CN216236063U - Sodium bromide apparatus for producing - Google Patents
Sodium bromide apparatus for producing Download PDFInfo
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- CN216236063U CN216236063U CN202122888537.4U CN202122888537U CN216236063U CN 216236063 U CN216236063 U CN 216236063U CN 202122888537 U CN202122888537 U CN 202122888537U CN 216236063 U CN216236063 U CN 216236063U
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Abstract
The utility model discloses a sodium bromide production device, wherein the top of a blow-out tower is communicated with an absorption tower through a pipeline; the absorption tower is respectively communicated with a sodium formate preparation tank and a sodium hydroxide storage tank through pipelines, the absorption tower is communicated with an absorption liquid storage tank through a pipeline, the absorption liquid storage tank is communicated with a refining kettle through a pipeline, the refining kettle is communicated with an evaporator through a pipeline, and the evaporator is communicated with a centrifuge through a pipeline. The production cost is greatly reduced by taking the brine as the raw material, the safety of the whole operation process is higher, the obtained product has two types of liquid and solid, different customer requirements are met, and the finally obtained product has high purity.
Description
Technical Field
The utility model relates to the technical field of sodium bromide production, in particular to a sodium bromide production device.
Background
At present, the production of sodium bromide generally adopts a method of neutralizing hydrobromic acid and sodium hydroxide or absorbing bromine by sodium hydroxide for production, and the two methods generate sodium bromate as an impurity, so that the quality of a sodium bromide product is reduced, the post-treatment is difficult, and the production cost is increased. Meanwhile, hydrobromic acid is an aqueous solution of hydrogen bromide, is stronger in acidity than hydrochloric acid but weaker in acidity than hydroiodic acid, and is one of the strongest inorganic acids, so that operators face greater potential safety hazards when the hydrobromic acid is used as a raw material to produce sodium bromide.
Disclosure of Invention
The technical problem to be solved by the utility model is as follows: aiming at the defects in the prior art, the sodium bromide production device is provided, the safety of the production process is good, and the obtained product has high purity and low production cost.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
a sodium bromide production device comprises an oxidation tower which is respectively communicated with a chlorine gas inlet pipeline and a brine inlet pipeline, wherein the oxidation tower is communicated with a blow-out tower through a pipeline, the lower part of the blow-out tower is communicated with an air inlet pipeline, and the top of the blow-out tower is communicated with an absorption tower through a pipeline;
the absorption tower is communicated with a sodium formate preparation tank and a sodium hydroxide storage tank through pipelines respectively, the absorption tower is communicated with an absorption liquid storage tank through a pipeline, the absorption liquid storage tank is communicated with a refining kettle through a pipeline, the refining kettle is communicated with an evaporator through a pipeline, the evaporator is communicated with a centrifugal machine through a pipeline, and a liquid phase outlet and a solid phase outlet of the centrifugal machine are communicated to the liquid sodium bromide storage tank and the solid sodium bromide storage tank through pipelines respectively.
As an improved technical scheme, the chlorine gas inlet pipeline and the brine feeding pipeline are communicated to a mixed feeding pipeline respectively, a static mixer is arranged on the mixed feeding pipeline, and the static mixer is communicated to the oxidation tower through a pipeline.
As an improved technical scheme, a plurality of feeding spray heads are arranged in the blow-out tower.
As an improved technical scheme, the absorption tower comprises a primary absorption tower, a secondary absorption tower and a tertiary absorption tower which are sequentially communicated through a pipeline, the primary absorption tower is communicated with the top of the blow-out tower through a pipeline, the top of the tertiary absorption tower is communicated to an air inlet of a fan through a pipeline, and an air outlet of the fan is communicated to the air inlet pipeline;
and the primary absorption tower, the secondary absorption tower and the tertiary absorption tower are all provided with absorption liquid circulating pumps.
As an improved technical scheme, the sodium hydroxide storage tank is communicated to the primary absorption tower through a pipeline, the sodium formate preparation tank is communicated to the tertiary absorption tower through a sodium formate feeding pump, a first overflow pipeline is arranged between the tertiary absorption tower and the secondary absorption tower, a second overflow pipeline is arranged between the secondary absorption tower and the primary absorption tower, and the first overflow pipeline and the second overflow pipeline enable materials in the sodium formate preparation tank to overflow from the tertiary absorption tower to the secondary absorption tower and then overflow to the primary absorption tower;
the first-stage absorption tower is communicated to the absorption liquid storage tank through an absorption liquid overflow pipeline.
