CN219239460U - Brine sulfate ion removal system in chlor-alkali production - Google Patents
Brine sulfate ion removal system in chlor-alkali production Download PDFInfo
- Publication number
- CN219239460U CN219239460U CN202320009279.4U CN202320009279U CN219239460U CN 219239460 U CN219239460 U CN 219239460U CN 202320009279 U CN202320009279 U CN 202320009279U CN 219239460 U CN219239460 U CN 219239460U
- Authority
- CN
- China
- Prior art keywords
- brine
- pipe
- heat exchanger
- nitrate
- permeate
- 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
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a brine sulfate ion removal system in chlor-alkali production, which comprises a brine buffer tank, a circulating water heat exchanger, a permeate brine heat exchanger, an active carbon tower, a high-pressure pump, a membrane component and the like, wherein low-nitrate brine enters the permeate brine tank after heat exchange of a secondary heat exchanger, the permeate brine tank is connected to the permeate brine heat exchanger through a permeate brine pipe b, a permeate brine pump, a communicating pipe, a heat exchange water supply valve and a recovery pipe are sequentially and fixedly connected to the pipeline, the communicating pipe is provided with the communicating valve, the recovery pipe is provided with the recovery valve, and a temperature remote transmission device arranged behind the active carbon tower, a PH on-line detector behind the tower and a free chlorine on-line detector behind the tower are electrically connected with the recovery valve; the low-nitrate brine and the osmotic brine which are arranged in the system are recycled and heat-exchanged, so that the load of a refrigerator and the water consumption of circulating water are reduced, the cold quantity of the low-nitrate brine is further utilized, meanwhile, the low-nitrate brine and the osmotic brine are initially heated, and the heat source consumption is saved after the low-nitrate brine and the osmotic brine return to a salt dissolving process; and the recovery pipeline and the communication pipeline are arranged, so that the stable operation of the process system is improved.
Description
Technical Field
The utility model belongs to the field of chlor-alkali production, and particularly relates to a sulfate ion removal system in brine.
Background
Raw salt is one of the main raw materials in the chlor-alkali production process, in actual production, the raw salt is required to be dissolved into saturated brine, and impurities are filtered out for the first time and refined for the second time, so that the produced brine meets the process requirement of ionic membrane electrolysis; one of the sources of sulfate ions in the brine is introduced as a raw material, the raw salt contains a certain amount of sulfate radical, the sulfate radical can be brought into the system along with the dissolution of the raw salt, the sulfate radical can not be brought out of caustic soda due to the characteristics of an ionic membrane, the sulfate radical can be enriched in the system, the other source is mainly generated in the dechlorination process of the dilute brine, the dechlorinated dilute brine at the outlet of an ionic membrane electrolysis tank is recycled to primary brine, in order to remove free chlorine in the brine, sodium sulfite is added for removal, and sulfate radical can be generated by sodium sulfite and free chloride in the system, so that the sulfate radical can be continuously accumulated in the system; if the content of various anions and cations, particularly sulfate ions, in the brine is too high, the ion membrane in the subsequent electrolysis process is blocked, so that the cell voltage is increased, the current efficiency is reduced, the normal electrolysis production is affected, and the production cost is increased.
The current advanced method is a membrane method denitration technology, and the method is widely used in chlor-alkali production. In the actual production process, the normal operation of the membrane treatment unit is directly influenced due to fluctuation of the index temperature of the feed brine, free chlorine, pH value and the like and the abnormal influence of a brine conveying pump, and the service life of the membrane component is adversely affected by frequent start and stop; and the subsequent freezing units have large freezing load, the temperature of cooling water does not reach the standard, the cold quantity is not fully utilized, and the like, so that the problem of poor crystallization sedimentation effect is solved.
Disclosure of Invention
In order to overcome the defects in the prior art, improve the stable operation of a process system, effectively solve the problems that the fluctuation of index temperature, free chlorine, pH value and the like of feed brine directly affects the normal operation of a membrane treatment unit, the cooling water temperature is not up to standard due to the fact that the subsequent freezing unit has large freezing load, the cooling water temperature is not fully utilized and the like, and the crystallization sedimentation effect is poor, the utility model provides a high-efficiency sulfate ion removal system for brine in chlor-alkali production.
