CN111153417A - Comprehensive treatment device for waste salt separation - Google Patents
Comprehensive treatment device for waste salt separation Download PDFInfo
- Publication number
- CN111153417A CN111153417A CN201911214100.3A CN201911214100A CN111153417A CN 111153417 A CN111153417 A CN 111153417A CN 201911214100 A CN201911214100 A CN 201911214100A CN 111153417 A CN111153417 A CN 111153417A
- Authority
- CN
- China
- Prior art keywords
- sodium sulfate
- tank
- pump
- sodium chloride
- falling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 150000003839 salts Chemical class 0.000 title claims abstract description 106
- 239000002699 waste material Substances 0.000 title claims abstract description 68
- 238000000926 separation method Methods 0.000 title claims abstract description 65
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 277
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 270
- 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 134
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 67
- 238000001704 evaporation Methods 0.000 claims abstract description 43
- 239000013078 crystal Substances 0.000 claims abstract description 32
- 239000012528 membrane Substances 0.000 claims abstract description 30
- 239000012452 mother liquor Substances 0.000 claims description 81
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 77
- 239000011552 falling film Substances 0.000 claims description 69
- 239000012267 brine Substances 0.000 claims description 65
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 65
- 239000002562 thickening agent Substances 0.000 claims description 49
- 230000008020 evaporation Effects 0.000 claims description 41
- 235000010333 potassium nitrate Nutrition 0.000 claims description 39
- 229910002651 NO3 Inorganic materials 0.000 claims description 38
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 25
- 239000007791 liquid phase Substances 0.000 claims description 24
- 239000007787 solid Substances 0.000 claims description 21
- 230000008018 melting Effects 0.000 claims description 17
- 238000002844 melting Methods 0.000 claims description 17
- 238000002425 crystallisation Methods 0.000 claims description 15
- 239000007790 solid phase Substances 0.000 claims description 14
- 230000008025 crystallization Effects 0.000 claims description 13
- 239000002002 slurry Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 8
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 claims 6
- 238000004064 recycling Methods 0.000 abstract description 8
- 238000011084 recovery Methods 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 36
- 238000000034 method Methods 0.000 description 28
- 239000000047 product Substances 0.000 description 16
- 238000001035 drying Methods 0.000 description 12
- 239000010446 mirabilite Substances 0.000 description 10
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 239000002904 solvent Substances 0.000 description 6
- 238000005119 centrifugation Methods 0.000 description 5
- 125000004122 cyclic group Chemical group 0.000 description 5
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 230000008014 freezing Effects 0.000 description 4
- 238000007710 freezing Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 235000010344 sodium nitrate Nutrition 0.000 description 4
- 239000004317 sodium nitrate Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 230000007547 defect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002440 industrial waste Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000035699 permeability Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 239000010812 mixed waste Substances 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
- 239000002910 solid waste Substances 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 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
- 239000012535 impurity Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000002689 soil 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
Images
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 waste salt separation, 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 of operations to obtain a solution containing residual sodium sulfate and all sodium chloride; and then, dissolving waste salt with sodium chloride being dominant in the solution, separating by a membrane separation system to obtain concentrated salt water and light salt water, and then evaporating, concentrating and crystallizing the two solutions respectively to finally obtain sodium sulfate crystals and sodium chloride crystals, thereby recycling 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 sodium sulfate and sodium chloride obtained by recovery can meet the requirements of industrial application, and the harmlessness, reduction and resource utilization of waste salt are fully realized.
Description
Technical Field
The invention relates to the field of industrial waste salt treatment, in particular to a comprehensive treatment device for waste salt separation.
Background
In recent years, with the rapid development of domestic economy, the industries such as petrifaction, coal chemical industry, pesticides, pharmacy, food, printing and dyeing and the like have also made great progress. In the development process of the industries, a large amount of high-salt wastewater is often generated, and the byproduct waste salt of the wastewater exceeds thousands of tons, most of the waste salt is not reasonably treated, so that great pressure is brought to the ecological environment and the social environment. The treatment of the waste salt in the industry generally has the defects of higher treatment cost, non-systematic treatment process, incomplete treatment, more dispersed treatment devices and the like. With the increasingly strict control of the country on the high-salt wastewater discharge enterprises, the establishment of a comprehensive waste salt disposal center is very necessary for protecting the natural environment and water resources on which people live. At present, the treatment method of the solid waste salt mainly comprises the following methods:
(1) burying method: the non-toxic, harmless, non-degradable and volatile solid waste salt is buried by selecting a proper geographical position;
(2) the burning method comprises the following steps: reducing and harmlessly treating waste salt by adopting high-temperature incineration;
(3) a dispersion treatment method: carrying out harmless treatment and salt separation treatment by each production enterprise according to the characteristics of industrial waste salt generated by the enterprise, and recycling the industrial waste salt;
comprehensively analyzing the three schemes, wherein the first scheme is only suitable for non-toxic and harmless waste salt disposal, and because reduction and resource treatment are not carried out, great pressure is caused on land resources due to long-term accumulation, and the surrounding soil is inevitably partially damaged; the second scheme has better adaptability to waste salt containing more combustible substances, particularly has better adaptability to waste salt containing single substance, and still has the problem of salt separation on complex waste salt containing multiple components; the third scheme is fragmentation and decentralized treatment, and has the characteristics of flexibility, strong applicability and the like, but has the defects of non-systematic process, 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 centralized comprehensive salt separation treatment on mixed waste salt with different contents of sodium chloride and sodium sulfate.