As an improved technical scheme, a refined liquid storage tank is arranged between the refining kettle and the evaporator.
As a preferred technical scheme, the evaporator comprises a first-effect evaporator and a second-effect evaporator, the first-effect evaporator comprises a first-effect evaporation chamber, a first-effect circulating pump and a first-effect heater which are communicated through a pipeline, the second-effect evaporator comprises a second-effect evaporation chamber, a second-effect circulating pump and a second-effect heater which are communicated through a pipeline, a bottom discharge port of the first-effect evaporation chamber is communicated to the second-effect evaporation chamber through a first-effect material transfer pump, and a bottom discharge port of the second-effect evaporation chamber is communicated to the centrifuge through a second-effect material transfer pump;
the top of the first-effect evaporation chamber is communicated to the second-effect heater through a pipeline, the top of the second-effect evaporation chamber is communicated to a condenser through a pipeline, and the condenser is communicated to a vacuum pump through a pipeline.
As a preferable technical scheme, the two-effect material transferring pump is communicated with a cyclone through a pipeline, the top of the cyclone is communicated with the two-effect evaporation chamber through a pipeline, the bottom of the cyclone is communicated with the thick kettle through a pipeline, and the thick kettle is communicated with the centrifugal machine through a pipeline.
As a preferable technical scheme, a liquid phase outlet of the centrifuge is communicated to a mother liquor tank through a pipeline, and the mother liquor tank is communicated to a liquid sodium bromide storage tank through a pipeline.
As a preferred technical scheme, the refining kettle is provided with an ammonia water feeding pipeline.
Due to the adoption of the technical scheme, the utility model has the beneficial effects that:
the utility model relates to a sodium bromide production device, which comprises an oxidation tower respectively communicated with a chlorine gas inlet pipeline and a brine feeding pipeline, wherein the oxidation tower is communicated to a blow-out tower through a pipeline; the absorption tower is communicated with a sodium formate preparation tank and a sodium hydroxide storage tank through pipelines respectively, the absorption tower is communicated with an absorption liquid storage tank through a pipeline, the absorption liquid storage tank is communicated with a refining kettle through a pipeline, the refining kettle is communicated with an evaporator through a pipeline, the evaporator is communicated with a centrifugal machine through a pipeline, and a liquid phase outlet and a solid phase outlet of the centrifugal machine are communicated to the liquid sodium bromide storage tank and the solid sodium bromide storage tank through pipelines respectively. The method comprises the steps of spraying an oxidation liquid formed by the reaction of chlorine and brine in an oxidation tower from the top of a blowing tower downwards, enabling the oxidation liquid to be in countercurrent contact with air blown from a fan at the bottom of the blowing tower, blowing bromine in the oxidation liquid out of the oxidation liquid and entering an absorption tower to be absorbed by a sodium formate solution to generate a mixed solution of sodium bromide and hydrobromic acid, then introducing sodium hydroxide to neutralize the hydrobromic acid to obtain sodium bromide, and further forming a sodium bromide absorption liquid in the absorption tower, wherein the sodium bromide absorption liquid is evaporated by an evaporator and subjected to centrifugal action to finally obtain liquid sodium bromide and solid sodium bromide. The production cost is greatly reduced by taking the brine as the raw material, the safety of the whole operation process is higher, the obtained product has two types of liquid and solid, different customer requirements are met, and the finally obtained product has high purity.
The chlorine gas inlet pipeline and the brine feeding pipeline are respectively communicated to a mixed feeding pipeline, a static mixer is arranged on the mixed feeding pipeline, and the static mixer is communicated to the oxidation tower through a pipeline. And (3) premixing and finally fully mixing chlorine and bromide ions in an oxidation tower through a static mixer to obtain bromine.
A plurality of feeding spray heads are arranged in the blow-out tower. The oxidizing liquid is uniformly dispersed and falls down from the top of the blowing tower through the feeding nozzles, so that the bromine can be blown out by air better, the waste of raw materials is avoided, and the yield is improved.