The technical scheme of the brine sulfate ion removal system in chlor-alkali production is as follows:
the brine sulfate ion removal system in chlor-alkali production comprises a brine buffer tank, a brine buffer pump, a circulating water heat exchanger, a permeate brine heat exchanger, an activated carbon tower, a security filter, a high-pressure pump and a membrane component which are sequentially connected, wherein one side of the membrane component is sequentially connected to a concentrated brine tank, a concentrated brine pump, a primary heat exchanger, a secondary heat exchanger, a tertiary heat exchanger and a solid-liquid separator through a concentrated brine outlet pipe, the upper end of the solid-liquid separator is connected to a low-nitrate brine tank through a low-nitrate brine pipe a, the low-nitrate brine tank is connected to the secondary heat exchanger through a low-nitrate brine pipe b, the low-nitrate brine pump is fixedly connected to a low-nitrate brine pipe, and the low-nitrate brine tank is connected to the permeate brine tank after heat exchange; the other side of the membrane component is connected with a permeate brine tank through a permeate brine outlet pipe; the osmotic brine tank is connected to the osmotic brine heat exchanger through an osmotic brine pipe b, and a pipeline is sequentially and fixedly connected with an osmotic brine pump, a communicating pipe, a heat exchange water supply valve and a recovery pipe, wherein the communicating pipe is provided with a communicating valve, and the recovery pipe is provided with a recovery valve; the active carbon tower front pipeline is provided with a tower front PH on-line detector and a tower front free chlorine on-line detector, the active carbon tower rear pipeline is provided with a temperature remote transmission, a tower rear PH on-line detector and a tower rear free chlorine on-line detector, and the temperature remote transmission, the tower rear PH on-line detector and the tower rear free chlorine on-line detector are electrically connected with a recovery valve.
Further, the brine buffer tank is connected with a brine feeding pipe, an acid adding pipe and a sodium sulfite adding pipe, and control valves are respectively arranged.
Furthermore, the brine buffer pump and the high-pressure pump are provided with frequency converters, and the system brine flow and pressure are effectively controlled through the frequency conversion controllers.
Furthermore, the membrane component is provided with a flushing pipe, and flushing water is pure water or sterilizing water.
Further, the primary heat exchanger, the secondary heat exchanger and the tertiary heat exchanger are respectively connected with a circulating water pipeline, a low-nitrate water pipeline and a calcium chloride salt water pipeline, and the secondary heat exchanger can be at least provided with 1, and can be provided with a plurality of serial connection when the cooling capacity is insufficient.
The beneficial effects of the utility model are as follows:
1. the low-nitrate brine and the osmotic brine which are arranged in the system are recycled and heat-exchanged, so that the load of a refrigerating machine of a subsequent refrigerating unit and the water consumption of cooling circulation are reduced, the cold quantity of the low-nitrate brine is further utilized, meanwhile, the low-nitrate brine and the osmotic brine are initially heated in the heat exchange process, and the heat source consumption is saved after the salt melting process is returned.
2. The recovery pipeline and the communication pipeline arranged in the process system improve the stable operation of the process system, effectively solve the problem that the temperature, free chlorine, pH value and the like of the index of the feed brine fluctuate, directly influence the normal operation of the membrane treatment unit, reduce the shutdown times, have high degree of automation and stable operation, realize the automatic detection and control of the DCS in the whole process, ensure the stable operation of the system and reduce the labor intensity of personnel.
Drawings
FIG. 1 is a schematic view of the present utility model
In the figure: 1. a brine buffer tank; 2. a brine buffer pump; 3. a circulating water heat exchanger; 4. a permeate brine heat exchanger; 5. an activated carbon tower; 6. a cartridge filter; 7. a high pressure pump; 8. a membrane module; 9. concentrated nitrate brine tank; 10. concentrated nitrate water pump; 11. a primary heat exchanger; 12. a secondary heat exchanger; 13. a three-stage heat exchanger; 14. a solid-liquid separator; 15. a low-nitrate brine tank; 16. a low nitrate water pump; 17. a low-nitrate water pipe a;18. a low-nitrate water pipe b;19. osmotic brine tank; 20. a penetrating salt water pipe a;21. a permeate brine pump; 22. a permeate brine pipe b;23. a communicating pipe; 24. a recovery pipe; 25. a heat exchange water supply valve; 26. a communication valve; 27. a recovery valve; 28. an online PH detector in front of the tower; 29. an online detector for free chlorine in front of the tower; 30. temperature remote transmission; 31. an online PH detector behind the tower; 32. a free chlorine on-line detector behind the tower; 33. a brine feed pipe; 34. an acid adding pipe; 35. adding sodium sulfite tube; 36. a flushing pipe; 37. concentrated nitrate water pipe.
