 7.0-8.5, conductivity of 8.0-9.0ms/cm, COD of 70-100mg/L and total hardness of 1200-1400 mg/L.
The treatment method comprises the following steps:
1) the strong brine firstly enters an adjusting tank to balance the water quality and the water quantity. And (3) enabling the effluent of the regulating reservoir to enter an electric flocculation device, selecting an aluminum polar plate as an electrode material of the electric flocculation device, controlling the reaction voltage to be 4V, controlling the distance between the polar plates to be 2cm, controlling the reaction time to be 20min, controlling the pH value of the wastewater to be 7.0, and adopting a periodic reversing power supply as the power supply for 6 s. After the electric flocculation treatment, metal ions such as suspended matters, calcium, magnesium and the like in the wastewater are effectively reduced; the effluent of the electric flocculation enters an electric adsorption device, the voltage of a polar plate of the electric adsorption device is controlled to be 0.8V, the distance between the polar plates is 1cm, the pH value of the wastewater is 7.0, and the concentrated electric adsorption water returns to a front-end regulating tank;
2) the produced water after the electro-adsorption treatment enters a sand filter device, a single-layer quartz sand homogeneous filter material is adopted, the turbidity and suspended matters of the filtered effluent are further reduced, sand filter backwash water enters a front-end regulating reservoir, the effluent enters ion exchange resin, and the residual metal ions such as calcium, magnesium and the like in the wastewater are adsorbed through the exchange performance of the resin, the regeneration wastewater of the ion exchange resin flows back to the regulating reservoir for circular treatment, the produced water of the ion exchange resin enters an ultrafiltration device, the pH of the wastewater is controlled to be 6.2, the ultrafiltration produced water meets the reverse osmosis water inlet condition that the oil is less than or equal to 0.1mg/L, SDI and less than or equal to 3 and the iron and the manganese are less than or equal to 0.05mg/L, and the ultrafiltration concentrated water flows back to the regulating. The ultrafiltration produced water enters a first reverse osmosis for concentration and separation, most of salt and micromolecule organic matters in the wastewater are intercepted, the first reverse osmosis produced water enters a fresh water storage tank for reuse in fresh water users, the first reverse osmosis concentrated water enters a second reverse osmosis for further concentration and separation, the second reverse osmosis produced water enters the fresh water storage tank for reuse in the fresh water users (the produced water conductance is less than 80 mu s/cm, the COD is less than 5mg/L, and the total hardness is less than 0.1mg/L), the water quality is far better than the standard requirement of GB/T19923 + 2005 urban sewage recycling industrial water quality, the total recovery rate of RO of a two-stage reverse osmosis system is 92%, and the high-salt water produced by the second reverse osmosis is used for slag flushing of a blast furnace.
Example 2
As shown in figure 1, the concentrated brine produced by the reverse osmosis process of the steel enterprises has pH of 7.0-8.5, conductivity of 8.0-9.0ms/cm, COD of 70-100mg/L and total hardness of 1200-1400 mg/L.
