CN215924417U - Production system for separating and refining sodium chloride and sodium sulfate mixed waste miscellaneous salt solution - Google Patents
Production system for separating and refining sodium chloride and sodium sulfate mixed waste miscellaneous salt solution Download PDFInfo
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Abstract
The utility model relates to a sodium chloride and sodium sulfate mixed waste miscellaneous salt solution separation refining production system, wherein a discharge port of a freezing crystallizer is sequentially connected with a freezing thickening tank through a freezing discharge pump, an outlet of the freezing thickening tank is connected with a freezing centrifuge, a centrifugal mother liquor outlet is connected with a freezing mother liquor tank, and an outlet of the freezing mother liquor tank is connected with a reflux port of the crystallizer through a freezing mother liquor pump and a freezing mother liquor pipe; the centrifugal solid phase outlet is connected with the hot melting tank, the overflow port of the hot melting tank is connected with the tube side of the hot melting heat exchanger through a hot melting circulating pump, and the tube side outlet is connected with the circulating port of the hot melting tank; an outlet of the hot melting tank is connected with a sodium sulfate evaporation crystallization unit through a hot melting discharge pump; the outlet of the freezing mother liquor pipe is also connected with the inlet of a nanofiltration membrane, the water production outlet of the nanofiltration membrane is connected with a sodium chloride evaporative crystallization unit, and the concentrated water outlet is connected with a freezing feed pool; the outlet of the freezing mother liquor pipe is also connected with a miscellaneous salt evaporation crystallization unit. The system has a wide application range, and can respectively obtain high-purity sodium chloride and sodium sulfate.
Description
Technical Field
The utility model relates to a waste miscellaneous salt treatment system, in particular to a production system for separating and refining a mixed waste miscellaneous salt solution of sodium chloride and sodium sulfate, belonging to the technical field of recycling of environmental protection resources.
Background
Most of the waste salt produced in the final water treatment process of the chemical production process is a large amount of waste salt, and most of the waste salt is treated as solid waste because the components in the waste salt are complex and contain a small amount of impurities. The waste miscellaneous salt mainly contains waste miscellaneous salt containing sodium chloride and sodium sulfate, and the ratio of the waste miscellaneous salt containing sodium chloride and sodium sulfate is more than 50% according to statistics. With the increase of environmental protection, the original sea drainage and landfill treatment mode is basically stopped due to the great pollution to the environment, and the treatment of the waste miscellaneous salt becomes a problem to be solved urgently, wherein the key is how to efficiently and stably realize the separation and refining production of the salt in the waste miscellaneous salt.
The conventional process of incineration, impurity removal and evaporative crystallization is generally adopted in the recovery process of waste miscellaneous salt containing sodium chloride and sodium sulfate, a single treatment process has certain applicability, and only the waste miscellaneous salt with a single proportion can be treated, but the sources of the waste miscellaneous salt (multiple industries such as chemical industry, medicine, pesticide, paper making and the like) are wide, and even the salt content and the components in the waste miscellaneous salt in the same industry are inconsistent. The existing waste salt treatment method comprises the following steps: high-temperature treatment: the single waste salt or the waste salt with low impurity content is subjected to pyrolysis through high-temperature treatment to remove organic matters, for example, the Chinese utility model patent with the publication number of CN207222538U adopts a high-temperature pyrolysis method to remove organic matters in industrial waste salt slag, but the energy consumption is high, the equipment is easy to corrode, and the maintenance cost is high.
② microwave treatment method: the microwave device is used for removing organic matters in the waste salt to obtain available salt, for example, the Chinese utility model patent application with the publication number of CN111847480A utilizes microwave pyrolysis to treat the sodium chloride waste salt, but the microwave treatment cost is higher, and the treated material must contain single salt which can be pyrolyzed, and the microwave device is not suitable for complex waste salt.
③ chemical treatment method: utilize chemical reaction or absorption, extraction technique to get rid of the impurity that contains in the miscellaneous salt of useless to obtain pure salt, for example the chinese utility model patent application of publication No. CN110642270A utilizes oxidation, absorption to get rid of the organic impurity in the miscellaneous salt of useless, thereby obtains the product of sodium chloride, but chemical treatment need add new material and get into miscellaneous salt of useless, has produced the secondary in the miscellaneous salt of processing useless and has admittedly useless, and the practicality of technology is less.
