CN111153417B - Comprehensive treatment device for separating salt from waste salt - Google Patents
Comprehensive treatment device for separating salt from waste salt Download PDFInfo
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- CN111153417B CN111153417B CN201911214100.3A CN201911214100A CN111153417B CN 111153417 B CN111153417 B CN 111153417B CN 201911214100 A CN201911214100 A CN 201911214100A CN 111153417 B CN111153417 B CN 111153417B
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- 150000003839 salts Chemical class 0.000 title claims abstract description 105
- 239000002699 waste material Substances 0.000 title claims abstract description 66
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 276
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 271
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 254
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 254
- 239000011780 sodium chloride Substances 0.000 claims abstract description 132
- 238000000926 separation method Methods 0.000 claims abstract description 60
- 238000001704 evaporation Methods 0.000 claims abstract description 58
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000012528 membrane Substances 0.000 claims abstract description 35
- 239000013078 crystal Substances 0.000 claims abstract description 30
- 239000012452 mother liquor Substances 0.000 claims description 107
- 229910002651 NO3 Inorganic materials 0.000 claims description 84
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 84
- 239000011552 falling film Substances 0.000 claims description 69
- 239000012267 brine Substances 0.000 claims description 63
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 63
- 230000008020 evaporation Effects 0.000 claims description 56
- 239000002562 thickening agent Substances 0.000 claims description 55
- 239000007791 liquid phase Substances 0.000 claims description 22
- 239000007787 solid Substances 0.000 claims description 21
- 238000002425 crystallisation Methods 0.000 claims description 20
- 238000002844 melting Methods 0.000 claims description 20
- 230000008018 melting Effects 0.000 claims description 16
- 239000012266 salt solution Substances 0.000 claims description 16
- 239000007790 solid phase Substances 0.000 claims description 16
- 230000008025 crystallization Effects 0.000 claims description 15
- 239000002002 slurry Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 239000013505 freshwater Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 abstract description 9
- 238000000034 method Methods 0.000 description 35
- 239000000243 solution Substances 0.000 description 35
- 239000010446 mirabilite Substances 0.000 description 13
- 238000001035 drying Methods 0.000 description 11
- 239000010413 mother solution Substances 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 238000005119 centrifugation Methods 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 125000004122 cyclic group Chemical group 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 238000007710 freezing Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 230000003139 buffering effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 239000010812 mixed waste Substances 0.000 description 2
- 125000000449 nitro group Chemical group [O-][N+](*)=O 0.000 description 2
- 231100000252 nontoxic Toxicity 0.000 description 2
- 230000003000 nontoxic effect Effects 0.000 description 2
- 239000000049 pigment Substances 0.000 description 2
- -1 so that on one hand Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009933 burial Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000001291 vacuum drying Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a comprehensive treatment device for separating salt from waste salt, which comprises a first sodium sulfate separation system, a membrane separation system, a sodium chloride separation system and a second sodium sulfate separation system; dissolving waste salt with dominant sodium sulfate, and recovering more than 90% of sodium sulfate in the waste salt with dominant sodium sulfate in a crystal form after series operation to obtain a solution containing residual sodium sulfate and all sodium chloride; and then dissolving the waste salt with dominant sodium chloride in the solution, separating by a membrane separation system to obtain concentrated water and light salt water, and respectively evaporating, concentrating and crystallizing the two solutions to finally obtain sodium sulfate crystals and sodium chloride crystals, thereby recovering all sodium sulfate and sodium chloride in the waste salt and realizing comprehensive centralized treatment of the sodium sulfate waste salt and the sodium chloride waste salt. The recovered sodium sulfate and sodium chloride can meet the requirements of industrial application, and fully realize the harmless, reduction and recycling utilization of waste salt.
Description
Technical Field
The invention relates to the field of industrial waste salt treatment, in particular to a comprehensive treatment device for waste salt.
Background
In recent years, along with the high-speed development of domestic economy, industries such as petrochemical industry, coal chemical industry, pesticide, pharmacy, food, printing and dyeing and the like also obtain great progress. In the development process of the industries, a large amount of high-salt-content wastewater is often generated, and the byproduct waste salt of the wastewater exceeds ten millions of tons, most of the waste salt is not reasonably disposed, and huge pressure is brought to ecological environment and social environment. The disposal of the waste salt in the industry generally has the defects of higher treatment cost, no system of treatment process, incomplete treatment, more dispersion of treatment devices and the like. Along with the stricter national control of enterprises with high salt-containing wastewater discharge, the establishment of a comprehensive disposal center for waste salt is very necessary for protecting natural environment and water resources on which we depend to live. The existing treatment methods of the solid waste salt mainly comprise the following methods:
(1) The burial method comprises the following steps: the solid waste salt which is nontoxic, harmless, not easy to degrade and volatilize is buried by selecting a proper geographic position;
(2) Incineration method: reducing and harmlessly treating the waste salt by adopting high-temperature incineration;
(3) Dispersion treatment method: each production enterprise respectively performs innocent treatment and salt separation treatment according to the characteristics of industrial waste salt generated by the enterprise and recycling;
The three schemes are comprehensively analyzed, the first scheme is only suitable for non-toxic and harmless waste salt treatment, and because the reduction and recycling treatment are not realized, the long-term accumulation can cause great pressure on the land resources of people, and the surrounding soil is inevitably damaged partially; the second scheme has better adaptability to waste salt containing more combustible matters, especially to waste salt containing single matters, and has the problem of salt separation to complex waste salt containing multiple components; the third scheme is fragmentation and dispersion treatment, and has the characteristics of flexibility, strong applicability and the like, but has the defects of no process system, high treatment cost, incomplete treatment, heavy enterprise burden and the like.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention aims to provide a comprehensive treatment device for waste salt, which can perform concentrated comprehensive salt separation treatment on mixed waste salts of sodium chloride and sodium sulfate with different contents.