The treatment method comprises the following steps:
1) the strong brine firstly enters an adjusting tank to balance the water quality and the water quantity. And (3) allowing the outlet of the regulating tank to enter an electric flocculation device, selecting an aluminum polar plate as an electrode material of the electric flocculation device, controlling the reaction voltage to be 5V, controlling the distance between the polar plates to be 3cm, controlling the reaction time to be 25min, controlling the pH value of the wastewater to be 7.5, and adopting a periodic reversing power supply as the power supply for 7 s. After the electric flocculation treatment, metal ions such as suspended matters, calcium, magnesium and the like in the wastewater are effectively reduced; the effluent of the electric flocculation enters an electric adsorption device, the voltage of a polar plate of the electric adsorption device is controlled to be 1.2V, the distance between the polar plates is 1.5cm, the pH value of the wastewater is 7.5, and the electric adsorption concentrated water returns to a front-end regulating reservoir;
2) the produced water after the electro-adsorption treatment enters a sand filter device, a single-layer quartz sand homogeneous filter material is adopted, the turbidity and suspended matters of the filtered effluent are further reduced, sand filter backwash water enters a front-end regulating reservoir, the effluent enters ion exchange resin, and the residual metal ions such as calcium, magnesium and the like in the wastewater are adsorbed through the exchange performance of the resin, the regeneration wastewater of the ion exchange resin flows back to the regulating reservoir for circular treatment, the produced water of the ion exchange resin enters an ultrafiltration device, the pH of the wastewater is controlled to be 6.4, the ultrafiltration produced water meets the reverse osmosis water inlet condition that the oil is less than or equal to 0.1mg/L, SDI and less than or equal to 3 and the iron and the manganese are less than or equal to 0.05mg/L, and the ultrafiltration concentrated water flows back to the regulating. The ultrafiltration produced water enters a first reverse osmosis for concentration and separation, most of salt and micromolecule organic matters in the wastewater are intercepted, the first reverse osmosis produced water enters a fresh water storage tank for reuse in fresh water users, the first reverse osmosis concentrated water enters a second reverse osmosis for further concentration and separation, the second reverse osmosis produced water enters the fresh water storage tank for reuse in the fresh water users (the produced water conductance is less than 80 mu s/cm, the COD is less than 5mg/L, and the total hardness is less than 0.1mg/L), the water quality is far better than the standard requirement of GB/T19923 + 2005 urban sewage recycling industrial water quality, the total recovery rate of RO of a two-stage reverse osmosis system is 89%, and the high-salt water produced by the second reverse osmosis is used for slag flushing of a blast furnace.
Example 3
As shown in figure 1, the concentrated brine produced by the reverse osmosis process of the steel enterprises has pH of 7.0-8.5, conductivity of 8.0-9.0ms/cm, COD of 70-100mg/L and total hardness of 1200-1400 mg/L.
The treatment method comprises the following steps:
1) the strong brine firstly enters an adjusting tank to balance the water quality and the water quantity. And (3) allowing the outlet of the regulating tank to enter an electric flocculation device, selecting an aluminum polar plate as an electrode material of the electric flocculation device, controlling the reaction voltage to be 6V, controlling the distance between the polar plates to be 4cm, controlling the reaction time to be 30min, controlling the pH value of the wastewater to be 8.0, and adopting a periodic reversing power supply as the power supply for 8 s. After the electric flocculation treatment, metal ions such as suspended matters, calcium, magnesium and the like in the wastewater are effectively reduced; the effluent of the electric flocculation enters an electric adsorption device, the voltage of a polar plate of the electric adsorption device is controlled to be 1.6V, the distance between the polar plates is 2cm, the pH value of the wastewater is 8.0, and the concentrated electric adsorption water returns to a front-end regulating tank;
2) the produced water after the electro-adsorption treatment enters a sand filter device, a single-layer quartz sand homogeneous filter material is adopted, the turbidity and suspended matters of the filtered effluent are further reduced, sand filter backwash water enters a front-end regulating reservoir, the effluent enters ion exchange resin, and the residual metal ions such as calcium, magnesium and the like in the wastewater are adsorbed through the exchange performance of the resin, the regeneration wastewater of the ion exchange resin flows back to the regulating reservoir for circular treatment, the produced water of the ion exchange resin enters an ultrafiltration device, the pH of the wastewater is controlled to be 6.6, the ultrafiltration produced water meets the reverse osmosis water inlet condition that the oil is less than or equal to 0.1mg/L, SDI and less than or equal to 3 and the iron and the manganese are less than or equal to 0.05mg/L, and the ultrafiltration concentrated water flows back to the regulating. The ultrafiltration produced water enters a first reverse osmosis for concentration and separation, most of salt and micromolecule organic matters in the wastewater are intercepted, the first reverse osmosis produced water enters a fresh water storage tank for reuse in fresh water users, the first reverse osmosis concentrated water enters a second reverse osmosis for further concentration and separation, the second reverse osmosis produced water enters the fresh water storage tank for reuse in the fresh water users (the produced water conductance is less than 80 mu s/cm, the COD is less than 5mg/L, and the total hardness is less than 0.1mg/L), the water quality is far better than the standard requirement of GB/T19923 + 2005 urban sewage recycling industrial water quality, the total recovery rate of RO of a two-stage reverse osmosis system is 91%, and the high-salt water produced by the second reverse osmosis is used for slag flushing of a blast furnace.