In conclusion, the existing waste salt treatment process generally has the problems of high energy consumption, low applicability, high maintenance cost, low quality of refined salt products and secondary solid waste treatment.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the problems in the prior art and provide a production system for separating and refining a mixed waste mixed salt solution of sodium chloride and sodium sulfate, which has a large adaptation range for the mutual proportion of sodium chloride and sodium sulfate, can respectively obtain high-purity sodium chloride and sodium sulfate, has low energy consumption and provides a new method and a new way for recycling industrial waste mixed salt.
In order to solve the technical problems, the sodium chloride and sodium sulfate mixed waste miscellaneous salt solution separation and refining production system comprises a freezing feed pool connected with a pretreatment working section, wherein an outlet of the freezing feed pool is connected with an inlet of a freezing feed pump, an outlet of the freezing feed pump is connected with an inlet of a freezing crystallizer, a discharge port of the freezing crystallizer is connected with an inlet of a freezing discharge pump, an outlet of the freezing discharge pump is connected with an inlet of a freezing thickening tank, an outlet at the bottom of the freezing thickening tank is connected with an inlet of a freezing centrifuge, a mother liquor outlet of the freezing centrifuge is connected with an inlet of a freezing mother liquor tank, an outlet of the freezing mother liquor tank is connected with an inlet of a freezing mother liquor pump, and an outlet of the freezing mother liquor pump is connected with a freezing mother liquor pipe; the first outlet of the freezing mother liquor pipe is connected with a reflux port of the freezing crystallizer; the solid phase outlet of the refrigerated centrifuge is connected with the inlet of the hot melting tank through a mirabilite pipe, the overflow outlet of the hot melting tank is connected with the tube side inlet of the hot melting heat exchanger through a hot melting circulating pump, and the tube side outlet of the hot melting heat exchanger is connected with the circulating port of the hot melting tank through a hot melting circulating liquid pipe; the bottom outlet of the hot melting tank is connected with a sodium sulfate evaporation crystallization unit through a hot melting discharge pump; the outlet II of the freezing mother liquor pipe is connected with the inlet of the nanofiltration membrane, the water production outlet of the nanofiltration membrane is connected with the sodium chloride evaporative crystallization unit, and the concentrated water outlet of the nanofiltration membrane is connected with the freezing feed pool; and the outlet III of the freezing mother liquor pipe is connected with a miscellaneous salt evaporation crystallization unit.
As an improvement of the utility model, the sodium sulfate evaporative crystallization unit comprises a sodium sulfate crystallizer, an outlet of a hot-melting discharge pump is connected with an inlet at the upper part of a salt leg of the sodium sulfate crystallizer through a hot-melting discharge pipe, an outlet at the lower part of the salt leg of the sodium sulfate crystallizer is connected with an inlet of a sodium sulfate thickening tank through a sodium sulfate discharge pump, an outlet at the bottom of the sodium sulfate thickening tank is connected with an inlet of a sodium sulfate centrifuge, and a solid phase outlet of the sodium sulfate centrifuge is connected with a sodium sulfate salt discharge pipe; the liquid phase outlet of the sodium sulfate centrifuge is connected with the inlet of a sodium sulfate mother liquor tank, the outlet of the sodium sulfate mother liquor tank is connected with a sodium sulfate circulating pipe through a sodium sulfate mother liquor pump and a sodium sulfate mother liquor pipe, the upper end of the sodium sulfate circulating pipe is connected with the circulating outlet of the sodium sulfate crystallizer, the lower end of the sodium sulfate circulating pipe is connected with the tube side inlet of a sodium sulfate heater through a sodium sulfate circulating pump, and the tube side outlet of the sodium sulfate heater is connected with the circulating inlet of the sodium sulfate heater; and the outlet of the sodium sulfate mother liquor pump is also connected with the inlet of the freezing feeding pool through a sodium sulfate mother liquor outer discharge pipe.