Detailed Description
The following description of the embodiments of the present utility model will be made with reference to the accompanying drawings, in which it is evident that the embodiments described are only some, but not all embodiments of the present utility model. Other embodiments, which are within the scope of the utility model, are within the purview of one skilled in the art without the creative effort.
Examples
Referring to fig. 1, the brine sulfate ion removal system in chlor-alkali production provided by the utility model comprises a brine buffer tank 1, a brine buffer pump 2, a circulating water heat exchanger 3, a permeate brine heat exchanger 4, an activated carbon tower 5, a security filter 6, a high-pressure pump 7 and a membrane component 8 which are sequentially connected, wherein one side of the membrane component 8 is sequentially connected to a concentrated brine tank 9, a concentrated brine pump 10, a primary heat exchanger 11, a secondary heat exchanger 12, a tertiary heat exchanger 13 and a solid-liquid separator 14 through a low-nitrate brine pipe a17, the upper end of the solid-liquid separator 14 is connected to a low-nitrate brine tank 15 through a low-nitrate brine pipe b18, the low-nitrate brine tank 15 is connected to a secondary heat exchanger 12, the low-nitrate brine pipe b18 is fixedly connected with a low-nitrate brine pump 16, and the low-nitrate brine tank 19 is connected after heat exchange; the other side of the membrane component 8 is connected with a permeate brine tank 19 through a permeate brine pipe a; the permeate brine tank 19 is connected to the permeate brine heat exchanger 4 through a permeate brine pipe b22, a permeate brine pump 21, a communicating pipe 23, a heat exchange water supply valve 25 and a recovery pipe 24 are sequentially and fixedly connected to the permeate brine pipe b22, the communicating pipe 23 is provided with a communicating valve 26, and the recovery pipe 24 is provided with a recovery valve 27; the front pipeline of the activated carbon tower 5 is provided with a front PH online detector 28 and a front free chlorine online detector 29, the rear pipeline of the activated carbon tower 5 is provided with a temperature remote transmission 30, a rear PH online detector 31 and a rear free chlorine online detector 32, and the temperature remote transmission 30, the rear PH online detector 31 and the rear free chlorine online detector 32 are electrically connected with the recovery valve 27.
Further, the brine buffer tank 1 is connected with a brine feed pipe 33, an acid adding pipe 34 and a sodium sulfite adding pipe 35, and is respectively provided with a control valve.
Further, the brine buffer pump 2 and the high-pressure pump 7 are provided with frequency converters, and the flow and the pressure of the brine in the system are effectively controlled through the frequency conversion controllers.
Further, the membrane module 8 is provided with a flushing pipe 36, and flushing water is pure water or sterilizing water.
Further, the primary heat exchanger 11, the secondary heat exchanger 12 and the tertiary heat exchanger 13 are respectively connected with a circulating water pipeline, a low-nitrate water pipeline and a calcium chloride salt water pipeline, the number of the secondary heat exchangers 12 can be at least 1, and when the cooling capacity is insufficient, a plurality of the secondary heat exchangers can be connected in series.
The working principle of the system is as follows: the fresh brine from the ionic membrane dechlorination is subjected to a pretreatment unit, a membrane filtration unit and a freezing unit, wherein the pretreatment aims at providing qualified brine for the membrane assembly, and free chlorine in the brine is removed by adjusting the temperature and the pH value of the brine and adsorbing the brine by activated carbon.
During the production process, high-purity hydrochloric acid is added, and the following reactions occur:
OH - +HCl - →Cl - +H20
in the production process, the activated carbon reacts with free chlorine as follows:
3HCIO+C*→>H 2 CO 3 +HCl+2CI -
the treated brine is firstly crushed and filtered by the cartridge filter before being sent into the membrane component and the high-pressure pump, the membrane is prevented from being blocked, the brine treated by the preprocessor is separated by sulfate radicals through the membrane component under the action of the high-pressure pump, so that concentrated solution and permeate are obtained, the permeate exchanges heat and returns to the water distribution tank after utilizing cold energy, the concentrated solution brine enters the rear refrigeration unit for solid-liquid separation, sulfate radicals are separated from brine in the form of sodium sulfate decahydrate, and the low-nitrate brine finally returns to the primary brine distribution tank after utilizing cold energy by heat.