The absorption tower comprises a primary absorption tower, a secondary absorption tower and a tertiary absorption tower which are sequentially communicated through a pipeline, the primary absorption tower is communicated with the top of the blow-out tower through a pipeline, the top of the tertiary absorption tower is communicated to an air inlet of a fan through a pipeline, and an air outlet of the fan is communicated to the air inlet pipeline; and the primary absorption tower, the secondary absorption tower and the tertiary absorption tower are all provided with absorption liquid circulating pumps. Through tertiary absorption, can thoroughly catch the bromine in the air, the raw materials high-usage has improved the yield, has also prevented simultaneously that unabsorbed bromine from spilling over to cause environmental pollution in the air. In addition, the absorption tower can be pumped by arranging the fan, and the blow-out tower can be supplied with air, so that the equipment is fully utilized.
The sodium hydroxide storage tank is communicated to the primary absorption tower through a pipeline, the sodium formate preparation tank is communicated to the tertiary absorption tower through a sodium formate feed pump, a first overflow pipeline is arranged between the tertiary absorption tower and the secondary absorption tower, a second overflow pipeline is arranged between the secondary absorption tower and the primary absorption tower, and the first overflow pipeline and the second overflow pipeline enable materials in the sodium formate preparation tank to overflow from the tertiary absorption tower to the secondary absorption tower and then overflow to the primary absorption tower; the first-stage absorption tower is communicated to the absorption liquid storage tank through an absorption liquid overflow pipeline. The index of the material entering the subsequent refining process can be controlled by controlling the index of the absorption liquid in the primary absorption tower, the control is simple, in addition, the transfer of the absorption liquid from the absorption tower to the absorption liquid storage tank is realized through the absorption liquid overflow pipeline, and the energy is saved.
Refined cauldron with be equipped with the refined liquid storage tank between the evaporimeter, can carry out parameter monitoring to the material in the refined liquid storage tank, make the material index that gets into the evaporimeter unanimous and reasonable, be favorable to improving the quality of product.
The evaporator comprises a first-effect evaporator and a second-effect evaporator, the first-effect evaporator comprises a first-effect evaporation chamber, a first-effect circulating pump and a first-effect heater which are communicated through a pipeline, the second-effect evaporator comprises a second-effect evaporation chamber, a second-effect circulating pump and a second-effect heater which are communicated through a pipeline, a bottom discharge port of the first-effect evaporation chamber is communicated to the second-effect evaporation chamber through a first-effect material transferring pump, and a bottom discharge port of the second-effect evaporation chamber is communicated to the centrifugal machine through a second-effect material transferring pump; the top of the first-effect evaporation chamber is communicated to the second-effect heater through a pipeline, the top of the second-effect evaporation chamber is communicated to a condenser through a pipeline, and the condenser is communicated to a vacuum pump through a pipeline. The material composition after the second-stage evaporation is more single, the purity of the finally obtained product is higher, the evaporation efficiency is improved, and the production time is saved.
The double-effect material transferring pump is communicated with a cyclone through a pipeline, the top of the cyclone is communicated to the double-effect evaporation chamber through a pipeline, the bottom of the cyclone is communicated to the thick kettle through a pipeline, and the thick kettle is communicated to the centrifugal machine through a pipeline. The gas carried by the evaporated material and not captured by the condenser enters the two-effect evaporation chamber again after passing through the cyclone, and is captured by the condenser again, meanwhile, the liquid is buffered in the thick kettle for temperature control, and finally enters the centrifuge, so that the temperature control of the material in the centrifuge is facilitated, and the centrifuge efficiency is improved.
A liquid phase outlet of the centrifuge is communicated to a mother liquor tank through a pipeline, and the mother liquor tank is communicated to a liquid sodium bromide storage tank through a pipeline. The mother liquor jar is kept in the material, carries out the index control through carrying out the material to the mother liquor jar in, guarantees the quality of the product that gets into liquid sodium bromide storage tank.
The refining kettle is provided with an ammonia water feeding pipeline, free bromine molecules are reduced through ammonia water, brown in the product is removed, and the transparency of the product is improved.
Drawings
The utility model is further illustrated with reference to the following figures and examples.
