CN219652757U - Processing system of titanium white powder trade embrane method denitration - Google Patents
Processing system of titanium white powder trade embrane method denitration Download PDFInfo
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- CN219652757U CN219652757U CN202321154528.5U CN202321154528U CN219652757U CN 219652757 U CN219652757 U CN 219652757U CN 202321154528 U CN202321154528 U CN 202321154528U CN 219652757 U CN219652757 U CN 219652757U
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- Prior art keywords
- brine
- tank
- dilute brine
- membrane
- buffer tank
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- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 30
- 235000010215 titanium dioxide Nutrition 0.000 title claims description 17
- 239000000843 powder Substances 0.000 title claims description 6
- 239000012267 brine Substances 0.000 claims abstract description 92
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 92
- 239000012528 membrane Substances 0.000 claims abstract description 64
- 238000004140 cleaning Methods 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 31
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims abstract description 28
- 238000001914 filtration Methods 0.000 claims abstract description 21
- 235000010265 sodium sulphite Nutrition 0.000 claims abstract description 14
- 239000000243 solution Substances 0.000 claims abstract description 14
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 13
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000004408 titanium dioxide Substances 0.000 claims abstract description 12
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- 238000010790 dilution Methods 0.000 claims abstract description 10
- 239000012895 dilution Substances 0.000 claims abstract description 10
- 238000006298 dechlorination reaction Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 27
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 24
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 11
- 239000000460 chlorine Substances 0.000 claims description 11
- 229910052801 chlorine Inorganic materials 0.000 claims description 11
- 238000007865 diluting Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 4
- 238000001728 nano-filtration Methods 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims 1
- 230000000149 penetrating effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 7
- 230000000903 blocking effect Effects 0.000 abstract description 3
- 230000029087 digestion Effects 0.000 abstract description 2
- 238000004090 dissolution Methods 0.000 abstract description 2
- 239000012466 permeate Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 3
- 238000001514 detection method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000010446 mirabilite Substances 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a membrane method denitration treatment system in the titanium dioxide industry, which comprises a pretreatment module and a membrane separation module, wherein the pretreatment module comprises a dilute brine buffer tank and a sodium sulfite dilution tank communicated with the dilute brine buffer tank; the dilute brine buffer tank is connected with the feeding buffer tank through a brine pipeline; the brine pipeline is sequentially provided with a primary dilute brine cooler and a secondary dilute brine cooler, and two cartridge filters which are arranged in parallel; the dilute brine in the feeding buffer tank enters a membrane separation module through a booster pump; the outlet end of the membrane separation module is respectively connected with a lean nitrate solution tank and a rich digestion solution tank, and the membrane separation module is also connected with an auxiliary cleaning module; the utility model not only effectively recovers the sulfate radicals enriched in the dechlorination and salt dissolution processes of the dilute brine, is convenient for secondary utilization, but also adds the auxiliary cleaning module, can timely clean the filtering membrane components with scaling and blocking conditions, greatly improves the filtering effect and saves the cost.
Description
Technical Field
The utility model relates to the technical field of brine denitration equipment, in particular to a membrane method denitration treatment system in the titanium dioxide industry.
Background
The brine denitration method needs to adopt a membrane filtration technology to carry out accurate and efficient denitration, generally comprises a pretreatment unit and a membrane separation unit, but in the process of using brine to remove the denitration, a plurality of free chlorine which can damage a filtering membrane is involved in the dilute brine after chlorine removal treatment, a certain amount of sodium sulfite is generally added to remove the free chlorine in the dilute brine during the dilute brine denitration, so that the PH value of the dilute brine reaches a required range, the pretreatment operation is completed, and then the dilute brine reaching the standard is placed into the membrane separation unit to be filtered, and the mirabilite crystal is obtained after freezing treatment.
But the concentration of sulfate radical can be continuously increased in the removal process, and the sulfate radical can be rapidly accumulated in the salt dissolving process, so that the enrichment of the sulfate radical can lead to the damage of a filter membrane of a membrane separation module, thereby reducing the denitration efficiency, and simultaneously, a large amount of sulfate radical in the denitration process can not be effectively utilized, thereby wasting the resource cost.