The invention is realized by the following technical scheme:
an integrated treatment device for separating salt from waste salt, comprising: a first sodium sulfate separation system, a membrane separation system, a sodium chloride separation system, and a second sodium sulfate separation system; the first sodium sulfate separation system comprises: the device comprises a sodium sulfate salt solution tank, a first brine conveying pump, a first filter, a first brine buffer tank, a first brine pump, a precooler, a first cooler, a first nitrate crystallization kettle, a first nitrate centrifuge, a first nitrate melting tank, a first crystal slurry pump, a first sodium sulfate thickener, a first sodium sulfate centrifuge and a first sodium sulfate solid treatment device which are connected in sequence; the system further comprises a first nitrate mother liquor tank and a first nitrate mother liquor pump, wherein the first nitrate mother liquor tank is connected to a liquid phase outlet of the first nitrate centrifuge, and the first nitrate mother liquor tank is connected to the precooler through the first nitrate mother liquor pump; The device comprises a first sodium sulfate thickener, a first sodium sulfate mother liquor tank, a first sodium sulfate mother liquor pump, a first preheater and a first evaporation concentration device, wherein a liquid phase outlet of the first sodium sulfate centrifuge and a top overflow port of the first sodium sulfate thickener are connected into the first sodium sulfate mother liquor tank, the first sodium sulfate mother liquor pump and the first preheater are sequentially connected, the first preheater is connected to the first evaporation concentration device, and the first evaporation concentration device is simultaneously connected with the first sodium sulfate thickener; the membrane separation system includes: the sodium chloride salt solution tank, the second brine conveying pump, the second filter, the second brine buffer tank, the second brine pump, the cartridge filter, the high-pressure pump and the membrane separator are connected in sequence; the membrane separator is connected with the membrane separator, and the membrane separator is connected with the membrane separator; the precooler is connected with the sodium chloride salt solution tank; the second sodium sulfate separation system comprises: the device comprises a concentrated water pump, a second cooler, a second nitrate crystallization kettle, a second nitrate centrifuge, a second nitrate melting tank, a second slurry pump, a second sodium sulfate thickener, a second sodium sulfate centrifuge and a second sodium sulfate solid treatment device which are connected in sequence; the device also comprises a second nitrate mother liquor tank and a second nitrate mother liquor pump, wherein the second nitrate mother liquor tank is connected to a liquid phase outlet of the second nitrate centrifuge, and the second nitrate mother liquor tank is connected to the second salt water buffer tank through the second nitrate mother liquor pump; The second sodium sulfate thickener comprises a second sodium sulfate mother liquor tank, a second sodium sulfate mother liquor pump, a second preheater and a second evaporation concentration device, wherein a liquid phase outlet of the second sodium sulfate centrifuge and a top overflow port of the second sodium sulfate thickener are connected into the second sodium sulfate mother liquor tank, the second sodium sulfate mother liquor pump and the second preheater are sequentially connected, the second preheater is connected to the second evaporation concentration device, and the second evaporation concentration device is simultaneously connected with the second sodium sulfate thickener; the second cooler is connected with the concentrated water tank; the sodium chloride separation system comprises: the brine pump, the brine preheater, the third evaporation concentration device, the sodium chloride thickener, the sodium chloride centrifuge and the sodium chloride solid treatment device are connected in sequence; The sodium chloride thickener comprises a sodium chloride thickener, a sodium chloride mother liquor tank, a sodium chloride salt water tank, a sodium chloride concentration tank and a sodium chloride concentration tank, wherein the sodium chloride concentration tank is connected with the sodium chloride concentration tank through the sodium chloride concentration tank; the fresh brine pump is connected with the fresh brine tank.
Further, the first sodium sulfate solid treatment device comprises: the first sodium sulfate conveyor, the first sodium sulfate dryer, the second sodium sulfate conveyor and the first finished sodium sulfate packer are connected in sequence; the first sodium sulfate conveyor is connected with a solid phase outlet of the first sodium sulfate centrifuge.
Further, the first evaporation concentration device includes: the device comprises a first falling film evaporator, a first vapor compressor, a first circulating pump, a first condensate tank and a first condensate pump; the first preheater is connected into the first falling film evaporator, a tube side liquid phase outlet of the first falling film evaporator is connected into the first sodium sulfate thickener through the first circulating pump, a tube side gas phase outlet of the first falling film evaporator is connected to an inlet of the first vapor compressor, an outlet of the first vapor compressor is simultaneously connected to a shell side vapor inlet of the first falling film evaporator, a shell side condensate outlet of the first falling film evaporator is connected into the first condensate tank, and the first condensate tank is connected to the first preheater through the first condensate pump.
Further, the second sodium sulfate solid treatment device comprises: the third sodium sulfate conveyor, the second sodium sulfate dryer, the fourth sodium sulfate conveyor and the second finished sodium sulfate packer are connected in sequence; and the third sodium sulfate conveyor is connected with a solid phase outlet of the second sodium sulfate centrifuge.
Further, the second evaporation concentration device includes: the second falling film evaporator, the second vapor compressor, the second circulating pump, the second vapor condensate tank and the second vapor condensate pump; the second preheater is connected into the second falling film evaporator, a tube side liquid phase outlet of the second falling film evaporator is connected into the second sodium sulfate thickener through the second circulating pump, a tube side gas phase outlet of the second falling film evaporator is connected to an inlet of the second vapor compressor, an outlet of the second vapor compressor is simultaneously connected to a shell side vapor inlet of the second falling film evaporator, a shell side condensate outlet of the second falling film evaporator is connected into the second condensate tank, and the second condensate tank is connected with the second preheater through the second condensate pump.
Further, the concentration multiple of sodium sulfate in the concentrated water tank is 1.5-3, and the sodium sulfate content in the dilute brine tank is not higher than 0.5% (wt).
Further, the sodium chloride solid treatment device comprises: the first sodium chloride conveyor, the sodium chloride dryer, the second sodium chloride conveyor and the finished sodium chloride packer are connected in sequence; the first sodium chloride conveyor is connected with a solid phase outlet of the sodium chloride centrifuge.
Further, the third evaporation concentration device includes: the third falling film evaporator, the third vapor compressor, the third circulating pump, the third vapor condensation tank and the third vapor condensation pump; the fresh-water salt preheater is connected into the third falling film evaporator, a tube side liquid phase outlet of the third falling film evaporator is connected into the sodium chloride thickener through the third circulating pump, a tube side gas phase outlet of the third falling film evaporator is connected to an inlet of the third vapor compressor, an outlet of the third vapor compressor is simultaneously connected to a shell side vapor inlet of the third falling film evaporator, a shell side condensed water outlet of the third falling film evaporator is connected into the third vapor condensate tank, and the third vapor condensate tank is connected to the fresh-water salt preheater through the third vapor condensate pump.
Further, the operation temperature of the first nitro-crystallizing kettle is between-5 ℃ and 5 ℃, the operation temperature of the first nitro-melting tank is between 70 ℃ and 90 ℃, and the operation temperature of the first sodium sulfate thickener is between 80 ℃ and 100 ℃.
Further, the operation temperature of the second nitro-crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the second nitro-melting tank is between 70 ℃ and 90 ℃, and the operation temperature of the second sodium sulfate thickener is between 80 ℃ and 100 ℃.
Compared with the prior art, the invention has the following beneficial effects: (1) The characteristic that the solubility of sodium sulfate is greatly reduced along with the temperature reduction at low temperature is utilized to produce mirabilite by adopting a freezing crystallization method, so that the sodium sulfate is separated from the solution; (2) Concentrating divalent salt by using a membrane separation device according to different permselectivity of monovalent salt and divalent salt to the membrane; (3) The mother solution obtained by freezing and separating the waste salt with dominant sodium sulfate is used as a solvent of the waste salt with dominant sodium chloride, so that on one hand, water resources are saved, on the other hand, sodium sulfate and sodium chloride in the mother solution can be effectively recovered, and the generation of secondary waste salt is eliminated; (4) Separating sodium chloride and sodium sulfate by utilizing different solubility when they are co-dissolved; (5) The invention can completely recycle sodium sulfate and sodium chloride, thereby reducing the generation of secondary waste salt and eliminating the factor of secondary pollution; (6) Compared with the decentralized treatment, the method has the advantages that the waste salt with dominant sodium sulfate and the waste salt with dominant sodium chloride are intensively and comprehensively treated, so that the purpose of salt separation can be achieved, the operation cost can be effectively reduced, the complete recycling of resources is achieved, and the method has good social benefits; (7) The purity of the recovered sodium sulfate and sodium chloride can reach more than 98.5%, and the recovered sodium sulfate and sodium chloride can be directly sold to the outside, so that the method has remarkable economic benefit.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present invention.
In the figure: 1. sodium sulfate solution tank; 2. a first brine transfer pump; 3. a first filter; 4. a first brine buffer tank; 5. a first brine pump; 6. a precooler; 7. a first cooler; 8. a first nitro crystallization kettle; 9. a first nitrocentrifuge; 10. a first mother liquor tank; 11. a first nitrate mother liquor pump; 12. a first nitrate melting tank; 13. a first slurry pump; 14. a first sodium sulfate thickener; 15. a first sodium sulfate centrifuge; 16. a first sodium sulfate mother liquor tank; 17. a first sodium sulfate mother liquor pump; 18. a first preheater; 19. a first falling film evaporator; 20. a first vapor compressor; 21. a first circulation pump; 22. a first condensate tank; 23. a first condensate pump; 24. a first sodium sulfate conveyor; 25. a first sodium sulfate dryer; 26. a second sodium sulfate conveyor; 27. a first finished sodium sulfate packer; 28. sodium chloride salt fluid bowl; 29. a second brine transfer pump; 30. a second filter; 31. a second brine buffer tank; 32. a second brine pump; 33. a cartridge filter; 34. a high pressure pump; 35. a membrane separator; 36. a fresh brine tank; 37. a concentrate tank; 38. a fresh brine pump; 39. a dilute brine preheater; 40. a third falling film evaporator; 41. a third vapor compressor; 42. a third circulation pump; 43. a third steam condensate tank; 44. a third condensate pump; 45. sodium chloride thickener; 46. a sodium chloride centrifuge; 47. sodium chloride mother liquor tank; 48. sodium chloride mother liquor pump; 49. a first sodium chloride conveyor; 50. a sodium chloride dryer; 51. a second sodium chloride conveyor; 52. a finished sodium chloride packer; 53. a concentrate pump; 54. a second cooler; 55. a second nitro crystallization kettle; 56. a second nitrocentrifuge; 57. a second mother liquor tank; 58. a second nitrate mother liquor pump; 59. a second nitrate melting tank; 60. a second slurry pump; 61. a second sodium sulfate thickener; 62. a second sodium sulfate centrifuge; 63. a second sodium sulfate mother liquor tank; 64. a second sodium sulfate mother liquor pump; 65. a second preheater; 66. a second falling film evaporator; 67. a second vapor compressor; 68. a second steam condensate tank; 69. a second condensate pump; 70. a second circulation pump; 71. a third sodium sulfate conveyor; 72. a second sodium sulfate dryer; 73. a fourth sodium sulfate conveyor; 74. and (5) a second finished sodium sulfate packer.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and detailed description, wherein it is to be understood that, on the premise of no conflict, the following embodiments or technical features may be arbitrarily combined to form new embodiments.
The invention provides a comprehensive treatment device for waste salt and a comprehensive treatment process for waste salt, which can perform concentrated comprehensive salt separation treatment on mixed waste salts of sodium chloride and sodium sulfate with different contents.
The raw material waste salt put into treatment in the invention has two kinds: firstly, sodium sulfate is dominant, sodium chloride is a small amount of waste salt, and secondly, sodium chloride is dominant, and sodium sulfate is a small amount of waste salt. Dissolving waste salt with dominant sodium sulfate, and recovering more than 90% of sodium sulfate in the waste salt with dominant sodium sulfate in a crystal form after series operation to obtain a solution containing residual sodium sulfate and all sodium chloride; and then dissolving the waste salt with dominant sodium chloride in the solution, separating by a membrane separation system to obtain concentrated water and light salt water, and respectively evaporating, concentrating and crystallizing the two solutions to finally obtain sodium sulfate crystals and sodium chloride crystals, thereby recovering all sodium sulfate and sodium chloride in the waste salt and realizing comprehensive centralized treatment of the sodium sulfate waste salt and the sodium chloride waste salt. The recovered sodium sulfate and sodium chloride can meet the requirements of industrial application, and fully realize the harmless, reduction and recycling utilization of waste salt. The invention has the advantages of low comprehensive energy consumption, excellent salt separation effect, higher product quality, no secondary pollution, high comprehensive efficiency and the like.
Referring to fig. 1, the disclosed comprehensive treatment device for waste salt includes: a first sodium sulfate separation system, a membrane separation system, a sodium chloride separation system, and a second sodium sulfate separation system.
The first sodium sulfate separation system comprises: the sodium sulfate salt solution tank 1, the first brine conveying pump 2, the first filter 3, the first brine buffer tank 4, the first brine pump 5, the precooler 6, the first cooler 7, the first nitrate crystallization kettle 8, the first nitrate centrifuge 9, the first nitrate melting tank 12, the first crystal slurry pump 13, the first sodium sulfate thickener 14, the first sodium sulfate centrifuge 15 and the first sodium sulfate solid treatment device are sequentially connected. In addition, the device also comprises a first nitrate mother liquor tank 10 and a first nitrate mother liquor pump 11, wherein the first nitrate mother liquor tank 10 is connected to a liquid phase outlet of the first nitrate centrifuge 9, and the first nitrate melting tank 12 is connected to a solid phase outlet of the first nitrate centrifuge 9; the first nitrate mother liquor tank 10 is connected to one side inlet of the precooler 6 through a first nitrate mother liquor pump 11, and the cold energy in the nitrate mother liquor is recycled. In addition, still include first sodium sulfate mother liquor groove 16, first sodium sulfate mother liquor pump 17, first pre-heater 18 and first evaporation concentration device, wherein the liquid phase export of first sodium sulfate centrifuge 15 and the top overflow mouth of first sodium sulfate thickener 14 all are connected to in the first sodium sulfate mother liquor groove 16, first sodium sulfate mother liquor pump 17, first pre-heater 18 connect gradually, first pre-heater 18 reconnection is to first evaporation concentration device department, first evaporation concentration device still is connected with first sodium sulfate thickener 14 simultaneously, realize the circulation evaporation concentration of sodium sulfate solution. In addition, the precooler 6 is connected to one inlet of a sodium chloride salt solution tank 28 of the membrane separation system.
Specifically, the first sodium sulfate solid treatment device includes: a first sodium sulfate conveyor 24, a first sodium sulfate dryer 25, a second sodium sulfate conveyor 26 and a first finished sodium sulfate packer 27 which are connected in sequence; the first sodium sulfate conveyor 24 is connected to the solid phase outlet of the first sodium sulfate centrifuge 15.
Specifically, the first evaporation concentration device includes: a first falling film evaporator 19, a first vapor compressor 20, a first circulating pump 21, a first condensate tank 22 and a first condensate pump 23. The first preheater 18 is connected to the inside of the first falling film evaporator 19, the tube side liquid phase outlet of the first falling film evaporator 19 is connected to the inside of the first sodium sulfate thickener 14 through the first circulating pump 21, the tube side gas phase outlet of the first falling film evaporator 19 is connected to the inlet of the first vapor compressor 20, the outlet of the first vapor compressor 20 is simultaneously connected to the shell side vapor inlet of the first falling film evaporator 19, the shell side condensed water outlet of the first falling film evaporator 19 is connected to the inside of the first condensed water tank 22, and the first condensed water tank 22 is connected to one side inlet of the first preheater 18 through the first condensed water pump 23.
The process flow and the working principle of the first sodium sulfate separation system, namely the waste salt treatment method with dominant sodium sulfate, are described in detail as follows:
The waste salt (200-300 ℃) which is mainly sodium sulfate and is used for removing organic matters and pigments after pretreatment is put into a sodium sulfate salt solution tank 1 for dissolution, a first brine conveying pump 2 pumps salt solution to a first filter 3 for filtering impurities, after standing and buffering in a first brine buffer tank 4, the salt solution is sequentially pumped to a precooler 6 by a first brine pump 5 for precooling to 25-30 ℃, cooled to-5 ℃ in a first cooler 7, then enters a first nitrate crystallization kettle 8 for crystallization at-5 ℃, and is centrifugally separated by a first nitrate centrifuge 9, so that mirabilite solution and mirabilite crystals are obtained.
The mirabilite solution obtained after centrifugal separation enters a first nitrate mother liquor tank 10, is pumped into a precooler 6 by a first nitrate mother liquor pump 11, then enters a sodium chloride salt solution tank 28, and is used as a solvent for dissolving waste salt with dominant sodium chloride. On the other hand, the mirabilite crystal obtained after centrifugal separation enters a first nitrate melting tank 12 to be melted at 70-90 ℃, fluid of melted sodium sulfate crystal is pumped into a first sodium sulfate thickener 14 through a first crystal slurry pump 13, and is fully crystallized and separated at 80-100 ℃, and then enters a first sodium sulfate centrifuge 15 to be subjected to centrifugal treatment, so that sodium sulfate mother liquor and sodium sulfate crystal are obtained.
The separated sodium sulfate crystals are discharged from a solid phase outlet of a first sodium sulfate centrifuge 15, conveyed into a first sodium sulfate dryer 25 by a first sodium sulfate conveyor 24 for drying treatment, and conveyed into a first finished sodium sulfate packer 27 by a second sodium sulfate conveyor 26 to finish drying, packing and outward transportation treatment of the solid sodium sulfate crystals. On the other hand, the sodium sulfate mother liquor after centrifugation enters the first sodium sulfate mother liquor tank 16, and meanwhile, the mother liquor overflowed from the top of the first sodium sulfate thickener 14 also enters the first sodium sulfate mother liquor tank 16, and the mixed liquor is pumped to the first preheater 18 through the first sodium sulfate mother liquor pump 17 and enters the first evaporation concentration device after being preheated, so that the circulating evaporation concentration of the sodium sulfate mother liquor is carried out.
The sodium sulfate mother liquor is preheated to 85-95 ℃ by steam condensate in one side of the first preheater 18 and then enters the first falling film evaporator 19 to be evaporated and concentrated at 100-110 ℃; the secondary steam obtained by evaporation is compressed and upgraded by the first steam compressor 20, then enters the shell side of the first falling film evaporator 19 again to be used as a heat source for heating sodium sulfate solution, so that the cyclic utilization of steam is realized, the condensed steam condensate enters the first steam condensate tank 22, and is pumped into the other side of the first preheater 18 by the first steam condensate pump 23, so that the sodium sulfate mother liquor is preheated, and the energy recycling is realized. The concentrated solution obtained after evaporation and concentration flows out from the bottom of the tube side of the first falling film evaporator 19, one part of the concentrated solution enters the first falling film evaporator 19 again through the first circulating pump 21 to be used as a replenishing solution to circulate and evaporate, the other part of the concentrated solution enters the first sodium sulfate thickener 14 to be thickened and crystallized, then enters the first sodium sulfate centrifuge 15 to be centrifuged, and the sodium sulfate mother solution obtained after centrifugation is preheated and evaporated again, so that the concentrated evaporation is continuously circulated and carried out, and finally sodium sulfate crystals in the solution are completely recovered.
It should be noted that the present invention only describes a mechanical vapor recompression evaporation (MVR) process technology to achieve the purpose of evaporation concentration. In practical evaporation and concentration processes, more MVR, MED (multiple effect evaporation) and MSF (multiple effect flash evaporation) are used in industrial applications; MVR is relatively the lowest cost to operate, but MED operates more stably, and MSF is commonly used in the field of seawater desalination. In general, the MVR and MED can meet the evaporation concentration requirements of the present disclosure, and in the light of the present disclosure, any evaporation concentration technique is adopted, so long as the evaporation concentration technique capable of meeting the crystallization separation conditions required by the present disclosure falls within the scope of the present disclosure. In addition, the drying process has the process technologies of normal pressure drying, vacuum drying and the like, and the drying process is within the protection scope of the invention no matter what drying equipment and drying process are adopted as long as the purpose of drying the centrifugally separated product to a qualified finished product can be achieved.
After the waste salt with dominant sodium sulfate is treated by the first sodium sulfate separation system, finally obtaining high-purity sodium sulfate crystal and mirabilite solution which is used as a solvent of the waste salt with dominant sodium chloride.
The membrane separation system includes: a sodium chloride salt solution tank 28, a second brine delivery pump 29, a second filter 30, a second brine buffer tank 31, a second brine pump 32, a cartridge filter 33, a high-pressure pump 34 and a membrane separator 35 which are connected in sequence; the membrane separator is characterized by further comprising a concentrated water tank 37 and a light brine tank 36, wherein the concentrated water tank 37 and the light brine tank 36 are respectively connected with the membrane separator 35. A sodium chloride salt solution tank 28 is connected to the outlet of the precooler 6 side in the first sodium sulfate separation system for introducing a mirabilite solution. The second filter 30 has a filtration accuracy of not more than 100 μm and the cartridge filter 33 has a filtration accuracy of not more than 5 μm.
The process flow and the working principle of the membrane separation system, namely the membrane separation method of waste salt with dominant sodium chloride, are described in detail as follows:
The waste salt which is pretreated and is mainly sodium chloride with the temperature of 200-300 ℃ and is used for removing organic matters and pigments is put into a sodium chloride salt solution tank 28, and the dissolved solvent is mirabilite solution from one side of a precooler 6 and a small amount of process water for supplementing insufficient solvent. The salt solution is mixed into the nitrate mother solution from the second nitrate mother solution tank 57, filtered by the second filter 30 through the second brine conveying pump 29, then enters the second brine buffer tank 31 for standing and buffering, is pumped into the cartridge filter 33 through the second brine pump 32 for precise filtration, and is pumped into the membrane separator 35 through the high-pressure pump 34 for salt separation at a temperature lower than 50 ℃. The divalent salt is concentrated by using a membrane separator 35 by utilizing the difference in the selective permeability of the monovalent salt and the divalent salt to the membrane, the separated concentrated water is introduced into a concentrated water tank 37, and the separated dilute brine is introduced into a dilute brine tank 36, and the next crystallization treatment is waited for.
Wherein, after separation by the membrane separator 35, the concentration multiple of sodium sulfate in the concentrated water tank 37 is 1.5-3, and the sodium sulfate content in the dilute brine tank 36 is not higher than 0.5% (wt). It should be noted that, in the case of membrane separation process, as long as the divalent salt can be concentrated to the multiple described in the disclosure of the present patent application, any separation equipment and separation process are adopted, and all such processes are within the scope of the present invention.
The second sodium sulfate separation system comprises: the concentrated water pump 53, the second cooler 54, the second nitrate crystallization kettle 55, the second nitrate centrifuge 56, the second nitrate melting tank 59, the second slurry pump 60, the second sodium sulfate thickener 61, the second sodium sulfate centrifuge 62 and the second sodium sulfate solid treatment device are connected in sequence. In addition, the device further comprises a second nitrate mother liquor tank 57 and a second nitrate mother liquor pump 58, wherein the second nitrate mother liquor tank 57 is connected to a liquid phase outlet of the second nitrate centrifuge 56, and the second nitrate melting tank 59 is connected to a solid phase outlet of the second nitrate centrifuge 56; the second nitrate mother liquor tank 57 is connected to the second brine buffer tank 31 through a second nitrate mother liquor pump 58, and realizes the circulation separation of the nitrate mother liquor. In addition, still include second sodium sulfate mother liquor groove 63, second sodium sulfate mother liquor pump 64, second pre-heater 65 and second evaporation concentration device, the liquid phase export of second sodium sulfate centrifuge 62 and the top overflow mouth of second sodium sulfate thickener 61 all are connected to in the second sodium sulfate mother liquor groove 63, second sodium sulfate mother liquor pump 64 and second pre-heater 65 one side entry connect gradually, second pre-heater 65 one side export reconnection is to second evaporation concentration device department, second evaporation concentration device still is connected with second sodium sulfate thickener 61 simultaneously, realize the circulation evaporation concentration of sodium sulfate mother liquor. The second cooler 54 is connected to the concentrate tank 37 for introducing sodium sulfate solution.
Specifically, the second sodium sulfate solid treatment device includes: a third sodium sulfate conveyor 71, a second sodium sulfate dryer 72, a fourth sodium sulfate conveyor 73, and a second finished sodium sulfate packer 74 connected in this order; the third sodium sulfate conveyor 71 is connected to the solid phase outlet of the second sodium sulfate centrifuge 62.
Specifically, the second evaporation and concentration device includes: a second falling film evaporator 66, a second vapor compressor 67, a second circulation pump 70, a second condensate tank 68, and a second condensate pump 69. The second preheater 65 is connected to the second falling film evaporator 66, the tube side liquid phase outlet of the second falling film evaporator 66 is connected to the second sodium sulfate thickener 61 through the second circulating pump 70, the tube side gas phase outlet of the second falling film evaporator 66 is connected to the inlet of the second vapor compressor 67, the outlet of the second vapor compressor 67 is simultaneously connected to the shell side vapor inlet of the second falling film evaporator 66, the shell side condensed water outlet of the second falling film evaporator 66 is connected to the second condensed water tank 68, and the second condensed water tank 68 is connected to the inlet on the other side of the second preheater 65 through the second condensed water pump 69.
The process flow and working principle of the second sodium sulfate separation system, namely the treatment method of the concentrated water, are described in detail below:
The concentrated water from the concentrated water tank 37 is pumped into a second cooler 54 through a concentrated water pump 53, cooled to-5 ℃ to 5 ℃, then enters a second nitrate crystallization kettle 55 for crystallization at-5 ℃ to 5 ℃, and then is separated by a second nitrate centrifuge 56 to obtain a mirabilite solution and mirabilite crystals. The mirabilite solution obtained after centrifugation enters a second nitrate mother liquor tank 57, and is pumped back into a second salt water buffer tank 31 by a second nitrate mother liquor pump 58 for circulating separation; on the other hand, the mirabilite crystal obtained after centrifugation enters a second nitrate melting tank 59 to be melted at 70-90 ℃, fluid of the sodium sulfate crystal obtained after melting is pumped into a second sodium sulfate thickener 61 through a second slurry pump 60, and is fully crystallized and separated at 80-100 ℃, and then enters a second sodium sulfate centrifuge 62 to be centrifuged, so that sodium sulfate mother liquor and sodium sulfate crystal are obtained.
The separated sodium sulfate crystals are discharged from the solid phase outlet of the second sodium sulfate centrifuge 62, are conveyed into a second sodium sulfate dryer 72 by a third sodium sulfate conveyor 71 to be dried, and are conveyed to a second finished sodium sulfate packer 74 by the third sodium sulfate conveyor 71 to finish the drying, packing and outward transportation of the solid sodium sulfate crystals. On the other hand, the sodium sulfate mother liquor obtained after centrifugation enters the second sodium sulfate mother liquor tank 63, and meanwhile, the mother liquor overflowed from the top of the second sodium sulfate thickener 61 also enters the second sodium sulfate mother liquor tank 63, and the mixed liquor is pumped into the second evaporation concentration device through the second sodium sulfate mother liquor pump 64 to carry out circulating evaporation concentration of the sodium sulfate mother liquor.
The sodium sulfate mother liquor is preheated to 85-95 ℃ in the second preheater 65 by steam condensate, then enters the second falling film evaporator 66, and is evaporated and concentrated at 100-110 ℃; the secondary steam obtained by evaporation is compressed and upgraded by a second steam compressor 67, then enters the shell side of a second falling film evaporator 66 again to be used as a heat source to heat sodium sulfate solution, so that the cyclic utilization of steam is realized, the condensed steam condensate enters a second steam condensate tank 68, and is pumped into the other side of the second preheater 65 by a second steam condensate pump 69, so that the preheating of sodium sulfate mother liquor is realized, and the recycling of energy is realized. And the concentrated solution obtained after evaporation and concentration flows out from the bottom of the second falling film evaporator 66, one part of the concentrated solution is pumped into the second falling film evaporator 66 again through the second circulating pump 70 to be used as a replenishing solution for circulation and evaporation, and the other part of the concentrated solution is pumped into the second sodium sulfate thickener 61 to be thickened and crystallized and then enters the second sodium sulfate centrifuge 62 to be separated again, so that the sodium sulfate solution is continuously subjected to circulation, evaporation, concentration and crystallization, and sodium sulfate crystals in the solution are completely recovered.
The sodium chloride separation system comprises: the brine pump 38, the brine preheater 39, the third evaporation concentration device, the sodium chloride thickener 45, the sodium chloride centrifuge 46 and the sodium chloride solid treatment device are connected in sequence. In addition, the device also comprises a sodium chloride mother liquor tank 47 and a sodium chloride mother liquor pump 48, wherein a liquid phase outlet of the sodium chloride centrifugal machine 46 and a top overflow port of the sodium chloride thickener 45 are connected into the sodium chloride mother liquor tank 47, and the sodium chloride mother liquor tank 47 is connected into the dilute brine tank 36 through the sodium chloride mother liquor pump 48; a brine pump 38 is connected to the brine tank 36.
Specifically, the sodium chloride solid treatment device comprises: a first sodium chloride conveyor 49, a sodium chloride dryer 50, a second sodium chloride conveyor 51 and a finished sodium chloride packer 52 connected in sequence; the first sodium chloride conveyor 49 is connected to the solid phase outlet of the sodium chloride centrifuge 46.
Specifically, the third evaporation concentration device includes: a third falling film evaporator 40, a third vapor compressor 41, a third circulating pump 42, a third condensate tank 43 and a third condensate pump 44. The fresh brine preheater 39 is connected to the third falling film evaporator 40, the tube side liquid phase outlet of the third falling film evaporator 40 is connected to the sodium chloride thickener 45 through the third circulating pump 42, the tube side gas phase outlet of the third falling film evaporator 40 is connected to the inlet of the third vapor compressor 41, the outlet of the third vapor compressor 41 is simultaneously connected to the shell side vapor inlet of the third falling film evaporator 40, the shell side condensed water outlet of the third falling film evaporator 40 is connected to the third condensed water tank 43, and the third condensed water tank 43 is connected to the inlet on one side of the fresh brine preheater 39 through the third condensed water pump 44.
The process flow and working principle of the sodium chloride separation system, namely the treatment method of the dilute brine, are described in detail as follows:
The dilute brine from the dilute brine tank 36 and the sodium chloride mother liquor from the sodium chloride mother liquor tank 47 are mixed, pumped to one side of the dilute brine preheater 39 by the dilute brine pump 38, preheated to 70-80 ℃ by the steam condensate, and then enter the third falling film evaporator 40 for evaporation concentration at 100-115 ℃; the secondary steam obtained after evaporation is compressed and upgraded by a third steam compressor 41, and then enters a third falling film evaporator 40 again as a heat source to heat sodium chloride solution, so that the cyclic utilization of steam is realized, the condensed steam condensate enters a third steam condensate tank 43, and is pumped into one side of a fresh brine preheater 39 by a third steam condensate pump 44 for preheating sodium chloride solution, so that the recycling of energy is realized. And the concentrated solution obtained after evaporation and concentration flows out through the bottom of the third falling film evaporator 40, one part of the concentrated solution is pumped into the third falling film evaporator 40 through the third circulating pump 42 to be circularly evaporated as a replenishing solution, the other part of the concentrated solution is pumped into the sodium chloride thickener 45, cooling, crystallizing and separating are carried out at the temperature of 40-50 ℃, and the fluid containing sodium chloride crystals, which is discharged from the bottom of the sodium chloride thickener 45, enters the sodium chloride centrifuge 46 to be centrifuged, so that sodium chloride mother solution and sodium chloride crystals are obtained.
The sodium chloride crystals obtained after separation are discharged from the solid phase outlet of the sodium chloride centrifuge 46, are conveyed into a sodium chloride dryer 50 for drying treatment by a first sodium chloride conveyor 49, and are conveyed to a finished sodium chloride packer 52 by a second sodium chloride conveyor 51, so that the drying, packing and outward transportation treatment of the solid sodium chloride crystals are completed. On the other hand, the sodium chloride mother liquor obtained after centrifugation enters the sodium chloride mother liquor tank 47, and meanwhile, the mother liquor overflowed from the top of the sodium chloride thickener 45 also enters the sodium chloride mother liquor tank 47, and the mixed liquor is pumped into the fresh brine tank 36 again through the sodium chloride mother liquor pump 48, so that the circulating separation and evaporation concentration of the sodium chloride mother liquor are performed. The sodium chloride crystals in the solution are completely recovered by continuous cyclic separation and evaporative concentration.
After the four steps, the sodium sulfate and the sodium chloride are separated respectively, and the purity of the sodium sulfate and the sodium chloride can reach more than 98.5 percent, thereby completely meeting the industrial requirements. In the whole treatment process, no secondary waste salt is generated, so that secondary pollution is reduced. Because no volatile component exists in the pretreated waste salt, the vaporized condensate water obtained by evaporation can be directly and completely reused as process water, and the effect of zero emission of waste water is realized.
In addition, the vapor recompression technique is used in the present process, and thus, vapor is hardly consumed. In the integrated process, the power consumption of the ton of products is only about 250 kilowatt-hours.
From the detailed description of the embodiments above, it will be appreciated that the present invention: (1) The characteristic that the solubility of sodium sulfate is greatly reduced along with the temperature reduction at low temperature is utilized to produce mirabilite by adopting a freezing crystallization method, so that the sodium sulfate is separated from the solution; (2) Concentrating divalent salt by using a membrane separation device according to different permselectivity of monovalent salt and divalent salt to the membrane; (3) The mother solution obtained by freezing and separating the waste salt with dominant sodium sulfate is used as a solvent of the waste salt with dominant sodium chloride, so that on one hand, water resources are saved, on the other hand, sodium sulfate and sodium chloride in the mother solution can be effectively recovered, and the generation of secondary waste salt is eliminated; (4) Separating sodium chloride and sodium sulfate by utilizing different solubility when they are co-dissolved; (5) The invention can completely recycle sodium sulfate and sodium chloride, thereby reducing the generation of secondary waste salt and eliminating the factor of secondary pollution; (6) Compared with the decentralized treatment, the method has the advantages that the waste salt with dominant sodium sulfate and the waste salt with dominant sodium chloride are intensively and comprehensively treated, so that the purpose of salt separation can be achieved, the operation cost can be effectively reduced, the complete recycling of resources is achieved, and the method has good social benefits; (7) The purity of the recovered sodium sulfate and sodium chloride can reach more than 98.5%, and the recovered sodium sulfate and sodium chloride can be directly sold to the outside, so that the method has remarkable economic benefit.
The above embodiments are only preferred embodiments of the present invention, and the scope of the present invention is not limited thereto, but any insubstantial changes and substitutions made by those skilled in the art on the basis of the present invention are intended to be within the scope of the present invention as claimed.
Claims (10)
1. An integrated treatment device for separating salt from waste salt, which is characterized by comprising: a first sodium sulfate separation system, a membrane separation system, a sodium chloride separation system, and a second sodium sulfate separation system;
The first sodium sulfate separation system comprises: the device comprises a sodium sulfate salt solution tank, a first brine conveying pump, a first filter, a first brine buffer tank, a first brine pump, a precooler, a first cooler, a first nitrate crystallization kettle, a first nitrate centrifuge, a first nitrate melting tank, a first crystal slurry pump, a first sodium sulfate thickener, a first sodium sulfate centrifuge and a first sodium sulfate solid treatment device which are connected in sequence; the system comprises a precooler, a first nitrate mother liquor tank, a first nitrate mother liquor pump, a second nitrate mother liquor tank, a first nitrate melting tank, a second nitrate mother liquor pump and a second nitrate mother liquor tank, wherein the first nitrate mother liquor tank is connected to a liquid phase outlet of the first nitrate centrifuge, the first nitrate melting tank is connected to a solid phase outlet of the first nitrate centrifuge, and the first nitrate mother liquor tank is connected to the precooler through the first nitrate mother liquor pump; the device comprises a first sodium sulfate thickener, a first sodium sulfate mother liquor tank, a first sodium sulfate mother liquor pump, a first preheater and a first evaporation concentration device, wherein a liquid phase outlet of the first sodium sulfate centrifuge and a top overflow port of the first sodium sulfate thickener are connected into the first sodium sulfate mother liquor tank, the first sodium sulfate mother liquor pump and the first preheater are sequentially connected, the first preheater is connected to the first evaporation concentration device, and the first evaporation concentration device is simultaneously connected with the first sodium sulfate thickener;
The membrane separation system includes: the sodium chloride salt solution tank, the second brine conveying pump, the second filter, the second brine buffer tank, the second brine pump, the cartridge filter, the high-pressure pump and the membrane separator are connected in sequence; the membrane separator is connected with the membrane separator, and the membrane separator is connected with the membrane separator;
The precooler is connected with the sodium chloride salt solution tank;
The second sodium sulfate separation system comprises: the device comprises a concentrated water pump, a second cooler, a second nitrate crystallization kettle, a second nitrate centrifuge, a second nitrate melting tank, a second slurry pump, a second sodium sulfate thickener, a second sodium sulfate centrifuge and a second sodium sulfate solid treatment device which are connected in sequence; the device also comprises a second nitrate mother liquor tank and a second nitrate mother liquor pump, wherein the second nitrate mother liquor tank is connected to a liquid phase outlet of the second nitrate centrifuge, the second nitrate melting tank is connected to a solid phase outlet of the second nitrate centrifuge, and the second nitrate mother liquor tank is connected to the second salt water buffer tank through the second nitrate mother liquor pump; the second sodium sulfate thickener comprises a second sodium sulfate mother liquor tank, a second sodium sulfate mother liquor pump, a second preheater and a second evaporation concentration device, wherein a liquid phase outlet of the second sodium sulfate centrifuge and a top overflow port of the second sodium sulfate thickener are connected into the second sodium sulfate mother liquor tank, the second sodium sulfate mother liquor pump and the second preheater are sequentially connected, the second preheater is connected to the second evaporation concentration device, and the second evaporation concentration device is simultaneously connected with the second sodium sulfate thickener;
The second cooler is connected with the concentrated water tank;
The sodium chloride separation system comprises: the brine pump, the brine preheater, the third evaporation concentration device, the sodium chloride thickener, the sodium chloride centrifuge and the sodium chloride solid treatment device are connected in sequence; the sodium chloride thickener comprises a sodium chloride thickener, a sodium chloride mother liquor tank, a sodium chloride salt water tank, a sodium chloride concentration tank and a sodium chloride concentration tank, wherein the sodium chloride concentration tank is connected with the sodium chloride concentration tank through the sodium chloride concentration tank;
the fresh brine pump is connected with the fresh brine tank.
2. The integrated waste salt treatment apparatus of claim 1, wherein the first sodium sulfate solid treatment apparatus comprises: the first sodium sulfate conveyor, the first sodium sulfate dryer, the second sodium sulfate conveyor and the first finished sodium sulfate packer are connected in sequence; the first sodium sulfate conveyor is connected with a solid phase outlet of the first sodium sulfate centrifuge.
3. The integrated waste salt treatment apparatus as claimed in claim 1, wherein said first evaporation concentration apparatus comprises: the device comprises a first falling film evaporator, a first vapor compressor, a first circulating pump, a first condensate tank and a first condensate pump; the first preheater is connected into the first falling film evaporator, a tube side liquid phase outlet of the first falling film evaporator is connected into the first sodium sulfate thickener through the first circulating pump, a tube side gas phase outlet of the first falling film evaporator is connected to an inlet of the first vapor compressor, an outlet of the first vapor compressor is simultaneously connected to a shell side vapor inlet of the first falling film evaporator, a shell side condensate outlet of the first falling film evaporator is connected into the first condensate tank, and the first condensate tank is connected to the first preheater through the first condensate pump.
4. The integrated waste salt treatment apparatus as claimed in claim 1, wherein the second sodium sulfate solid treatment apparatus comprises: the third sodium sulfate conveyor, the second sodium sulfate dryer, the fourth sodium sulfate conveyor and the second finished sodium sulfate packer are connected in sequence; and the third sodium sulfate conveyor is connected with a solid phase outlet of the second sodium sulfate centrifuge.
5. The comprehensive treatment device for waste salt according to claim 1, wherein the second evaporation and concentration device comprises: the second falling film evaporator, the second vapor compressor, the second circulating pump, the second vapor condensate tank and the second vapor condensate pump; the second preheater is connected into the second falling film evaporator, a tube side liquid phase outlet of the second falling film evaporator is connected into the second sodium sulfate thickener through the second circulating pump, a tube side gas phase outlet of the second falling film evaporator is connected to an inlet of the second vapor compressor, an outlet of the second vapor compressor is simultaneously connected to a shell side vapor inlet of the second falling film evaporator, a shell side condensate outlet of the second falling film evaporator is connected into the second condensate tank, and the second condensate tank is connected with the second preheater through the second condensate pump.
6. The comprehensive treatment device for waste salt according to claim 1, wherein the concentration multiple of sodium sulfate in the concentrated water tank is 1.5-3, and the sodium sulfate content in the dilute brine tank is not higher than 0.5% (wt).
7. The integrated waste salt treatment apparatus as claimed in claim 1, wherein the sodium chloride solid treatment apparatus comprises: the first sodium chloride conveyor, the sodium chloride dryer, the second sodium chloride conveyor and the finished sodium chloride packer are connected in sequence; the first sodium chloride conveyor is connected with a solid phase outlet of the sodium chloride centrifuge.
8. The comprehensive treatment device for waste salt according to claim 1, wherein the third evaporation and concentration device comprises: the third falling film evaporator, the third vapor compressor, the third circulating pump, the third vapor condensation tank and the third vapor condensation pump; the fresh-water salt preheater is connected into the third falling film evaporator, a tube side liquid phase outlet of the third falling film evaporator is connected into the sodium chloride thickener through the third circulating pump, a tube side gas phase outlet of the third falling film evaporator is connected to an inlet of the third vapor compressor, an outlet of the third vapor compressor is simultaneously connected to a shell side vapor inlet of the third falling film evaporator, a shell side condensed water outlet of the third falling film evaporator is connected into the third vapor condensate tank, and the third vapor condensate tank is connected to the fresh-water salt preheater through the third vapor condensate pump.
9. The comprehensive treatment device for waste salt according to claim 1, wherein the operation temperature of the first nitro-crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the first nitro-melting tank is between 70 ℃ and 90 ℃, and the operation temperature of the first sodium sulfate thickener is between 80 ℃ and 100 ℃.
10. The comprehensive treatment device for waste salt according to claim 1, wherein the operation temperature of the second nitro-crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the second nitro-melting tank is between 70 ℃ and 90 ℃, and the operation temperature of the second sodium sulfate thickener is between 80 ℃ and 100 ℃.
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