The invention is realized by the following technical scheme:
an integrated treatment device for waste salt and salt separation, comprising: the sodium sulfate separation system comprises 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 system comprises a sodium sulfate salt dissolving tank, a first brine delivery 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 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 sodium sulfate concentration device comprises a first sodium sulfate mother liquid tank, a first sodium sulfate mother liquid 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 liquid tank, the first sodium sulfate mother liquid 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 system comprises a sodium chloride salt dissolving tank, a second brine conveying pump, a second filter, a second brine buffer tank, a second brine pump, a cartridge filter, a high-pressure pump and a membrane separator which are connected in sequence; the membrane separator also comprises a concentrated water tank and a weak brine tank, wherein the concentrated water tank and the weak brine tank are respectively connected with the membrane separator; the precooler is connected with the sodium chloride salt dissolving tank; the second sodium sulfate separation system comprises: the concentrated water pump, the second cooler, the second nitrate crystallization kettle, the second nitrate centrifuge, the second nitrate melting tank, the second crystal slurry pump, the second sodium sulfate thickener, the second sodium sulfate centrifuge and the second sodium sulfate solid treatment device are sequentially connected; the second saltpeter mother liquid tank is connected to a liquid phase outlet of the second saltpeter centrifuge and is connected to the second saltpeter buffer tank through the second saltpeter mother liquid pump; the sodium sulfate evaporator comprises a sodium sulfate centrifuge, a sodium sulfate mother liquor pump, a first preheater and a first evaporation concentration device, wherein a liquid phase outlet of the sodium sulfate centrifuge and a top overflow port of the sodium sulfate thickener are connected into the sodium sulfate mother liquor tank; the second cooler is connected with the concentrated water tank; the sodium chloride separation system comprises: the system comprises a dilute brine pump, a dilute brine preheater, a third evaporation concentration device, a sodium chloride thickener, a sodium chloride centrifugal machine and a sodium chloride solid treatment device which are connected in sequence; the sodium chloride thickener is characterized by also comprising a sodium chloride mother liquid tank and a sodium chloride mother liquid pump, wherein a liquid phase outlet of the sodium chloride centrifuge and a top overflow port of the sodium chloride thickener are both connected into the sodium chloride mother liquid tank, and the sodium chloride mother liquid tank is connected into the light salt water tank through the sodium chloride mother liquid pump; the weak brine pump is connected with the weak brine tank.
Further, the first sodium sulfate solids treatment device comprises: the first sodium sulfate conveyor, the first sodium sulfate dryer, the second sodium sulfate conveyor and the first finished product sodium sulfate packer are connected in sequence; and the first sodium sulfate conveyor is connected with a solid phase outlet of the first sodium sulfate centrifugal machine.
Further, the first evaporation concentration apparatus includes: the system comprises a first falling film evaporator, a first steam compressor, a first circulating pump, a first condensate water tank and a first condensate water pump; the first preheater is connected to the first falling-film evaporator, a tube side liquid phase outlet of the first falling-film evaporator is connected to 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 steam compressor, an outlet of the first steam compressor is connected to a shell side steam inlet of the first falling-film evaporator, a shell side condensate outlet of the first falling-film evaporator is connected to 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: a third sodium sulfate conveyor, a second sodium sulfate dryer, a fourth sodium sulfate conveyor and a second finished product sodium sulfate packer which are connected in sequence; and the third sodium sulfate conveyor is connected with the solid phase outlet of the second sodium sulfate centrifugal machine.
Further, the second evaporation concentration apparatus includes: the second falling film evaporator, a second steam compressor, a second circulating pump, a second condensate water tank and a second condensate water pump; the second preheater is connected to in the second falling-film evaporator, the tube side liquid phase outlet of second falling-film evaporator passes through the second circulating pump and is connected to in the second sodium sulfate thickener, the tube side gas phase outlet of second falling-film evaporator is connected to the entry of second steam compressor, the export of second steam compressor is connected to simultaneously the shell side steam inlet of second falling-film evaporator, the shell side comdenstion water export of second falling-film evaporator is connected to in the second condensate water groove, the second condensate water groove warp the second condensate water pump is connected the second preheater.
Furthermore, the concentration multiple of sodium sulfate in the concentrated water tank is 1.5-3, and the content of sodium sulfate in the light brine tank is not higher than 0.5% (wt).
Further, the sodium chloride solids processing apparatus includes: the first sodium chloride conveyor, the sodium chloride dryer, the second sodium chloride conveyor and the finished product sodium chloride packing machine are connected in sequence; the first sodium chloride conveyor is connected with a solid phase outlet of the sodium chloride centrifugal machine.
Further, the third evaporation concentration apparatus includes: the third falling film evaporator, a third vapor compressor, a third circulating pump, a third condensate tank and a third condensate pump; the light salt brine preheater is connected into the third falling-film evaporator, a tube pass liquid phase outlet of the third falling-film evaporator is connected into the sodium chloride thickener through the third circulating pump, a tube pass gas phase outlet of the third falling-film evaporator is connected to an inlet of the third steam compressor, an outlet of the third steam compressor is simultaneously connected to a shell pass steam inlet of the third falling-film evaporator, a shell pass condensate water outlet of the third falling-film evaporator is connected into the third condensate water tank, and the third condensate water tank is connected to the light salt brine preheater through the third condensate water pump.
Further, the operation temperature of the first sodium nitrate crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the first sodium nitrate 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 nitrate crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the second nitrate 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 can achieve the following beneficial effects: (1) the sodium sulfate is produced by a freezing crystallization method by utilizing the characteristic that the solubility of the sodium sulfate is greatly reduced along with the reduction of the temperature at low temperature, so that the sodium sulfate is separated from the solution; (2) concentrating the divalent salt by adopting a membrane separation device according to different selective permeability of the monovalent salt and the divalent salt to the membrane; (3) mother liquor obtained by freezing and separating sodium sulfate-dominated waste salt is used as a solvent of sodium chloride-dominated waste salt, so that water resources are saved, sodium sulfate and sodium chloride in the mother liquor can be effectively recovered, and secondary waste salt is eliminated; (4) separating sodium chloride and sodium sulfate respectively by utilizing different solubilities when the sodium chloride and the sodium sulfate 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 distributed treatment, the method has the advantages that the waste salt dominated by sodium sulfate and the waste salt dominated by sodium chloride are subjected to centralized comprehensive treatment, 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 good social benefits are achieved; (7) the purity of the recovered sodium sulfate and sodium chloride can reach more than 98.5 percent, and the recovered sodium sulfate and sodium chloride can be directly sold to the outside, thereby having remarkable economic benefit.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention.