As a further improvement of the utility model, a top exhaust port of the sodium sulfate heater is connected with a steam inlet of a sodium sulfate steam compressor through a sodium sulfate secondary steam pipe, a steam outlet of the sodium sulfate steam compressor is connected with a shell pass inlet of the sodium sulfate heater, and a shell pass outlet of the sodium sulfate heater is connected with a sodium sulfate condensate water tank; and an outlet of the sodium sulfate condensate water tank is connected with a sodium sulfate condensate pipe through a sodium sulfate condensate pump, and the sodium sulfate condensate pipe is connected with an outlet of the sodium sulfate steam compressor.
Compared with the prior art, the utility model has the following beneficial effects: 1. after impurity removal by pretreatment, the maximum concentration difference of the system entering a freezing feeding pool can be the sodium sulfate content: the sodium chloride content =1: 4-3: 1, namely the highest concentration difference is that the concentration of sodium chloride is four times that of sodium sulfate, or the concentration of sodium sulfate is three times that of sodium chloride, and in the range of large concentration difference between sodium chloride and sodium sulfate, the sodium chloride and sodium sulfate can be separated, and the purpose of secondary utilization of industrial refined salt quality is achieved, and the energy consumption is low.
2. The method has the advantages that the separation of sodium chloride and sodium sulfate is realized by utilizing the difference of crystallization temperatures of sodium chloride and sodium sulfate and selectively utilizing the combination of evaporative crystallization and frozen crystalline phase, and qualified sodium chloride and sodium sulfate products meeting the recycling requirement of industrial production are produced, wherein the sodium sulfate products reach the first-class standard of class I of industrial anhydrous sodium sulfate GB/T6009-2014, can be directly used as industrial raw materials for reuse, and have great economic benefit and environmental protection benefit.
3. The resource recycling of the waste miscellaneous salt of sodium chloride and sodium sulfate is realized through an evaporative crystallization system, a refrigeration system and the like, the dilemma that the existing solid waste treatment enterprises can only treat single salt is broken, the resource recycling efficiency of the solid waste miscellaneous salt is improved, and the resource recycling regeneration of the waste miscellaneous salt is realized.
Drawings
The utility model will be described in further detail with reference to the following drawings and detailed description, which are provided for reference and illustration purposes only and are not intended to limit the utility model.
FIG. 1 is a flow diagram of a freezing system and a hot melt system according to the present invention;
FIG. 2 is a flow diagram of a sodium sulfate evaporative crystallization unit in the present invention.
In the figure: 17. a freezing feed tank; 18. a freezing crystallizer; 19. a freezing heat exchanger; 20. freezing the thick tank; 21. freezing the centrifuge; 22. a frozen mother liquor tank; 23. a hot melting tank; 24. a hot melt heat exchanger; 25. a hot melting condensation water tank; 26. a sodium sulfate heater; 27. a sodium sulfate crystallizer; 28. a sodium sulfate condensate tank; 29. a sodium sulfate thickening tank; 30. a sodium sulfate centrifuge; 31. a sodium sulfate mother liquor tank; 32. a sodium sulfate liquid accumulation tank; 33. a sodium sulfate vapor compressor; B10. a refrigerated feed pump; B11. a refrigeration circulating pump; B12. a freezing discharge pump; B13. a frozen mother liquor pump; B14. a hot melt circulation pump; B15. a hot melting discharge pump; B16. a hot melt condensate pump; B17. a sodium sulfate circulating pump; B18. a sodium sulfate condensate pump; B19. a sodium sulfate discharge pump; B20. a sodium sulfate mother liquor pump; B21. a sodium sulfate liquid accumulation pump; G21. a raw steam pipe; G25. a feed pipe; G30. a freezing feed tube; G31. freezing a discharge pipe; G32. freezing the mother liquor pipe; G33. mirabilite tube; G34. refrigerating fluid enters the pipe; G35. a refrigerating fluid outlet pipe; G36. a hot-melting circulating liquid pipe; G37. a hot melting discharge pipe; G38. a hot melting condensate pipe; G39. a sodium sulfate discharge pipe; G40. a sodium sulfate mother liquor pipe; G41. discharging the sodium sulfate mother liquor from the pipe; G42. sodium sulfate secondary steam pipe; G43. a sodium sulfate compressor steam outlet pipe; G44. sodium sulfate noncondensable tube; G45. a sodium sulfate condensate pipe; G46. a sodium sulfate liquid accumulating tube; G47. a sodium sulfate discharging pipe; G48. sodium sulfate effusion output pipe; G50. a concentrated water return pipe; G51. and a produced water output pipe.