In addition, the condition that scaling and blockage appear in the filtering membrane easily in the membrane separation process, the clearance of filtering membrane can not be accomplished in time to current denitration technique, leads to the filter effect to reduce, needs often to change filtering membrane subassembly, and the cost is higher.
Disclosure of Invention
The technical problem to be solved by the utility model is to provide the membrane method denitration treatment system for the titanium dioxide industry, which can effectively recover sulfate radicals in the membrane separation module on the premise of precisely denitration, clean the filtering membrane in time, improve the filtering effect and save the cost.
In order to solve the technical problems, the technical scheme adopted by the utility model is as follows.
The membrane method denitration treatment system in the titanium dioxide industry comprises a pretreatment module and a membrane separation module, wherein the pretreatment module comprises a dilute brine buffer tank containing dilute brine after dechlorination treatment and a sodium sulfite dilution tank which is communicated with the dilute brine buffer tank and is used for effectively removing free chlorine in the dilute brine; the dilute brine buffer tank is connected with a feed buffer tank for storing dilute brine through a brine pipeline, and a dilute brine pump is arranged at the outlet of the dilute brine buffer tank; the brine pipeline is sequentially provided with a primary dilute brine cooler, a secondary dilute brine cooler and two security filters which are arranged in parallel, wherein the primary dilute brine cooler and the secondary dilute brine cooler have a cooling effect; a sodium sulfite metering pump is arranged at the outlet of the sodium sulfite dilution tank; the dilute brine in the feeding buffer tank enters a membrane separation module through a booster pump; the membrane separation module adopts a three-section nanofiltration series process, and 5 membrane elements are arranged in each membrane shell; the outlet end of the membrane separation module is respectively connected with the lean nitrate solution tank and the rich digestion solution tank, and the membrane separation module is also connected with an auxiliary cleaning module for circularly cleaning the filtering membrane.
Above-mentioned titanium white powder trade embrane method denitration processing system, the brine pipeline that is close to the fresh brine pump communicates with the hydrochloric acid diluting tank of regulation fresh brine pH value, and the exit of hydrochloric acid diluting tank is provided with the hydrochloric acid metering pump.
Above-mentioned titanium white powder trade embrane method denitration processing system is provided with the pH strapping table that detects the fresh brine pH value and detects the ORP strapping table of free chlorine content in the fresh brine respectively on the brine pipeline that is close to feeding buffer tank one side.
According to the treatment system for removing the nitrate by the membrane method in the titanium dioxide industry, the auxiliary cleaning module comprises the cleaning liquid tank which forms a circulating closed cleaning route through the liquid inlet pipe, the liquid outlet pipe and the membrane separation module, and the outlet end of the cleaning liquid tank is provided with the cleaning liquid pump; the liquid inlet pipe is provided with a cleaning filter for finely filtering the recovered cleaning liquid.
Above-mentioned titanium white powder trade embrane method denitration processing system, the exit end of lean in the liquid tank is provided with lean in the liquid pump of nitre, and the connecting line of lean in the liquid tank is connected with the salt dissolving tank after the cooling of one-level weak brine cooler.
By adopting the technical scheme, the utility model has the following technical progress.
The utility model provides a membrane method denitration treatment system for the titanium dioxide industry, which not only effectively recovers sulfate radicals enriched in the dechlorination and salt dissolution processes of light brine and is convenient for secondary utilization, but also adds an auxiliary cleaning module, so that a filtering membrane component with scaling and blocking conditions can be cleaned in time, the filtering effect is greatly improved, and the cost is saved.
Drawings
FIG. 1 is a schematic diagram of a specific structure of a pretreatment module according to the present utility model;
fig. 2 is a schematic structural diagram of a membrane separation module according to the present utility model.
Wherein: 1. the system comprises a fresh brine buffer tank, a fresh brine pump, a sodium sulfite dilution tank, a sodium sulfite metering pump, a hydrochloric acid dilution tank, a hydrochloric acid metering pump, a primary fresh brine cooler, a secondary fresh brine cooler, a safety filter, a feed buffer tank, a booster pump, a salt tank, a salt dissolving tank, a lean solution pump, a lean solution tank, a membrane separation module, a cleaning solution tank, a cleaning solution pump, a cleaning solution filter, a 19.ORP meter and a 20.PH meter.