In the figure: 1. a sodium sulfate salt dissolving tank; 2. a first brine delivery 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 nitre crystallization kettle; 9. a first nitrate centrifuge; 10. a first nitre mother liquor tank; 11. a first saltpeter mother liquor pump; 12. a first saltpeter 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 product sodium sulfate packer; 28. a sodium chloride salt dissolving tank; 29. a second brine delivery 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 dilute brine tank; 37. a dense water tank; 38. a dilute brine pump; 39. a light brine preheater; 40. a third falling-film evaporator; 41. a third vapor compressor; 42. a third circulation pump; 43. a third condensate tank; 44. a third condensate pump; 45. a sodium chloride thickener; 46. a sodium chloride centrifuge; 47. a sodium chloride mother liquor tank; 48. a sodium chloride mother liquor pump; 49. a first sodium chloride conveyor; 50. a sodium chloride dryer; 51. a second sodium chloride conveyor; 52. packing machine for sodium chloride product; 53. a concentrate pump; 54. a second cooler; 55. a second nitrate crystallization kettle; 56. a second nitrate centrifuge; 57. a second nitre mother liquor tank; 58. a second saltpeter 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 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 a second finished product sodium sulfate packing machine.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the detailed description, and it should be noted that any combination of the embodiments or technical features described below can be used to form a new embodiment without conflict.
The invention provides a comprehensive treatment device for waste salt and a comprehensive treatment process for waste salt and salt separation, which can be used for carrying out concentrated comprehensive salt separation treatment on mixed waste salt of sodium chloride and sodium sulfate with different contents.
The raw material waste salt which is put into the treatment of the invention has two types: one is waste salt with sodium sulfate being dominant and sodium chloride being small, and the other is waste salt with sodium chloride being dominant and sodium sulfate being small. 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 of operations to obtain a solution containing residual sodium sulfate and all sodium chloride; and then, dissolving waste salt with sodium chloride being dominant in the solution, separating by a membrane separation system to obtain concentrated salt water and light salt water, and then evaporating, concentrating and crystallizing the two solutions respectively to finally obtain sodium sulfate crystals and sodium chloride crystals, thereby recycling 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 sodium sulfate and sodium chloride obtained by recovery can meet the requirements of industrial application, and the harmlessness, reduction and resource utilization of waste salt are fully realized. The invention has the advantages of small comprehensive energy consumption, good salt separation effect, high product quality, no secondary pollution, high comprehensive efficiency and the like.
Referring to fig. 1, the comprehensive treatment device for waste salt and sub-salt disclosed by the invention comprises: 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 dissolving tank comprises a sodium sulfate salt dissolving tank 1, a first brine conveying pump 2, a first filter 3, a first brine buffer tank 4, a first brine pump 5, a precooler 6, a first cooler 7, a first nitrate crystallization kettle 8, a first nitrate centrifuge 9, a first nitrate melting tank 12, a first crystal slurry pump 13, a first sodium sulfate thickener 14, a first sodium sulfate centrifuge 15 and a first sodium sulfate solid treatment device which are connected in sequence. In addition, the device also comprises a first saltpeter mother liquor tank 10 and a first saltpeter mother liquor pump 11, wherein the first saltpeter mother liquor tank 10 is connected to a liquid phase outlet of the first saltpeter centrifuge 9, and the first saltpeter melting tank 12 is connected to a solid phase outlet of the first saltpeter centrifuge 9; the first saltpeter mother liquor tank 10 is connected to an inlet at one side of the precooler 6 through a first saltpeter mother liquor pump 11, and the cold in the saltpeter mother liquor is recycled. In addition, still include first sodium sulfate mother liquor cistern 16, first sodium sulfate mother liquor pump 17, first preheater 18 and first evaporative 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 first sodium sulfate mother liquor cistern 16, first sodium sulfate mother liquor pump 16, first preheater 18 connect gradually, first preheater 18 reconnects to first evaporative concentration device department again, first evaporative concentration device still is connected with first sodium sulfate thickener 14 simultaneously, realize the circulation evaporative concentration of sodium sulfate solution. In addition, the precooler 6 is connected to an inlet of the sodium chloride salt dissolving 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 product sodium sulfate packer 27 which are connected in sequence; a first sodium sulfate conveyor 24 is connected to the solid phase outlet of the first sodium sulfate centrifuge 15.
Specifically, the first evaporation and concentration apparatus described above includes: a first falling-film evaporator 19, a first vapor compressor 20, a first circulation pump 21, a first condensate tank 22, and a first condensate pump 23. The first preheater 18 is connected into the first falling-film evaporator 19, a tube side liquid phase outlet of the first falling-film evaporator 19 is connected into the first sodium sulfate thickener 14 through a first circulating pump 21, a tube side gas phase outlet of the first falling-film evaporator 19 is connected to an inlet of a first steam compressor 20, an outlet of the first steam compressor 20 is simultaneously connected to a shell side steam inlet of the first falling-film evaporator 19, a shell side condensate outlet of the first falling-film evaporator 19 is connected into a first condensate water tank 22, and the first condensate water tank 22 is connected to an inlet on one side of the first preheater 18 through a first condensate water pump 23.
The process flow and the working principle of the first sodium sulfate separation system, i.e. the method for treating waste salt dominated by sodium sulfate, are explained in detail below:
waste salt (200-300 ℃) which is pre-treated and is mainly made of sodium sulfate and is removed of contained organic matters and pigments is put into a sodium sulfate salt dissolving tank 1 to be dissolved, a salt solution is pumped to a first filter 3 by a first brine delivery pump 2 to be filtered to remove impurities, the waste salt is kept still and buffered in a first brine buffer tank 4, then is sequentially pumped to a precooler 6 by a first brine pump 5 to be precooled to 25-30 ℃, is cooled to-5 ℃ in a first cooler 7, then is put into a first saltpeter crystallizing kettle 8 to be crystallized at-5 ℃, and then is centrifugally separated by a first saltpeter centrifuge 9 to obtain a saltpeter solution and saltpeter crystals.