Detailed Description
As shown in figure 1 of the drawings, in which, as shown in fig. 2, the production system for separating and refining the mixed waste mixed salt solution of sodium chloride and sodium sulfate comprises a freezing feed pool 17 connected with a pretreatment working section, a feed pipe G25 connected with an inlet of the freezing feed pool 17, an outlet of the freezing feed pool 17 connected with an inlet of a freezing feed pump B10, an outlet of a freezing feed pump B10 connected with an inlet of a freezing crystallizer 18 through a freezing feed pipe G30, a discharge port of the freezing crystallizer 18 connected with an inlet of a freezing discharge pump B12, an outlet of a freezing discharge pump B12 connected with an inlet of a freezing thick tank 20 through a freezing discharge pipe G31, a bottom outlet of the freezing thick tank 20 connected with an inlet of a freezing centrifuge 21, a mother liquor outlet of the freezing centrifuge 21 connected with an inlet of a freezing mother liquor tank B13, an outlet of the freezing mother liquor tank 22 connected with an inlet of a freezing mother liquor tank B13, and an outlet of the freezing mother liquor pump B13 connected with a freezing mother liquor pipe G32.
The solid phase outlet of the refrigerated centrifuge 21 is connected with the inlet of the hot melting tank 23 through a mirabilite pipe G33, the overflow outlet of the hot melting tank 23 is connected with the tube side inlet of the hot melting heat exchanger 24 through a hot melting circulating pump B14, and the tube side outlet of the hot melting heat exchanger 24 is connected with the circulating port of the hot melting tank 23 through a hot melting circulating liquid pipe G36; the shell pass inlet of the hot melting heat exchanger 24 is connected with the raw steam pipe G21, the shell pass outlet of the hot melting heat exchanger 24 is connected with the inlet of the hot melting condensation water tank 25, the outlet of the hot melting condensation water tank 25 is connected with the inlet of the hot melting condensation water pump B16, and the outlet of the hot melting condensation water pump B16 is output through the hot melting condensation water pipe G38. The heat source of the hot melting system is live steam, an external circulation forced heater is adopted, external water is not required, the treatment capacity of the sodium sulfate MVR evaporation crystallization unit is reduced, and the energy consumption is reduced.
The bottom outlet of the hot melting tank 23 is connected with a sodium sulfate evaporation crystallization unit through a hot melting discharge pump B15, the sodium sulfate evaporation crystallization unit comprises a sodium sulfate crystallizer 27, the outlet of a hot melting discharge pump B15 is connected with the inlet at the upper part of the salt leg of the sodium sulfate crystallizer 27 through a hot melting discharge pipe G37, the outlet at the lower part of the salt leg of the sodium sulfate crystallizer 27 is connected with the inlet of a sodium sulfate thickening tank 29 through a sodium sulfate discharge pump B19, the bottom outlet of the sodium sulfate thickening tank 29 is connected with the inlet of a sodium sulfate centrifuge 30, and the solid phase outlet of the sodium sulfate centrifuge 30 is connected with a sodium sulfate discharge pipe G47; a liquid phase outlet of the sodium sulfate centrifuge 30 is connected with an inlet of a sodium sulfate mother liquor tank 31, an outlet of the sodium sulfate mother liquor tank 31 is connected with a sodium sulfate circulating pipe through a sodium sulfate mother liquor pump B20 and a sodium sulfate mother liquor pipe G40, the upper end of the sodium sulfate circulating pipe is connected with a circulating outlet of a sodium sulfate crystallizer 27, the lower end of the sodium sulfate circulating pipe is connected with a tube side inlet of a sodium sulfate heater 26 through a sodium sulfate circulating pump B17, and a tube side outlet of the sodium sulfate heater 26 is connected with a circulating inlet of the sodium sulfate heater 26; the outlet of the sodium sulfate mother liquor pump B20 is also connected with the inlet of the freezing feed pool 17 through a sodium sulfate mother liquor outlet pipe G41. The upper part of the tube side of the sodium sulfate heater 26 is connected with a vacuum-pumping system through a sodium sulfate noncondensable gas tube G44.