Detailed Description
The utility model will be described in further detail with reference to the drawings and the detailed description.
The membrane method denitration treatment system in the titanium dioxide industry comprises a pretreatment module and a membrane separation module 15, wherein the pretreatment module comprises a dilute brine buffer tank 1 containing dilute brine after dechlorination treatment and a sodium sulfite dilution tank 3 positioned at one side of the dilute brine tank 1, and can effectively remove free chlorine in the dilute brine; the membrane separation module 15 is connected with an auxiliary cleaning module for circularly cleaning the filtering membrane.
As shown in fig. 1, a fresh brine pump 2 is arranged at the outlet of the fresh brine buffer tank 1, the fresh brine buffer tank 1 is communicated with a feeding buffer tank 10 through a brine pipeline, and a primary fresh brine cooler 7, a secondary fresh brine cooler 8 and two security filters 9 which are arranged in parallel are sequentially arranged on the brine pipeline.
The primary and secondary brine coolers 7 and 8 are capable of cooling the dechlorinated high Wen Dan brine to a suitable temperature to ensure that the requirements for access to the membrane separation module 15 are met.
The cartridge filter 9 is capable of filtering the dilute brine after the acid treatment so as to adjust the pH of the dilute brine to an appropriate range.
The outlet of the sodium sulfite dilution tank 3 is provided with a sodium sulfite metering pump 4, and the sodium sulfite dilution tank 3 is directly communicated with the dilute brine buffer tank 1 and is used for removing free chlorine in the dechlorinated dilute brine.
The brine pipeline at the outlet of the dilute brine pump 2 is also communicated with a hydrochloric acid diluting tank 5, the outlet end of the hydrochloric acid diluting tank 5 is provided with a hydrochloric acid metering pump 6, the hydrochloric acid can adjust the pH value of the dilute brine in the feeding buffer tank 10, and meanwhile, the amount of free chlorine in the dilute brine is further reduced through electrolytic reaction.
An ORP meter 19 for detecting whether the residual amount of free chlorine in the brine reaches the standard and a pH meter 20 for detecting whether the pH value of the fresh brine is qualified are also arranged on the brine pipeline near the feed buffer tank 10, and if one detection result does not reach the detection requirement, the controller will automatically cut off the feed main valve for controlling the fresh brine to enter the membrane separation module 15.
The light salt water reaching the standard in the feeding buffer tank 10 is sent into the membrane separation module 15 for filtration through the booster pump 11, the membrane separation module 15 adopts a three-section nanofiltration series process, and 5 membrane elements are arranged in each membrane shell.
In the module, the weak brine is separated into permeate and concentrate, divalent ions are selectively intercepted by the membrane to produce the permeate lean in nitrate, the permeate flows out from each stage of filter assembly to a permeate main pipe, is measured by a flowmeter, returns to a salt dissolving water main pipe, and is cooled by a primary salt water cooler 7 to be crystallized in a salt dissolving tank 12.
The separated concentrated solution of the first section is used as the water for the next section to be continuously separated, sodium sulfate in the dilute brine is concentrated step by step through the serially connected filter components, the concentration of the sodium sulfate is continuously increased, and the concentrated solution is sent into a concentrated nitrate solution storage tank after reaching the designed concentration multiple and is periodically transported to the outside of the boundary region through a tank truck.
The auxiliary cleaning module comprises a cleaning liquid tank 16 which is connected with a liquid outlet pipe through a liquid inlet pipe and forms a circulating closed cleaning route with a membrane separation module 15, a cleaning liquid pump 17 is arranged at the outlet end of the cleaning liquid tank 16, a cleaning filter 18 is arranged on the liquid inlet pipe, and the recovered cleaning liquid can be subjected to fine filtration treatment.
The auxiliary cleaning module can regularly clean or recover the activity of the polluted and blocked or oxidized and failed nanofiltration membrane component, so that the separation efficiency and the permeation quantity of the membrane core to sulfate radicals are recovered to a normal working state.