Claims (2)
1. A treatment method for recycling strong brine of a metallurgical enterprise is characterized by comprising the following steps:
1) the method comprises the following steps of (1) enabling strong brine of a metallurgical enterprise to firstly enter a regulating tank to balance water quality and water quantity; the effluent of the regulating reservoir enters an electrocoagulation device, and the high salinity characteristic of the wastewater is utilized to reduce the electric quantity consumption required by the electrocoagulation; selecting an aluminum polar plate as an electrode material of the electric flocculation device, controlling the reaction voltage to be 4V-6V, controlling the distance between the polar plates to be 2cm-4cm, controlling the reaction time to be 20-30min, controlling the pH of the wastewater to be 7.0-8.0, and adopting a periodic reversing power supply to exchange the cathode and the anode of the electric flocculation in a certain period, wherein the reversing period is 6-8 s; sludge discharged by the electric flocculation device enters a sludge treatment system for treatment, and suspended matters and calcium and magnesium metal ions in the wastewater are reduced after the electric flocculation treatment;
2) the effluent of the electric flocculation device enters an electric adsorption device, and ions and charged particles in the water are adsorbed by a charged electrode, so that dissolved salts and other charged substances are enriched and concentrated on the surface of the electrode to realize wastewater purification; controlling the voltage of the polar plates to be 0.8-1.6V, the distance between the polar plates to be 1cm-2cm, the pH value of the wastewater to be 7.0-8.0, and returning the electro-adsorption concentrated water to the front-end regulating tank;
3) the produced water after the electro-adsorption treatment enters a sand filtration device, a single-layer quartz sand homogeneous filter material is adopted, the turbidity and suspended matters of the filtered effluent are further reduced, the sand filtration backwash water enters a front-end regulating reservoir, the effluent enters chelate ion exchange resin, the exchange performance of the resin is utilized to adsorb residual calcium and magnesium metal ions in the wastewater, the regeneration wastewater of the ion exchange resin flows back to a regulating reservoir for circulation treatment, the produced water of the ion exchange resin enters an ultrafiltration device, the pH of the wastewater is controlled to be 6.2-6.6, the suspended matters and colloidal pollutants in the wastewater are further intercepted through an ultrafiltration membrane, the ultrafiltration produced water meets the reverse osmosis water inlet condition that the oil is less than or equal to 0.1mg/L, SDI and less than or equal to 3 and the iron and manganese are less than or equal to 0.05mg/L, and the ultrafiltration concentrated water flows back to the regulating reservoir for circulation; the ultrafiltration product water enters a first reverse osmosis for concentration and separation, most of salt and micromolecule organic matters in the wastewater are intercepted, the first reverse osmosis product water enters a fresh water storage tank for reuse in fresh water users, the first reverse osmosis concentrated water enters a second reverse osmosis for further concentration and separation, the second reverse osmosis product water enters the fresh water storage tank for reuse in the fresh water users, the high-salt water generated by the second reverse osmosis is used for blast furnace slag flushing, and the total RO recovery rate of a two-stage reverse osmosis system is 85% -95%.
2. The method as claimed in claim 1, wherein the concentrated brine produced by the reverse osmosis process of the iron and steel enterprises has pH of 7.0-8.5, conductivity of 8.0-9.0ms/cm, COD of 70-100mg/L, and total hardness of 1200-1400 mg/L.
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