A top exhaust port of the sodium sulfate heater 26 is connected with a steam inlet of a sodium sulfate steam compressor 33 through a sodium sulfate secondary steam pipe G42, a steam outlet of the sodium sulfate steam compressor 33 is connected with a shell-side inlet of the sodium sulfate heater 26, and a shell-side outlet of the sodium sulfate heater 26 is connected with a sodium sulfate condensate water tank 28; an outlet of the sodium sulfate condensate water tank 28 is connected with a sodium sulfate condensate water pipe G45 through a sodium sulfate condensate water pump B18, and a sodium sulfate condensate water pipe G45 is connected with an outlet of the sodium sulfate vapor compressor 33.
The mixed solution of sodium chloride and sodium sulfate in the freezing feed pool 17 is pumped by a freezing feed pump B10 and is sent into a freezing crystallizer 18 for cold freezing crystals, the upper part of the freezing crystallizer 18 overflows and is sent into the tube side of a freezing heat exchanger 19 by a freezing circulating pump B11, a cold source of the freezing heat exchanger 19 is freezing liquid generated by a freezing unit, the freezing liquid with the temperature of-10 ℃ enters the shell side inlet of the freezing heat exchanger 19 from a freezing liquid inlet tube G34 and is connected, the shell side outlet of the freezing heat exchanger 19 is connected with a freezing liquid outlet tube G35, the freezing liquid and the mixed solution carry out indirect heat exchange, the temperature of the mixed solution of sodium chloride and sodium sulfate is reduced to-5 ℃, the sodium sulfate is crystallized and separated, the sodium chloride is not separated, the freezing circulating liquid enters the bottom center of the freezing crystallizer 18 along a central tube, large-particle sodium sulfate crystal grains are settled at the bottom of the freezing crystallizer 18, and small-particle sodium sulfate crystal grains float upwards and flow out from the overflow port, and enters a refrigeration circulating pump B11 to circulate along the refrigeration circulating pipe.
The bottom discharge of the freezing crystallizer 18 is pumped out by a freezing discharge pump B12 and sent into the freezing thickening tank 20 for sedimentation, and the underflow of the freezing thickening tank 20 enters a freezing centrifuge 21 for separation; the mother liquor separated by the refrigerated centrifuge 21 and the mother liquor overflowing from the refrigerated thick stock tank 20 respectively enter a refrigerated mother liquor tank 22 for temporary storage, and then are sent to a refrigerated mother liquor pipe G32 by a refrigerated mother liquor pump B13.
The outlet of the freezing mother liquor pipe G32 is connected with the return port of the freezing crystallizer 18. In the initial stage of operation, the frozen mother liquor enters the reflux port of the freezing crystallizer 18 from the outlet of the frozen mother liquor pipe G32 to increase the concentration of the crystal slurry in the freezing crystallizer 18 as soon as possible.
And the outlet II of the freezing mother liquor pipe G32 is connected with the inlet of the nanofiltration membrane, and the concentrated water outlet of the nanofiltration membrane returns to the freezing feed tank 17 through a concentrated water return pipe G50 to circulate. The water production outlet of the nanofiltration membrane is connected with the sodium chloride evaporation crystallization unit through a water production output pipe G51. After the production is stable, most of the frozen mother liquor a is discharged from the outlet II of the frozen mother liquor pipe G32 and enters a nanofiltration membrane for filtration, and concentrated water of the nanofiltration membrane returns to the freezing feed tank 17 for repeated freezing; sodium sulfate content in the produced water of the nanofiltration membrane is less than or equal to 0.3 percent by weight, and the sodium sulfate enters a sodium chloride evaporation crystallization unit to obtain a sodium chloride product with purity of more than 98.7 percent through evaporation crystallization.
The outlet III of the freezing mother liquor pipe G32 is connected with a miscellaneous salt evaporation crystallization unit. And a small part of frozen mother liquor b is discharged from an outlet III of the frozen mother liquor pipe G32 and enters a mixed salt evaporation crystallization unit for evaporation, concentration and crystallization to obtain mixed salt. The flow rate of the freezing mother liquor a is more than 8 times of that of the freezing mother liquor b.