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
wherein: 1. a chlorine gas inlet pipe; 2. a brine feed pipeline; 3. an oxidation tower; 4. blowing out of the tower; 5. an air intake duct; 6. a sodium formate preparation tank; 7. a sodium hydroxide storage tank; 8. an absorption liquid storage tank; 9. a refining kettle; 10. a centrifuge; 11. a liquid sodium bromide storage tank; 12. a solid sodium bromide storage tank; 13. a mixed feed conduit; 14. a static mixer; 15. a feed nozzle; 16. a first-stage absorption tower; 17. a secondary absorption tower; 18. a third stage absorption tower; 19. an absorption liquid circulating pump; 20. a sodium formate feeding pump; 21. a first overflow conduit; 22. a second overflow conduit; 23. a refined liquid storage tank; 24. an absorption liquid overflow conduit; 25. a first-effect evaporation chamber; 26. a one-effect circulation pump; 27. a primary heater; 28. a two-effect evaporation chamber; 29. a two-effect circulating pump; 30. a dual-effect heater; 31. a effect transfer pump; 32. a two-effect material transfer pump; 33. a condenser; 34. a vacuum pump; 35. a swirler; 36. a thick kettle; 37. a mother liquor tank; 38. an ammonia water feed line; 39. a fan; 40. steam; 41. process water; 42. and blowing the waste brine.
Detailed Description
The utility model is further illustrated below with reference to the figures and examples.
As shown in fig. 1, a sodium bromide production device comprises an oxidation tower 3 respectively communicated with a chlorine gas inlet pipeline 1 and a brine inlet pipeline 2, wherein the oxidation tower 3 is communicated with a blow-out tower 4 through a pipeline, the lower part of the blow-out tower 4 is communicated with an air inlet pipeline 5, and the top of the blow-out tower 4 is communicated with an absorption tower through a pipeline; the absorption tower is respectively communicated with a sodium formate preparation tank 6 and a sodium hydroxide storage tank 7 through pipelines, the sodium formate preparation tank 6 is communicated with process water 41, the absorption tower is communicated with an absorption liquid storage tank 8 through a pipeline, the absorption liquid storage tank 8 is communicated with a refining kettle 9 through a pipeline, the refining kettle 9 is communicated with an evaporator through a pipeline, the evaporator is communicated with a centrifugal machine 10 through a pipeline, and a liquid phase outlet and a solid phase outlet of the centrifugal machine 10 are respectively communicated with a liquid sodium bromide storage tank 11 and a solid sodium bromide storage tank 12 through pipelines. The oxidizing solution formed by the reaction of chlorine and brine in the oxidation tower 3 is sprayed from the top of the blowing tower 4 and flows down, and is in countercurrent contact with the air blown from the fan 39 at the bottom of the blowing tower 4, bromine in the oxidizing solution is blown out and enters the absorption tower to be absorbed by the sodium formate solution to generate a mixed solution of sodium bromide and hydrobromic acid, then sodium hydroxide is introduced to neutralize the hydrobromic acid to obtain sodium bromide, so that a sodium bromide absorption solution is formed in the absorption tower, and the sodium bromide absorption solution is evaporated by an evaporator and centrifuged to finally obtain liquid sodium bromide and solid sodium bromide. The production cost is greatly reduced by taking the brine as the raw material, the safety of the whole operation process is higher, the obtained product has two types of liquid and solid, different customer requirements are met, and the finally obtained product has high purity. The blown-out waste brine 42 can be backfilled to the sea, so that the waste of treatment resources is not needed, and the environment is not damaged.
Chlorine inlet line 1 with brine feed pipeline 2 communicates respectively to mixed feed pipeline 13, be equipped with static mixer 14 on the mixed feed pipeline 13, static mixer 14 communicates to oxidation tower 3 through the pipeline. Chlorine and bromide ions are premixed and finally fully mixed in the oxidation tower 3 through a static mixer 14 to obtain bromine.
A plurality of feeding nozzles 15 are arranged in the blow-out tower 4. The oxidizing liquid is uniformly dispersed and falls down from the top of the blow-off tower 4 through the feeding nozzles 15, so that bromine can be blown off by air better, the waste of raw materials is avoided, and the yield is improved.