The working process of the system comprises the following steps: the dilute brine conveyed by the ionic membrane enters a brine buffer tank 1, hydrochloric acid and sodium sulfite are added into the brine buffer tank 1, and the pH value and free chlorine at the outlet of an activated carbon filter are regulated; the dechlorinated brine is conveyed to the two-stage cooler through the brine buffer pump 2, the first stage is the permeate brine heat exchanger 3, the permeate brine is used as a cold source, the second stage is the circulating water cooler, and the circulating water is used as the cold source. After two-stage cooling, the residual little free chlorine in the brine mainly exists in the form of HClO, and the free chlorine is removed after entering the activated carbon tower 5. The inlet pipeline in the activated carbon tower is provided with a pre-tower PH online detector 28 and a pre-tower free chlorine online detector 29, the post-tower pipeline of the activated carbon tower 5 is provided with a temperature remote transmission 30, a post-tower PH online detector 31 and a post-tower free chlorine online detector 32, the temperature remote transmission 30, the post-tower PH online detector 31 and the post-tower free chlorine online detector 32 are electrically connected with a recovery valve 27, if any index of the temperature remote transmission 30, the post-tower PH online detector 31 and the post-tower free chlorine online detector 32 is unqualified, the recovery valve 27 is opened to recover unqualified brine to a water distribution tank, when the short-time stop is performed, the heat exchange water supply valve 25 is closed, the communication valve 26 is opened, the low-flow operation of a membrane module is ensured by using the permeated brine as circulating liquid, the frequent start-stop of the membrane module is avoided, the service life is shortened, the state of the valve is recovered after the fault removal, and the system is normally operated. When the vehicle is parked for a long time, pure water or sterilizing water is injected into the membrane module through the flushing pipe 36, gas is discharged, and after the membrane shell and related pipelines are filled with salt water or pure water, the gas is prevented from entering the membrane module 8 to ensure that the sterilizing liquid is filled with the membrane module; under normal conditions, the monitoring indexes are qualified, brine from the activated carbon tower enters a cartridge filter 6, a small amount of finely-divided activated carbon particles carried in the filtered brine are removed, and then the fresh brine enters a membrane component 8 through a high-pressure pump 7; after the light brine is filtered, the sulfate radical of the permeate brine reaches a control index, and the permeate brine enters a permeate brine pipe a and flows into a permeate brine tank 19; concentrated brine flows into the concentrated brine tank 9 through the concentrated brine pipe 37, is sent into the primary cooler 11, the secondary cooler 12 and the tertiary cooler 13 through the concentrated brine pump 10, is sent into the solid-liquid separator 14 after the brine temperature is qualified, sulfate ions are separated from brine in the form of sodium sulfate decahydrate, low-nitrate brine overflows to the low-nitrate brine tank 15 from the upper part of the solid-liquid separator, is sent to the secondary cooler 12 by the low-nitrate water pump 16, exchanges heat and utilizes cold energy, and finally returns to the primary brine water distribution tank.
The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.
Claims (5)
1. The system for removing sulfate ions in brine in chlor-alkali production is characterized in that: the device comprises a brine buffer tank, a brine buffer pump, a circulating water heat exchanger, a permeate brine heat exchanger, an activated carbon tower, a cartridge filter, a high-pressure pump and a membrane component which are sequentially connected, wherein one side of the membrane component is sequentially connected to a concentrated nitrate brine tank, a concentrated nitrate brine pump, a primary heat exchanger, a secondary heat exchanger, a tertiary heat exchanger and a solid-liquid separator through a concentrated nitrate brine outlet pipe, the upper end of the solid-liquid separator is connected to the low nitrate brine tank through a low nitrate brine pipe a, the low nitrate brine tank is connected to the secondary heat exchanger through a low nitrate brine pipe b, the low nitrate brine pump is fixedly connected to a low nitrate brine pipeline, and the low nitrate brine tank is connected to the permeate brine tank after heat exchange; the other side of the membrane component is connected with a permeate brine tank through a permeate brine outlet pipe; the osmotic brine tank is connected to the osmotic brine heat exchanger through an osmotic brine pipe b, and a pipeline is sequentially and fixedly connected with an osmotic brine pump, a communicating pipe, a heat exchange water supply valve and a recovery pipe, wherein the communicating pipe is provided with a communicating valve, and the recovery pipe is provided with a recovery valve; the active carbon tower front pipeline is provided with a tower front PH on-line detector and a tower front free chlorine on-line detector, the active carbon tower rear pipeline is provided with a temperature remote transmission, a tower rear PH on-line detector and a tower rear free chlorine on-line detector, and the temperature remote transmission, the tower rear PH on-line detector and the tower rear free chlorine on-line detector are electrically connected with a recovery valve.