The utility model provides a membrane method denitration treatment system for the titanium dioxide industry, which not only effectively recovers sulfate radicals enriched in the processes of dechlorination and salinization of dilute brine and is convenient for secondary utilization, but also adds an auxiliary cleaning module, so that a filtering membrane component with scaling and blocking conditions can be cleaned in time, the filtering membrane can be ensured to be restored to a normal working state, the filtering effect is greatly improved, and the cost is saved.
Claims (5)
1. The utility model provides a titanium white powder trade embrane method denitration processing system, includes pretreatment module and membrane separation module (15), its characterized in that: the pretreatment module comprises a dilute brine buffer tank (1) filled with dilute brine after dechlorination treatment and a sodium sulfite dilution tank (3) communicated with the dilute brine buffer tank (1) and used for effectively removing free chlorine in the dilute brine; the dilute brine buffer tank (1) is connected with a feeding buffer tank (10) for storing dilute brine through a brine pipeline, and a dilute brine pump (2) is arranged at the outlet of the dilute brine buffer tank (1); the brine pipeline is sequentially provided with a primary dilute brine cooler (7) and a secondary dilute brine cooler (8) which play a role in cooling, and two security filters (9) which are arranged in parallel; a sodium sulfite metering pump (4) is arranged at the outlet of the sodium sulfite dilution tank (3); the dilute brine in the feeding buffer tank (10) enters a membrane separation module (15) through a booster pump (11); the membrane separation module (15) adopts a three-section nanofiltration series process, and 5 membrane elements are arranged in each membrane shell; the outlet end of the membrane separation module (15) is respectively connected with the lean nitrate solution tank (14) and the rich solution tank, and the membrane separation module (15) is also connected with an auxiliary cleaning module for circularly cleaning the filtering membrane.
2. The system for treating the titanium dioxide industry by adopting a membrane method to remove the nitrate according to claim 1 is characterized in that: the brine pipeline close to the dilute brine pump (2) is communicated with a hydrochloric acid diluting tank (5) for adjusting the pH value of the dilute brine, and a hydrochloric acid metering pump (6) is arranged at the outlet of the hydrochloric acid diluting tank (5).
3. The system for treating the titanium dioxide industry by adopting a membrane method to remove the nitrate according to claim 1 is characterized in that: and a pH meter (20) for detecting the pH value of the fresh brine and an ORP meter (19) for detecting the free chlorine content in the fresh brine are respectively arranged on the brine pipeline close to one side of the feeding buffer tank (10).
4. The system for treating the titanium dioxide industry by adopting a membrane method to remove the nitrate according to claim 1 is characterized in that: the auxiliary cleaning module comprises a cleaning liquid tank (16) which is connected with the liquid outlet pipe and the membrane separation module (15) through a liquid inlet pipe to form a circulating closed cleaning route, and a cleaning liquid pump (17) is arranged at the outlet end of the cleaning liquid tank (16); the liquid inlet pipe is provided with a cleaning filter (18) for finely filtering the recovered cleaning liquid.
5. The system for treating the titanium dioxide industry by adopting a membrane method to remove the nitrate according to claim 1 is characterized in that: the outlet end of the lean nitrate liquid tank (14) is provided with a lean nitrate liquid pump (13), and a penetrating fluid main pipe connected with the lean nitrate liquid tank (14) is connected with the salt dissolving tank (12) after being cooled by the primary dilute brine cooler (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321154528.5U CN219652757U (en) | 2023-05-15 | 2023-05-15 | Processing system of titanium white powder trade embrane method denitration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321154528.5U CN219652757U (en) | 2023-05-15 | 2023-05-15 | Processing system of titanium white powder trade embrane method denitration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219652757U true CN219652757U (en) | 2023-09-08 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321154528.5U Active CN219652757U (en) | 2023-05-15 | 2023-05-15 | Processing system of titanium white powder trade embrane method denitration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219652757U (en) |
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2023
- 2023-05-15 CN CN202321154528.5U patent/CN219652757U/en active Active
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