The absorption tower comprises a primary absorption tower 16, a secondary absorption tower 17 and a tertiary absorption tower 18 which are sequentially communicated through a pipeline, the primary absorption tower 16 is communicated with the top of the blow-out tower 4 through a pipeline, the top of the tertiary absorption tower 18 is communicated to an air inlet of a fan 39 through a pipeline, and an air outlet of the fan 39 is communicated to the air inlet pipeline 5; the first-stage absorption tower 16, the second-stage absorption tower 17 and the third-stage absorption tower 18 are all provided with absorption liquid circulating pumps 19. Through tertiary absorption, can thoroughly catch the bromine in the air, the raw materials high-usage has improved the yield, has also prevented simultaneously that unabsorbed bromine from spilling over to cause environmental pollution in the air. In addition, the air suction of the absorption tower can be realized by arranging the fan 39, and the air supply of the blow-out tower 4 can be realized, so that the equipment is fully utilized.
The sodium hydroxide storage tank 7 is communicated to the primary absorption tower 16 through a pipeline, the sodium formate preparation tank 6 is communicated to the tertiary absorption tower 18 through a sodium formate feeding pump 20, a first overflow pipeline 21 is arranged between the tertiary absorption tower 18 and the secondary absorption tower 17, a second overflow pipeline 22 is arranged between the secondary absorption tower 17 and the primary absorption tower 16, and the first overflow pipeline 21 and the second overflow pipeline 22 enable materials in the sodium formate preparation tank 6 to overflow from the tertiary absorption tower 18 to the secondary absorption tower 17 and then overflow to the primary absorption tower 16; the primary absorption tower 16 is communicated to the absorption liquid storage tank 8 through an absorption liquid overflow pipeline 24. The index of the material entering the subsequent refining process can be controlled by controlling the index of the absorption liquid in the primary absorption tower 16, the control is simple, in addition, the transfer of the absorption liquid from the absorption tower to the absorption liquid storage tank 8 is realized through the absorption liquid overflow pipeline 24, and the energy is saved.
Refined cauldron 9 with be equipped with refined liquid storage tank 23 between the evaporimeter, can carry out parameter monitoring to the material in the refined liquid storage tank 23, make the material index that gets into the evaporimeter unanimous and reasonable, be favorable to improving the quality of product.
The evaporator comprises a first-effect evaporator and a second-effect evaporator, the first-effect evaporator comprises a first-effect evaporation chamber 25, a first-effect circulating pump 26 and a first-effect heater 27 which are communicated through pipelines, the first-effect heater 27 is communicated with steam 40, the second-effect evaporator comprises a second-effect evaporation chamber 28, a second-effect circulating pump 29 and a second-effect heater 30 which are communicated through pipelines, a bottom discharge port of the first-effect evaporation chamber 25 is communicated to the second-effect evaporation chamber 28 through a first-effect material transferring pump 31, and a bottom discharge port of the second-effect evaporation chamber 28 is communicated to the centrifuge 10 through a second-effect material transferring pump 32; the top of the primary-effect evaporation chamber 25 is communicated to the secondary-effect heater 30 through a pipeline, the top of the secondary-effect evaporation chamber 28 is communicated to a condenser 33 through a pipeline, and the condenser 33 is communicated to a vacuum pump 34 through a pipeline. The material composition after the second-stage evaporation is more single, the purity of the finally obtained product is higher, the evaporation efficiency is improved, and the production time is saved.
The double-effect material transferring pump 32 is communicated with a cyclone 35 through a pipeline, the top of the cyclone 35 is communicated with the double-effect evaporation chamber 28 through a pipeline, the bottom of the cyclone 35 is communicated with a thick kettle 36 through a pipeline, and the thick kettle 36 is communicated with the centrifuge 10 through a pipeline. The gas carried by the evaporated material and not captured by the condenser 33 passes through the cyclone 35 and then enters the two-effect evaporation chamber 28 again, and is captured by the condenser 33 again, meanwhile, the liquid is buffered in the thick kettle 36 for temperature control, and finally enters the centrifuge 10, so that the temperature control of the material in the centrifuge 10 is facilitated, and the centrifugal efficiency is improved.
The liquid phase outlet of the centrifuge 10 is communicated to a mother liquor tank 37 through a pipeline, and the mother liquor tank 37 is communicated to the liquid sodium bromide storage tank 11 through a pipeline. The mother liquor tank 37 is used for temporarily storing the materials, and the quality of the product entering the liquid sodium bromide storage tank 11 is guaranteed by monitoring the indexes of the materials in the mother liquor tank 37.