2. The system for removing brine sulfate ions in chlor-alkali production according to claim 1, wherein the brine buffer tank is connected with a brine feeding pipe, an acid adding pipe and a sodium sulfite adding pipe, and control valves are respectively arranged.
3. The system for removing brine sulfate ions in chlor-alkali production according to claim 1, wherein the brine buffer pump and the high-pressure pump are provided with frequency converters, and the brine flow and the brine pressure of the system are effectively controlled by the frequency conversion controllers.
4. The system for removing sulfate ions in brine in the production of chlor-alkali according to claim 1, wherein the membrane module is provided with a flushing pipe, and the flushing water is pure water or sterilizing water.
5. The system for removing sulfate ions from brine in chlor-alkali production according to claim 1, further characterized in that the primary heat exchanger, the secondary heat exchanger and the tertiary heat exchanger are respectively connected with a circulating water pipeline, a low-nitrate water pipeline and a calcium chloride salt water pipeline, the number of the secondary heat exchangers is at least 1, and when the cooling capacity is insufficient, a plurality of the secondary heat exchangers can be connected in series.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320009279.4U CN219239460U (en) | 2023-01-04 | 2023-01-04 | Brine sulfate ion removal system in chlor-alkali production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320009279.4U CN219239460U (en) | 2023-01-04 | 2023-01-04 | Brine sulfate ion removal system in chlor-alkali production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219239460U true CN219239460U (en) | 2023-06-23 |
Family
ID=86807905
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202320009279.4U Active CN219239460U (en) | 2023-01-04 | 2023-01-04 | Brine sulfate ion removal system in chlor-alkali production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219239460U (en) |
-
2023
- 2023-01-04 CN CN202320009279.4U patent/CN219239460U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110065958B (en) | Method for preparing lithium hydroxide by treating salt lake brine through integrated selective electrodialysis and selective bipolar membrane electrodialysis | |
| CN212403781U (en) | But resource recovery's desulfurization effluent disposal system | |
| CN111517533A (en) | Thermal power plant desulfurization wastewater resource utilization system and method with low reagent consumption | |
| CN111268834A (en) | Desulfurization wastewater treatment system and method capable of recycling resources | |
| CN114262035B (en) | Continuous electric desalting system and method | |
| CN109231371A (en) | A kind of ternary precursor wastewater electrolytic treatment system and its processing method | |
| CN110917882A (en) | Four-channel electrodialysis device for extracting lithium from salt lake and method for extracting lithium from salt lake | |
| CN103274550B (en) | Brine impurity removal method in sodium chlorate production technology | |
| CN210481411U (en) | Separation system for preparing xylose | |
| CN219239460U (en) | Brine sulfate ion removal system in chlor-alkali production | |
| CN113026003A (en) | Reduction regeneration method for chemical nickel plating aging solution | |
| CN111170519A (en) | Treatment process and treatment system for desulfurization wastewater | |
| CN204311142U (en) | A kind of light salt brine replaces the device of part refined brine electrolysis caustic soda | |
| CN211972013U (en) | Device for removing sodium sulfate in coal chemical industry byproduct sodium chloride saturated solution | |
| CN216764349U (en) | Get rid of automation equipment of calcium ion in lithium hydroxide solution | |
| CN110436679A (en) | The devices and methods therefor of lithium carbonate wash water comprehensive utilization of resources | |
| CN113401924B (en) | Brine refining method | |
| CN111362471A (en) | Device for removing sodium sulfate in coal chemical industry byproduct sodium chloride saturated solution | |
| CN211111482U (en) | Lithium carbonate washing water resource comprehensive utilization's device | |
| CN114409160A (en) | Treatment method for preparing high-purity basic magnesium chloride whisker by removing ions from desulfurized slurry and recycling concentrated solution | |
| CN208829465U (en) | A kind of device of twin flue embrane method denitration | |
| CN202297195U (en) | Refrigeration denitration device for brine rich in nitro | |
| CN217868479U (en) | High-temperature brine denitration device | |
| CN209652063U (en) | A kind of processing system of high temperature film method for removing sulfate ion | |
| CN203668163U (en) | Device for nitrate removal by membrane method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |