CN111233219A - Treatment method for recycling strong brine of metallurgical enterprise - Google Patents
Treatment method for recycling strong brine of metallurgical enterprise Download PDFInfo
- Publication number
- CN111233219A CN111233219A CN202010071541.9A CN202010071541A CN111233219A CN 111233219 A CN111233219 A CN 111233219A CN 202010071541 A CN202010071541 A CN 202010071541A CN 111233219 A CN111233219 A CN 111233219A
- Authority
- CN
- China
- Prior art keywords
- enters
- water
- wastewater
- reverse osmosis
- treatment
- 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.)
- Pending
Links
Images
Classifications
-
- 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
-
- 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
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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010071541.9A CN111233219A (en) | 2020-01-21 | 2020-01-21 | Treatment method for recycling strong brine of metallurgical enterprise |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010071541.9A CN111233219A (en) | 2020-01-21 | 2020-01-21 | Treatment method for recycling strong brine of metallurgical enterprise |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111233219A true CN111233219A (en) | 2020-06-05 |
Family
ID=70867543
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010071541.9A Pending CN111233219A (en) | 2020-01-21 | 2020-01-21 | Treatment method for recycling strong brine of metallurgical enterprise |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111233219A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112374705A (en) * | 2020-12-02 | 2021-02-19 | 邯郸钢铁集团有限责任公司 | High-salinity wastewater treatment process for iron and steel enterprises |
| CN113526751A (en) * | 2021-05-31 | 2021-10-22 | 广东邦普循环科技有限公司 | Method for treating high-salinity wastewater by discharging waste batteries and application |
| CN113603276A (en) * | 2021-08-17 | 2021-11-05 | 鞍钢股份有限公司 | Treatment method for resource utilization of strong brine of coking enterprise |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276094A (en) * | 2011-07-27 | 2011-12-14 | 宝钢工程技术集团有限公司 | Method for treating strong brine |
| CN102674632A (en) * | 2012-05-21 | 2012-09-19 | 龙岩市康琦环保科技有限公司 | Garbage leachate zero-emission reuse treatment method |
| CN103342432A (en) * | 2013-07-23 | 2013-10-09 | 南京工业大学 | Near zero emission process of salt-containing waste water |
| CN104341066A (en) * | 2013-08-06 | 2015-02-11 | 中国科学院过程工程研究所 | Deep-treatment and reusing system and method for industrial standard-meeting externally-discharged wastewater |
| CN104692574A (en) * | 2014-12-22 | 2015-06-10 | 内蒙古久科康瑞环保科技有限公司 | Treatment method of high saline wastewater |
| CN105800886A (en) * | 2016-05-23 | 2016-07-27 | 北京今大禹环境技术股份有限公司 | Resource recycling and treatment technology of high-concentration degradation-resistant salt-containing organic waste water |
-
2020
- 2020-01-21 CN CN202010071541.9A patent/CN111233219A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102276094A (en) * | 2011-07-27 | 2011-12-14 | 宝钢工程技术集团有限公司 | Method for treating strong brine |
| CN102674632A (en) * | 2012-05-21 | 2012-09-19 | 龙岩市康琦环保科技有限公司 | Garbage leachate zero-emission reuse treatment method |
| CN103342432A (en) * | 2013-07-23 | 2013-10-09 | 南京工业大学 | Near zero emission process of salt-containing waste water |
| CN104341066A (en) * | 2013-08-06 | 2015-02-11 | 中国科学院过程工程研究所 | Deep-treatment and reusing system and method for industrial standard-meeting externally-discharged wastewater |
| CN104692574A (en) * | 2014-12-22 | 2015-06-10 | 内蒙古久科康瑞环保科技有限公司 | Treatment method of high saline wastewater |
| CN105800886A (en) * | 2016-05-23 | 2016-07-27 | 北京今大禹环境技术股份有限公司 | Resource recycling and treatment technology of high-concentration degradation-resistant salt-containing organic waste water |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112374705A (en) * | 2020-12-02 | 2021-02-19 | 邯郸钢铁集团有限责任公司 | High-salinity wastewater treatment process for iron and steel enterprises |
| CN113526751A (en) * | 2021-05-31 | 2021-10-22 | 广东邦普循环科技有限公司 | Method for treating high-salinity wastewater by discharging waste batteries and application |
| WO2022252603A1 (en) * | 2021-05-31 | 2022-12-08 | 广东邦普循环科技有限公司 | Method for treating high-salt wastewater by discharging waste batteries and use thereof |
| CN113603276A (en) * | 2021-08-17 | 2021-11-05 | 鞍钢股份有限公司 | Treatment method for resource utilization of strong brine of coking enterprise |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111233219A (en) | Treatment method for recycling strong brine of metallurgical enterprise | |
| CN102452753B (en) | Saliferous organic wastewater treatment method | |
| CN110526346B (en) | Electrochemical anaerobic membrane biological sewage treatment device and treatment method thereof | |
| CN111233237A (en) | Method for realizing zero discharge of high-concentration brine in steel production enterprise | |
| CN111285531A (en) | Method and system for concentrating high-salinity mine water | |
| CN109626672A (en) | Based on nitrate nitrogen method in electrochemistry and resin combination technique advanced treatment of waste water | |
| CN111233265A (en) | Method for recycling comprehensive wastewater in steel production | |
| CN111268859A (en) | Method for simultaneously preparing hydrochloric acid and sodium hydroxide by utilizing reverse osmosis strong brine | |
| CN107226581B (en) | Zinc-containing wastewater treatment method, treatment system and application | |
| CN111170587A (en) | Spraying wastewater treatment process | |
| CN108328836B (en) | Water inlet control system based on high-salt-content wastewater reduction process | |
| CN114212859B (en) | Two-stage electrochemical crosslinking electrodialysis desalination treatment system and application thereof | |
| CN218810941U (en) | A processing system for metallurgical enterprise strong brine recycle | |
| CN111233220A (en) | Pretreatment method for reducing concentrated brine in steel industry | |
| CN111620484A (en) | Treatment method and treatment device for three-gas combined production water | |
| CN218321020U (en) | Iron and steel industry strong brine minimizing pretreatment system | |
| CN218435298U (en) | System for utilize reverse osmosis strong brine preparation acid-base | |
| CN113105036A (en) | High-salinity water body desalting system based on electric adsorption technology | |
| CN218321021U (en) | High-concentration salt water zero-discharge system for iron and steel production enterprises | |
| CN107365013B (en) | Cyanide-containing wastewater treatment method, treatment system and application | |
| CN220182990U (en) | Zero discharge system of comprehensive wastewater of steel and iron combined enterprises | |
| CN111233264A (en) | Treatment method for recycling comprehensive wastewater in metallurgical industry | |
| CN219637065U (en) | Full quantization treatment process system for landfill leachate | |
| CN219174358U (en) | Reclaimed water source desalting concentrated water recycling system | |
| CN218435383U (en) | Landfill leachate fully-quantized processing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200605 |
|
| RJ01 | Rejection of invention patent application after publication |