The refining kettle 9 is provided with an ammonia water feeding pipeline 38, free bromine molecules are reduced through ammonia water, brown in the product is removed, and the transparency of the product is improved.
The working principle of the utility model is as follows:
1. flow path of brine
Brine in the brine pond is carried brine charge-in pipeline 2 through the pump of beating brine, mix into oxidizing solution with chlorine in static mixer 14, oxidizing solution gets into the top of blowing out tower 4 through oxidation tower 3, oxidizing solution sprays and down from the top of blowing out tower 4, with the air countercurrent contact of blowing out tower 4 bottom insufflation, bromine in the oxidizing solution is blown out, oxidizing solution becomes to blow useless brine and is discharged by the tower cauldron bottom of blowing out tower 4, dropwise add caustic soda in the useless brine that blows out tower 4 exhaust, after the PH value that will blow useless brine is adjusted to the value of requirement, backfill or other processings.
2. Scheme for bromine
Bromine ions in the brine are oxidized into bromine by chlorine and enter the top of the blow-off tower 4 along with an oxidizing solution, the oxidizing solution is sprayed from the top of the blow-off tower 4 and contacts with air blown from the bottom of the blow-off tower 4 in a countercurrent manner, the bromine in the oxidizing solution is blown out and discharged from the top of the blow-off tower 4 along with the air, the bromine-containing air enters a primary absorption tower 16, the bromine in the air is absorbed by a sodium formate absorbing solution in the primary absorption tower 16 to generate a mixed solution of sodium bromide and hydrobromic acid, the bromine which is not absorbed enters a secondary absorption tower 17 along with the air, and the bromine enters a tertiary absorption tower 18 in sequence until the bromine is completely absorbed.
3. Flow path of sodium formate absorption liquid
Sodium formate absorbent with certain concentration is pumped into a third-stage absorption tower 18 at a certain flow rate, sodium formate absorption liquid is circularly sprayed by an absorption liquid circulating pump 19, incompletely absorbed bromine in a second-stage absorption tower 17 is absorbed and overflows to the second-stage absorption tower 17 by means of potential difference, the same operation is carried out in the second-stage absorption tower 17, the absorption liquid overflows to a first-stage absorption tower 16, the index of the absorption liquid in the first-stage absorption tower 16 is controlled to meet the production requirement, and the absorption liquid reaching the reaction end point overflows to an absorption liquid storage tank 8.
4. Process for refining absorption liquid
The absorbent in absorbent storage tank 8 was pumped into reactor 9 by a pump, and a predetermined amount of aqueous ammonia was added to reactor 9 to react with the free bromine in the solution to remove the free bromine.
5. Sodium bromide solution concentration and crystallization process
The refined sodium bromide clear solution is pumped into a double-effect evaporator, steam 40 is used for heating in the evaporator, the sodium bromide solution is concentrated until sodium bromide crystals are separated out, solid sodium bromide is obtained through centrifugation of a centrifuge 10, and the centrifugal mother liquor is sold as a liquid product.
It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Further, it should be understood that various changes or modifications of the present invention may be made by those skilled in the art after reading the teaching of the present invention, and such equivalents may fall within the scope of the present invention as defined in the appended claims.
Claims (10)
1. A sodium bromide apparatus for producing, its characterized in that: the device comprises an oxidation tower which is respectively communicated with a chlorine gas inlet pipeline and a brine feeding pipeline, wherein the oxidation tower is communicated with a blow-out tower through a pipeline, the lower part of the blow-out tower is communicated with an air inlet pipeline, and the top of the blow-out tower is communicated with an absorption tower through a pipeline;
the absorption tower is communicated with a sodium formate preparation tank and a sodium hydroxide storage tank through pipelines respectively, the absorption tower is communicated with an absorption liquid storage tank through a pipeline, the absorption liquid storage tank is communicated with a refining kettle through a pipeline, the refining kettle is communicated with an evaporator through a pipeline, the evaporator is communicated with a centrifugal machine through a pipeline, and a liquid phase outlet and a solid phase outlet of the centrifugal machine are communicated to the liquid sodium bromide storage tank and the solid sodium bromide storage tank through pipelines respectively.
2. A sodium bromide production plant as claimed in claim 1, wherein: the chlorine gas inlet pipeline with brine feed pipeline communicates respectively to mixing feed pipeline, be equipped with static mixer on the mixing feed pipeline, static mixer communicates to the oxidation tower through the pipeline.
3. A sodium bromide production plant as claimed in claim 1, wherein: a plurality of feeding spray heads are arranged in the blow-out tower.
4. A sodium bromide production plant as claimed in claim 1, wherein: the absorption tower comprises a primary absorption tower, a secondary absorption tower and a tertiary absorption tower which are sequentially communicated through a pipeline, the primary absorption tower is communicated with the top of the blow-out tower through a pipeline, the top of the tertiary absorption tower is communicated to an air inlet of a fan through a pipeline, and an air outlet of the fan is communicated to the air inlet pipeline;
and the primary absorption tower, the secondary absorption tower and the tertiary absorption tower are all provided with absorption liquid circulating pumps.
5. The sodium bromide production apparatus as claimed in claim 4, wherein: the sodium hydroxide storage tank is communicated to the primary absorption tower through a pipeline, the sodium formate preparation tank is communicated to the tertiary absorption tower through a sodium formate feed pump, a first overflow pipeline is arranged between the tertiary absorption tower and the secondary absorption tower, a second overflow pipeline is arranged between the secondary absorption tower and the primary absorption tower, and the first overflow pipeline and the second overflow pipeline enable materials in the sodium formate preparation tank to overflow from the tertiary absorption tower to the secondary absorption tower and then overflow to the primary absorption tower;
the first-stage absorption tower is communicated to the absorption liquid storage tank through an absorption liquid overflow pipeline.
6. A sodium bromide production plant as claimed in claim 1, wherein: a refined liquid storage tank is arranged between the refining kettle and the evaporator.
7. A sodium bromide production plant as claimed in claim 1, wherein: the evaporator comprises a first-effect evaporator and a second-effect evaporator, the first-effect evaporator comprises a first-effect evaporation chamber, a first-effect circulating pump and a first-effect heater which are communicated through a pipeline, the second-effect evaporator comprises a second-effect evaporation chamber, a second-effect circulating pump and a second-effect heater which are communicated through a pipeline, a bottom discharge port of the first-effect evaporation chamber is communicated to the second-effect evaporation chamber through a first-effect material transferring pump, and a bottom discharge port of the second-effect evaporation chamber is communicated to the centrifugal machine through a second-effect material transferring pump;
the top of the first-effect evaporation chamber is communicated to the second-effect heater through a pipeline, the top of the second-effect evaporation chamber is communicated to a condenser through a pipeline, and the condenser is communicated to a vacuum pump through a pipeline.
8. The sodium bromide production apparatus as claimed in claim 7, wherein: the double-effect material transferring pump is communicated with a cyclone through a pipeline, the top of the cyclone is communicated to the double-effect evaporation chamber through a pipeline, the bottom of the cyclone is communicated to the thick kettle through a pipeline, and the thick kettle is communicated to the centrifugal machine through a pipeline.
9. A sodium bromide production plant as claimed in claim 1, wherein: a liquid phase outlet of the centrifuge is communicated to a mother liquor tank through a pipeline, and the mother liquor tank is communicated to a liquid sodium bromide storage tank through a pipeline.
10. A sodium bromide production plant as claimed in claim 1, wherein: and the refining kettle is provided with an ammonia water feeding pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122888537.4U CN216236063U (en) | 2021-11-22 | 2021-11-22 | Sodium bromide apparatus for producing |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122888537.4U CN216236063U (en) | 2021-11-22 | 2021-11-22 | Sodium bromide apparatus for producing |
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| CN216236063U true CN216236063U (en) | 2022-04-08 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114436293A (en) * | 2022-04-12 | 2022-05-06 | 天津长芦汉沽盐场有限责任公司 | Method for directly producing sodium bromide from low-concentration brine |
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2021
- 2021-11-22 CN CN202122888537.4U patent/CN216236063U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114436293A (en) * | 2022-04-12 | 2022-05-06 | 天津长芦汉沽盐场有限责任公司 | Method for directly producing sodium bromide from low-concentration brine |
| CN114436293B (en) * | 2022-04-12 | 2022-07-01 | 天津长芦汉沽盐场有限责任公司 | Method for directly producing sodium bromide from low-concentration brine |
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