The method comprises the following steps that crystal salt separated by a refrigerated centrifuge 21 is mirabilite, the mirabilite is sodium sulfate decahydrate, the crystal salt is fed into a hot melting tank 23 of a hot melting system and is subjected to hot melting at 70-80 ℃ to form sodium sulfate salt solution, the sodium sulfate salt solution is fed into the upper part of a salt leg of a sodium sulfate crystallizer 27, small sodium sulfate particles float upwards, circulating liquid flows out of a circulating outlet of the sodium sulfate crystallizer 27 and is sent to a tube side of a sodium sulfate heater 26 by a sodium sulfate circulating pump B17, secondary steam discharged from the top of the sodium sulfate crystallizer 27 enters a sodium sulfate steam compressor 33 through a sodium sulfate secondary steam tube G42 to be compressed, and then returns to a shell side inlet of the sodium sulfate heater 26 through a steam outlet tube G43 of the sodium sulfate compressor to heat sodium sulfate circulating liquid, and complete cyclic utilization of the secondary steam is achieved; condensed water flowing out of a shell pass outlet of the sodium sulfate heater 26 enters a sodium sulfate condensed water tank 28 for temporary storage, is pumped out by a sodium sulfate condensed water pump B18 and is sent to an outlet of a sodium sulfate steam compressor 33 through a sodium sulfate condensed water pipe G45 for spraying so as to adjust the steam temperature.
The bottom accumulated liquid outlet of the sodium sulfate vapor compressor 33 enters the sodium sulfate accumulated liquid tank 32 through a sodium sulfate accumulated liquid pipe G46, the top flash steam port of the sodium sulfate accumulated liquid tank 32 is connected with a sodium sulfate secondary steam pipe G42, the bottom outlet of the sodium sulfate accumulated liquid tank 32 is connected with the inlet of a sodium sulfate accumulated liquid pump B21, and the outlet of the sodium sulfate accumulated liquid pump B21 is connected with a sodium sulfate accumulated liquid output pipe G48.
Large-particle sodium sulfate sinks to the bottom of the salt leg, is pumped out by a sodium sulfate discharge pump B19 and is sent into a sodium sulfate thickening tank 29 through a sodium sulfate discharge pipe G39 for sedimentation, and the underflow of the sodium sulfate thickening tank 29 enters a sodium sulfate centrifuge 30 for separation; mother liquor separated by the sodium sulfate centrifuge 30 and mother liquor overflowing from the sodium sulfate thickening tank 29 respectively enter the sodium sulfate mother liquor tank 31 for temporary storage, then are pumped out by a sodium sulfate mother liquor pump B20, return to a sodium sulfate circulating pipe through a sodium sulfate mother liquor pipe G40 for circulating concentration, and a small part of the mother liquor is discharged through a sodium sulfate mother liquor outer discharge pipe G41 and returns to the freezing feed tank 17. The concentration of sodium chloride in the circulating material of the sodium sulfate evaporation crystallization unit is strictly controlled by the sodium sulfate mother liquor, so that the quality of sodium sulfate crystallized salt is improved.
The solid phase separated by the sodium sulfate centrifuge 30 is sodium sulfate crystal salt, the sodium sulfate crystal salt is output through a sodium sulfate salt discharge pipe G47, and then a sodium sulfate product with the purity higher than 99.4% is obtained through a sodium sulfate drying and packaging unit, so that the sodium sulfate product reaches the first-class standard of industrial anhydrous sodium sulfate GB/T6009-2014.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the present invention. Technical features of the present invention which are not described may be implemented by or using the prior art, and will not be described herein.
Claims (3)
1. A sodium chloride and sodium sulfate mixed waste miscellaneous salt solution separation refining production system comprises a freezing feed pool connected with a pretreatment working section, and is characterized in that an outlet of the freezing feed pool is connected with an inlet of a freezing feed pump, an outlet of the freezing feed pump is connected with an inlet of a freezing crystallizer, a discharge port of the freezing crystallizer is connected with an inlet of a freezing discharge pump, an outlet of the freezing discharge pump is connected with an inlet of a freezing thickening tank, an outlet at the bottom of the freezing thickening tank is connected with an inlet of a freezing centrifuge, a mother liquor outlet of the freezing centrifuge is connected with an inlet of a freezing mother liquor tank, an outlet of the freezing mother liquor tank is connected with an inlet of a freezing mother liquor pump, and an outlet of the freezing mother liquor pump is connected with a freezing mother liquor pipe; the first outlet of the freezing mother liquor pipe is connected with a reflux port of the freezing crystallizer; the solid phase outlet of the refrigerated centrifuge is connected with the inlet of the hot melting tank through a mirabilite pipe, the overflow outlet of the hot melting tank is connected with the tube side inlet of the hot melting heat exchanger through a hot melting circulating pump, and the tube side outlet of the hot melting heat exchanger is connected with the circulating port of the hot melting tank through a hot melting circulating liquid pipe; the bottom outlet of the hot melting tank is connected with a sodium sulfate evaporation crystallization unit through a hot melting discharge pump; the outlet II of the freezing mother liquor pipe is connected with the inlet of the nanofiltration membrane, the water production outlet of the nanofiltration membrane is connected with the sodium chloride evaporative crystallization unit, and the concentrated water outlet of the nanofiltration membrane is connected with the freezing feed pool; and the outlet III of the freezing mother liquor pipe is connected with a miscellaneous salt evaporation crystallization unit.
2. The system for separating and refining the mixed waste miscellaneous salt solution of sodium chloride and sodium sulfate according to claim 1, wherein the sodium sulfate evaporative crystallization unit comprises a sodium sulfate crystallizer, an outlet of the hot-melt discharge pump is connected with an inlet at the upper part of a salt leg of the sodium sulfate crystallizer through a hot-melt discharge pipe, an outlet at the lower part of the salt leg of the sodium sulfate crystallizer is connected with an inlet of a sodium sulfate thickening tank through a sodium sulfate discharge pump, an outlet at the bottom of the sodium sulfate thickening tank is connected with an inlet of a sodium sulfate centrifuge, and a solid phase outlet of the sodium sulfate centrifuge is connected with a sodium sulfate salt discharge pipe; the liquid phase outlet of the sodium sulfate centrifuge is connected with the inlet of a sodium sulfate mother liquor tank, the outlet of the sodium sulfate mother liquor tank is connected with a sodium sulfate circulating pipe through a sodium sulfate mother liquor pump and a sodium sulfate mother liquor pipe, the upper end of the sodium sulfate circulating pipe is connected with the circulating outlet of the sodium sulfate crystallizer, the lower end of the sodium sulfate circulating pipe is connected with the tube side inlet of a sodium sulfate heater through a sodium sulfate circulating pump, and the tube side outlet of the sodium sulfate heater is connected with the circulating inlet of the sodium sulfate heater; and the outlet of the sodium sulfate mother liquor pump is also connected with the inlet of the freezing feeding pool through a sodium sulfate mother liquor outer discharge pipe.
3. The separation and refinement production system of the mixed waste miscellaneous salt solution of sodium chloride and sodium sulfate according to claim 2, characterized in that a top exhaust port of the sodium sulfate heater is connected with a steam inlet of a sodium sulfate steam compressor through a sodium sulfate secondary steam pipe, a steam outlet of the sodium sulfate steam compressor is connected with a shell pass inlet of the sodium sulfate heater, and a shell pass outlet of the sodium sulfate heater is connected with a sodium sulfate condensate water tank; and an outlet of the sodium sulfate condensate water tank is connected with a sodium sulfate condensate pipe through a sodium sulfate condensate pump, and the sodium sulfate condensate pipe is connected with an outlet of the sodium sulfate steam compressor.
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| CN202122428007.1U CN215924417U (en) | 2021-10-09 | 2021-10-09 | Production system for separating and refining sodium chloride and sodium sulfate mixed waste miscellaneous salt solution |
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| CN202122428007.1U CN215924417U (en) | 2021-10-09 | 2021-10-09 | Production system for separating and refining sodium chloride and sodium sulfate mixed waste miscellaneous salt solution |
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