The mirabilite solution obtained after centrifugal separation enters a first sodium nitrate mother liquor tank 10, is pumped into a precooler 6 by a first sodium nitrate mother liquor pump 11, then enters a sodium chloride salt dissolving tank 28, and is used as a solvent for dissolving waste salt dominated by sodium chloride. On the other hand, mirabilite crystals obtained after centrifugal separation enter a first nitrate melting tank 12 to be melted at 70-90 ℃, the melted fluid containing sodium sulfate crystals is pumped into a first sodium sulfate thickener 14 through a first crystal slurry pump 13 to be sufficiently crystallized and separated at 80-100 ℃, and then enters a first sodium sulfate centrifuge 15 to be centrifuged to obtain sodium sulfate mother liquor and sodium sulfate crystals.
The separated sodium sulfate crystals are discharged from a solid phase outlet of the first sodium sulfate centrifuge 15, conveyed into a first sodium sulfate dryer 25 by a first sodium sulfate conveyor 24 for drying, and then conveyed to a first finished product sodium sulfate packer 27 by a second sodium sulfate conveyor 26, so that the drying, packing and outward transportation of the solid sodium sulfate crystals are completed. On the other hand, the centrifuged sodium sulfate mother liquor enters the first sodium sulfate mother liquor tank 16, meanwhile, the mother liquor overflowing 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, preheated and then enters the first evaporation concentration device to perform cyclic evaporation concentration of the sodium sulfate mother liquor.
Preheating the sodium sulfate mother liquor to 85-95 ℃ in one side of a first preheater 18 by using steam condensate water, then feeding the sodium sulfate mother liquor into a first falling film evaporator 19, and carrying out evaporation concentration at 100-110 ℃; the secondary steam obtained by evaporation is compressed and upgraded by a first steam compressor 20, and then enters the shell side of the first falling-film evaporator 19 again to be used as a heat source for heating the sodium sulfate solution, so that the cyclic utilization of the steam is realized, and the condensed steam condensate enters the first steam condensate tank 22 and is pumped into the other side of the first preheater 18 through a first steam condensate pump 23 to preheat the sodium sulfate mother liquor, so that the recycling of energy is realized. And the concentrated solution obtained after evaporation concentration flows out from the bottom of the tube pass of the first falling-film evaporator 19, a part of the concentrated solution enters the first falling-film evaporator 19 again through the first circulating pump 21 to be circularly evaporated as a supplemented solution, the other part of the concentrated solution enters the first sodium sulfate thickener 14 to be thickened and crystallized, and then enters the first sodium sulfate centrifuge 15 to be centrifugally separated, the sodium sulfate mother solution obtained by centrifugation is preheated to be evaporated and concentrated again, so that the sodium sulfate crystals in the solution are finally and completely recovered through continuous circular concentration and evaporation.
It should be noted that the present invention only introduces a mechanical vapor recompression evaporation (MVR) process technology to achieve the purpose of evaporation concentration. In the actual evaporation concentration process, MVR, MED (multiple effect evaporation) and MSF (multiple effect flash evaporation) are used more in industrial application; the MVR has relatively lowest operation cost, but the MED is stable in operation, and the MSF is mostly used in the field of seawater desalination. In general, both MVR and MED can achieve the concentration requirements of the present disclosure, and any concentration technique that can meet the crystallization conditions required by the present disclosure falls within the scope of the present disclosure, regardless of the concentration technique. In addition, the drying process includes the process technologies such as normal pressure drying and vacuum drying, and whatever drying equipment and drying process are adopted, the drying process belongs to the protection scope of the invention as long as the aim of drying the centrifugally separated product to a qualified finished product can be achieved.
After the waste salt with sodium sulfate as the main component is treated by the first sodium sulfate separation system, high-purity sodium sulfate crystals and a mirabilite solution are finally obtained, and the mirabilite solution is used as a solvent of the waste salt with sodium chloride as the main component.
The membrane separation system includes: a sodium chloride salt dissolving 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; and the device also comprises a concentrated water tank 37 and a dilute brine tank 36, wherein the concentrated water tank 37 and the dilute brine tank 36 are respectively connected with the membrane separator 35. The sodium chloride salt dissolving tank 28 is connected to an outlet at one side of the precooler 6 in the first sodium sulfate separation system and is used for introducing a mirabilite solution. The filtration accuracy of second filter 30 is not more than 100 μm, and the filtration accuracy of security filter 33 is not more than 5 μm.
The process flow and the working principle of the membrane separation system, i.e. the membrane separation method of waste salt dominated by sodium chloride, are explained in detail below:
waste salt which is pre-treated and contains organic matters and pigment and is mainly sodium chloride at 200-300 ℃ is put into a sodium chloride salt dissolving tank 28, and the dissolved solvent is mirabilite solution from one side of the precooler 6 and a small amount of process water for supplementing insufficient solvent. After being mixed into the nitre mother liquor from the second nitre mother liquor tank 57, the saline solution is pumped to the second filter 30 for filtration by the second saltwater delivery pump 29, then enters the second saltwater buffer tank 31 for standing and buffering, is pumped into the security filter 33 for precise filtration by the second saltwater pump 32, and is pumped into the membrane separator 35 by the high-pressure pump 34 to realize salt separation at the temperature lower than 50 ℃. The divalent salt is concentrated by a membrane separator 35 by utilizing the difference in selective permeability of the monovalent salt and the divalent salt to the membrane, the separated concentrated water enters a concentrated water tank 37, and the separated weak brine enters a weak brine tank 36 to wait for the next crystallization treatment, respectively.
Wherein, after being separated by the membrane separator 35, the concentration multiple of sodium sulfate in the concentrated water tank 37 is 1.5-3, and the content of sodium sulfate in the light brine tank 36 is not higher than 0.5% (wt). It should be noted that, for the membrane separation process, whatever separation equipment and separation process are used, is within the scope of the present invention, as long as the concentration of the divalent salt to the multiple specified in the disclosure of the present invention can be achieved.
The second sodium sulfate separation system comprises: the system comprises a concentrated water pump 53, a second cooler 54, a second nitrate crystallizing kettle 55, a second nitrate centrifuge 56, a second nitrate melting tank 59, a second slurry pump 60, a second sodium sulfate thickener 61, a second sodium sulfate centrifuge 62 and a second sodium sulfate solid treatment device which are connected in sequence. In addition, a second saltpeter mother liquid tank 57 and a second saltpeter mother liquid pump 58 are also included, the second saltpeter mother liquid tank 57 is connected to a liquid phase outlet of the second saltpeter centrifuge 56, and a second saltpeter melting tank 59 is connected to a solid phase outlet of the second saltpeter centrifuge 56; the second saltpeter mother liquor tank 57 is connected to the second saltpeter buffer tank 31 through a second saltpeter mother liquor pump 58, so that the circulating separation of saltpeter mother liquor is realized. In addition, still include second sodium sulfate mother liquor cistern 63, second sodium sulfate mother liquor pump 64, second pre-heater 65 and second evaporative 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 cistern 63, second sodium sulfate mother liquor pump 64 is connected gradually with second pre-heater 65 one side entry, second pre-heater 65 one side export reconnection is to second evaporative concentration device department, second evaporative concentration device still is connected with second sodium sulfate thickener 61 simultaneously, realize the circulation evaporative concentration of sodium sulfate mother liquor. The second cooler 54 is connected to the concentrate tank 37 for introducing a sodium sulfate solution.
Specifically, the above-mentioned 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 product sodium sulfate packer 74 which are connected in sequence; 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 apparatus described above 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 into the second falling-film evaporator 66, a tube side liquid phase outlet of the second falling-film evaporator 66 is connected into the second sodium sulfate thickener 61 through a second circulating pump 70, a tube side gas phase outlet of the second falling-film evaporator 66 is connected to an inlet of a second steam compressor 67, an outlet of the second steam compressor 67 is simultaneously connected to a shell side steam inlet of the second falling-film evaporator 66, a shell side condensate outlet of the second falling-film evaporator 66 is connected into a second condensate water tank 68, and the second condensate water tank 68 is connected to an inlet on the other side of the second preheater 65 through a second condensate water pump 69.
The process flow and the working principle of the second sodium sulfate separation system, namely the treatment method of the concentrated water, are explained in detail as follows:
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 ℃, then enters a second nitrate crystallization kettle 55 to be crystallized at the temperature of-5 ℃, and then is separated by a second nitrate centrifuge 56 to obtain mirabilite solution and mirabilite crystals. The mirabilite solution obtained after centrifugation enters a second saltpeter mother liquor tank 57 and is pumped back to the second saltpeter buffer tank 31 by a second saltpeter mother liquor pump 58 for circular separation; on the other hand, mirabilite crystals obtained after centrifugation enter a second nitrate melting tank 59 to be melted at 70-90 ℃, fluid containing sodium sulfate crystals obtained after melting is pumped into a second sodium sulfate thickener 61 through a second slurry pump 60 to be fully crystallized and separated at 80-100 ℃, and then enters a second sodium sulfate centrifuge 62 to be centrifuged to obtain sodium sulfate mother liquor and sodium sulfate crystals.
The separated sodium sulfate crystals are discharged from a solid phase outlet of the second sodium sulfate centrifuge 62, conveyed into a second sodium sulfate dryer 72 by a third sodium sulfate conveyor 71 for drying treatment, and then conveyed to a second finished product sodium sulfate packer 74 by the third sodium sulfate conveyor 71, so that the drying, packing and outward transportation treatment of the solid sodium sulfate crystals are completed. On the other hand, the sodium sulfate mother liquor obtained after centrifugation enters the second sodium sulfate mother liquor tank 63, meanwhile, the mother liquor overflowing 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 and concentration device through the second sodium sulfate mother liquor pump 64 to perform cyclic evaporation and concentration of the sodium sulfate mother liquor.
Preheating the sodium sulfate mother liquor to 85-95 ℃ in a second preheater 65 by using steam condensate water, then entering a second falling film evaporator 66, and carrying out evaporation concentration at 100-110 ℃; the secondary steam obtained by evaporation is compressed and upgraded by a second steam compressor 67, and then enters the shell pass of the second falling-film evaporator 66 again to be used as a heat source for heating the sodium sulfate solution, so that the cyclic utilization of the steam is realized, and 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 to be used for preheating the sodium sulfate mother liquor, so that the recycling of energy is realized. And the concentrated solution obtained after evaporation 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 circularly evaporated as a supplementary solution, the other part of the concentrated solution is pumped into the second sodium sulfate thickener 61 to be thickened and crystallized, and then the thickened and crystallized solution enters the second sodium sulfate centrifuge 62 to be separated again, so that the sodium sulfate solution is continuously circularly evaporated, concentrated and crystallized, and the sodium sulfate crystals in the solution are completely recovered.
The sodium chloride separation system comprises: a weak brine pump 38, a weak brine preheater 39, a third evaporation concentration device, a sodium chloride thickener 45, a sodium chloride centrifuge 46 and a sodium chloride solid treatment device which are connected in sequence. In addition, a sodium chloride mother liquor tank 47 and a sodium chloride mother liquor pump 48 are also included, a liquid phase outlet of the sodium chloride centrifuge 46 and a top overflow port of the sodium chloride thickener 45 are both connected into the sodium chloride mother liquor tank 47, and the sodium chloride mother liquor tank 47 is connected into the weak brine tank 36 through the sodium chloride mother liquor pump 48; a saline pump 38 is connected to the saline 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 product sodium chloride packer 52 which are 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 apparatus includes: a third falling-film evaporator 40, a third vapor compressor 41, a third circulation pump 42, a third condensate tank 43, and a third condensate pump 44. The fresh brine preheater 39 is connected into the third falling-film evaporator 40, a tube-side liquid-phase outlet of the third falling-film evaporator 40 is connected into the sodium chloride thickener 45 through a third circulating pump 42, a tube-side gas-phase outlet of the third falling-film evaporator 40 is connected to an inlet of a third steam compressor 41, an outlet of the third steam compressor 41 is simultaneously connected to a shell-side steam inlet of the third falling-film evaporator 40, a shell-side condensate outlet of the third falling-film evaporator 40 is connected into a third condensate water tank 43, and the third condensate water tank 43 is connected to an inlet on one side of the fresh brine preheater 39 through a third condensate water pump 44.
The process flow and the working principle of the sodium chloride separation system, namely the treatment method of the dilute brine, are explained in detail as follows:
mixing the dilute brine from the dilute brine tank 36 and the sodium chloride mother liquor from the sodium chloride mother liquor tank 47, pumping the mixture to one side of a dilute brine preheater 39 through a dilute brine pump 38, preheating the mixture to 70-80 ℃ through steam condensate, and then entering a 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, enters the third falling-film evaporator 40 again to be used as a heat source for heating the sodium chloride solution, so that the cyclic utilization of the steam is realized, and 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 to be used for preheating the sodium chloride solution, so that the recycling of energy is realized. And the concentrated solution obtained after evaporation concentration flows out from 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 a third circulating pump 42 to be circularly evaporated as a supplementary solution, the other part of the concentrated solution is pumped into a sodium chloride thickener 45 to be cooled, crystallized and separated at the temperature of 40-50 ℃, and the fluid containing sodium chloride crystals and discharged from the bottom of the sodium chloride thickener 45 enters a sodium chloride centrifuge 46 to be centrifuged to obtain sodium chloride mother liquor and sodium chloride crystals.
The separated sodium chloride crystals are discharged from a solid phase outlet of the sodium chloride centrifuge 46, conveyed into a sodium chloride dryer 50 by a first sodium chloride conveyor 49 for drying treatment, and then conveyed to a finished product sodium chloride packing machine 52 by a second sodium chloride conveyor 51 to complete the drying, packing and outward transportation treatment of the solid sodium chloride crystals. On the other hand, the sodium chloride mother liquor obtained after centrifugation enters the sodium chloride mother liquor tank 47, meanwhile, the mother liquor overflowing 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 weak brine tank 36 again through the sodium chloride mother liquor pump 48 to perform the circulating separation and the evaporation concentration of the sodium chloride mother liquor. Through continuous circulation separation and evaporation concentration, sodium chloride crystals in the solution are completely recovered.
After the four steps, the sodium sulfate and the sodium chloride in the waste salt with different compositions are respectively separated, and the purity of the sodium sulfate and the sodium chloride can reach more than 98.5 percent, thereby completely meeting the industrial requirement. In the whole treatment process, no secondary waste salt is generated, thereby reducing secondary pollution. Because no volatile component exists in the pretreated waste salt, the steam condensate obtained by evaporation can be directly and completely reused as process water, and the effect of zero discharge of waste water is realized.
In addition, the process adopts a vapor recompression technology, so that steam is hardly consumed. The comprehensive power consumption of the product per ton is only about 250 kilowatt hours.
By way of detailed explanation of the above embodiments, it can be understood that the present invention: (1) the sodium sulfate is produced by a freezing crystallization method by utilizing the characteristic that the solubility of the sodium sulfate is greatly reduced along with the reduction of the temperature at low temperature, so that the sodium sulfate is separated from the solution; (2) concentrating the divalent salt by adopting a membrane separation device according to different selective permeability of the monovalent salt and the divalent salt to the membrane; (3) mother liquor obtained by freezing and separating sodium sulfate-dominated waste salt is used as a solvent of sodium chloride-dominated waste salt, so that water resources are saved, sodium sulfate and sodium chloride in the mother liquor can be effectively recovered, and secondary waste salt is eliminated; (4) separating sodium chloride and sodium sulfate respectively by utilizing different solubilities when the sodium chloride and the sodium sulfate 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 distributed treatment, the method has the advantages that the waste salt dominated by sodium sulfate and the waste salt dominated by sodium chloride are subjected to centralized comprehensive treatment, 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 good social benefits are achieved; (7) the purity of the recovered sodium sulfate and sodium chloride can reach more than 98.5 percent, and the recovered sodium sulfate and sodium chloride can be directly sold to the outside, thereby having remarkable economic benefit.
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Claims (10)
1. The utility model provides a comprehensive processing apparatus of salt is divided to waste salt which characterized in that includes: the sodium sulfate separation system comprises 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 system comprises a sodium sulfate salt dissolving tank, a first brine delivery 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 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 sodium sulfate concentration device comprises a first sodium sulfate mother liquid tank, a first sodium sulfate mother liquid 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 liquid tank, the first sodium sulfate mother liquid 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 system comprises a sodium chloride salt dissolving tank, a second brine conveying pump, a second filter, a second brine buffer tank, a second brine pump, a cartridge filter, a high-pressure pump and a membrane separator which are connected in sequence; the membrane separator also comprises a concentrated water tank and a weak brine tank, wherein the concentrated water tank and the weak brine tank are respectively connected with the membrane separator;
the precooler is connected with the sodium chloride salt dissolving tank;
the second sodium sulfate separation system comprises: the concentrated water pump, the second cooler, the second nitrate crystallization kettle, the second nitrate centrifuge, the second nitrate melting tank, the second crystal slurry pump, the second sodium sulfate thickener, the second sodium sulfate centrifuge and the second sodium sulfate solid treatment device are sequentially connected; the second saltpeter mother liquid tank is connected to a liquid phase outlet of the second saltpeter centrifuge and is connected to the second saltpeter buffer tank through the second saltpeter mother liquid pump; the sodium sulfate evaporator comprises a sodium sulfate centrifuge, a sodium sulfate mother liquor pump, a first preheater and a first evaporation concentration device, wherein a liquid phase outlet of the sodium sulfate centrifuge and a top overflow port of the sodium sulfate thickener are connected into the sodium sulfate mother liquor tank;
the second cooler is connected with the concentrated water tank;
the sodium chloride separation system comprises: the system comprises a dilute brine pump, a dilute brine preheater, a third evaporation concentration device, a sodium chloride thickener, a sodium chloride centrifugal machine and a sodium chloride solid treatment device which are connected in sequence; the sodium chloride thickener is characterized by also comprising a sodium chloride mother liquid tank and a sodium chloride mother liquid pump, wherein a liquid phase outlet of the sodium chloride centrifuge and a top overflow port of the sodium chloride thickener are both connected into the sodium chloride mother liquid tank, and the sodium chloride mother liquid tank is connected into the light salt water tank through the sodium chloride mother liquid pump;
the weak brine pump is connected with the weak brine tank.
2. The integrated waste salt treatment plant of claim 1, wherein the first sodium sulfate solids treatment plant comprises: the first sodium sulfate conveyor, the first sodium sulfate dryer, the second sodium sulfate conveyor and the first finished product sodium sulfate packer are connected in sequence; and the first sodium sulfate conveyor is connected with a solid phase outlet of the first sodium sulfate centrifugal machine.
3. The integrated waste salt treatment apparatus of claim 1, wherein the first evaporative concentration apparatus comprises: the system comprises a first falling film evaporator, a first steam compressor, a first circulating pump, a first condensate water tank and a first condensate water pump; the first preheater is connected to the first falling-film evaporator, a tube side liquid phase outlet of the first falling-film evaporator is connected to 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 steam compressor, an outlet of the first steam compressor is connected to a shell side steam inlet of the first falling-film evaporator, a shell side condensate outlet of the first falling-film evaporator is connected to 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 plant of claim 1, wherein the second sodium sulfate solids treatment plant comprises: a third sodium sulfate conveyor, a second sodium sulfate dryer, a fourth sodium sulfate conveyor and a second finished product sodium sulfate packer which are connected in sequence; and the third sodium sulfate conveyor is connected with the solid phase outlet of the second sodium sulfate centrifugal machine.
5. The integrated waste salt treatment apparatus of claim 1, wherein the second evaporation and concentration apparatus comprises: the second falling film evaporator, a second steam compressor, a second circulating pump, a second condensate water tank and a second condensate water pump; the second preheater is connected to in the second falling-film evaporator, the tube side liquid phase outlet of second falling-film evaporator passes through the second circulating pump and is connected to in the second sodium sulfate thickener, the tube side gas phase outlet of second falling-film evaporator is connected to the entry of second steam compressor, the export of second steam compressor is connected to simultaneously the shell side steam inlet of second falling-film evaporator, the shell side comdenstion water export of second falling-film evaporator is connected to in the second condensate water groove, the second condensate water groove warp the second condensate water pump is connected the second preheater.
6. The integrated waste salt treatment apparatus according to claim 1, wherein the concentration ratio of sodium sulfate in the concentrated water tank is 1.5-3, and the content of sodium sulfate in the dilute brine tank is not higher than 0.5% (wt).
7. The integrated waste salt treatment apparatus of 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 product sodium chloride packing machine are connected in sequence; the first sodium chloride conveyor is connected with a solid phase outlet of the sodium chloride centrifugal machine.
8. The integrated waste salt treatment apparatus of claim 1, wherein the third evaporation and concentration apparatus comprises: the third falling film evaporator, a third vapor compressor, a third circulating pump, a third condensate tank and a third condensate pump; the light salt brine preheater is connected into the third falling-film evaporator, a tube pass liquid phase outlet of the third falling-film evaporator is connected into the sodium chloride thickener through the third circulating pump, a tube pass gas phase outlet of the third falling-film evaporator is connected to an inlet of the third steam compressor, an outlet of the third steam compressor is simultaneously connected to a shell pass steam inlet of the third falling-film evaporator, a shell pass condensate water outlet of the third falling-film evaporator is connected into the third condensate water tank, and the third condensate water tank is connected to the light salt brine preheater through the third condensate water pump.
9. The integrated waste salt treatment apparatus according to claim 1, wherein the operation temperature of the first saltpeter crystallization kettle is between-5 ℃ and 5 ℃, the operation temperature of the first saltpeter melting tank is between 70 ℃ and 90 ℃, and the operation temperature of the first sodium sulfate thickener is between 80 ℃ and 100 ℃.
10. The integrated waste salt treatment apparatus according to claim 1, wherein the second nitrate crystallizing tank is operated at a temperature of-5 ℃ to 5 ℃, the second nitrate melting tank is operated at a temperature of 70 ℃ to 90 ℃, and the second sodium sulfate thickener is operated at a temperature of 80 ℃ to 100 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911214100.3A CN111153417B (en) | 2019-12-02 | 2019-12-02 | Comprehensive treatment device for separating salt from waste salt |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911214100.3A CN111153417B (en) | 2019-12-02 | 2019-12-02 | Comprehensive treatment device for separating salt from waste salt |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111153417A true CN111153417A (en) | 2020-05-15 |
| CN111153417B CN111153417B (en) | 2024-06-25 |
Family
ID=70556309
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911214100.3A Active CN111153417B (en) | 2019-12-02 | 2019-12-02 | Comprehensive treatment device for separating salt from waste salt |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111153417B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112079515A (en) * | 2020-10-12 | 2020-12-15 | 江苏迈安德节能蒸发设备有限公司 | Method for recycling TDI industrial wastewater |
| CN114368763A (en) * | 2021-12-28 | 2022-04-19 | 华夏碧水环保科技有限公司 | Comprehensive treatment method for industrial waste salt |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105254099A (en) * | 2015-10-22 | 2016-01-20 | 东华工程科技股份有限公司 | High-purity crystallization and salt-withdrawal process for coal chemical industry high-salinity waste water |
| CN105461134A (en) * | 2015-12-01 | 2016-04-06 | 陕西省石油化工研究设计院 | Technology and device applied to recycling of high-salinity wastewater in coal chemical industry |
| CN105523676A (en) * | 2015-12-23 | 2016-04-27 | 倍杰特国际环境技术股份有限公司 | High-salt wastewater zero-discharge evaporation crystallization salt substance-division method |
| CN105585194A (en) * | 2016-01-07 | 2016-05-18 | 王文领 | Comprehensive utilization method of high-concentration waste saline water containing Na<+>, Ka<+>, NH<4+>, Cl<->, SO4<2-> and NO<3-> in coal chemical industry |
| US20160368783A1 (en) * | 2015-06-22 | 2016-12-22 | Eureka Resources, Llc | Method and System for Treating Wastewater |
| WO2017181696A1 (en) * | 2016-04-21 | 2017-10-26 | 广州市心德实业有限公司 | Method for treating and recycling brine wastewater containing sodium chloride and sodium sulfate |
| CN108203197A (en) * | 2015-12-23 | 2018-06-26 | 倍杰特国际环境技术股份有限公司 | A kind of processing system of brine waste |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN109292797A (en) * | 2018-11-02 | 2019-02-01 | 江苏中圣高科技产业有限公司 | A kind of brine waste sub-prime recovery method |
| CN110040908A (en) * | 2019-04-22 | 2019-07-23 | 天津科技大学 | A kind of sodium chloride and sodium sulphate ultrasonic type evaporative crystallization divide salt system and method |
| CN212198525U (en) * | 2019-12-02 | 2020-12-22 | 广州维港环保科技有限公司 | Comprehensive treatment device for waste salt separation |
| CN113880115A (en) * | 2021-10-09 | 2022-01-04 | 江苏迈安德节能蒸发设备有限公司 | Production method for separating and refining waste miscellaneous salt containing sodium chloride and sodium sulfate |
-
2019
- 2019-12-02 CN CN201911214100.3A patent/CN111153417B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20160368783A1 (en) * | 2015-06-22 | 2016-12-22 | Eureka Resources, Llc | Method and System for Treating Wastewater |
| CN105254099A (en) * | 2015-10-22 | 2016-01-20 | 东华工程科技股份有限公司 | High-purity crystallization and salt-withdrawal process for coal chemical industry high-salinity waste water |
| CN105461134A (en) * | 2015-12-01 | 2016-04-06 | 陕西省石油化工研究设计院 | Technology and device applied to recycling of high-salinity wastewater in coal chemical industry |
| CN105523676A (en) * | 2015-12-23 | 2016-04-27 | 倍杰特国际环境技术股份有限公司 | High-salt wastewater zero-discharge evaporation crystallization salt substance-division method |
| CN108203197A (en) * | 2015-12-23 | 2018-06-26 | 倍杰特国际环境技术股份有限公司 | A kind of processing system of brine waste |
| CN105585194A (en) * | 2016-01-07 | 2016-05-18 | 王文领 | Comprehensive utilization method of high-concentration waste saline water containing Na<+>, Ka<+>, NH<4+>, Cl<->, SO4<2-> and NO<3-> in coal chemical industry |
| WO2017181696A1 (en) * | 2016-04-21 | 2017-10-26 | 广州市心德实业有限公司 | Method for treating and recycling brine wastewater containing sodium chloride and sodium sulfate |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN109292797A (en) * | 2018-11-02 | 2019-02-01 | 江苏中圣高科技产业有限公司 | A kind of brine waste sub-prime recovery method |
| CN110040908A (en) * | 2019-04-22 | 2019-07-23 | 天津科技大学 | A kind of sodium chloride and sodium sulphate ultrasonic type evaporative crystallization divide salt system and method |
| CN212198525U (en) * | 2019-12-02 | 2020-12-22 | 广州维港环保科技有限公司 | Comprehensive treatment device for waste salt separation |
| CN113880115A (en) * | 2021-10-09 | 2022-01-04 | 江苏迈安德节能蒸发设备有限公司 | Production method for separating and refining waste miscellaneous salt containing sodium chloride and sodium sulfate |
Non-Patent Citations (1)
| Title |
|---|
| 熊日华等: "高盐废水分盐结晶工艺及其技术经济分析", 煤炭科学技术, vol. 46, no. 9, pages 37 - 43 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112079515A (en) * | 2020-10-12 | 2020-12-15 | 江苏迈安德节能蒸发设备有限公司 | Method for recycling TDI industrial wastewater |
| CN114368763A (en) * | 2021-12-28 | 2022-04-19 | 华夏碧水环保科技有限公司 | Comprehensive treatment method for industrial waste salt |
| CN114368763B (en) * | 2021-12-28 | 2024-04-30 | 华夏碧水环保科技股份有限公司 | Comprehensive treatment method for industrial waste salt |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111153417B (en) | 2024-06-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109292797B (en) | Method for recycling salt-containing wastewater according to quality | |
| CN106495384B (en) | Process for preparing industrial refined salt by utilizing organic pollution high-salinity wastewater | |
| CN107867707A (en) | The sodium sulfate in high purity and the sub-prime method for crystallising of sodium chloride that extraction resourcebility utilizes from high-salt wastewater | |
| WO2006094437A1 (en) | A method and an multi-effect evaporation for waste water of alkylene oxides | |
| CN105502438B (en) | The highly concentrated saline treatment method and apparatus of coal chemical industry | |
| CN113149059B (en) | Method and system for crystallization separation of fly ash water washing liquid and separation and purification of sodium salt and potassium salt based on seed crystal method | |
| CN104926011B (en) | The evaporative crystallization zero-discharge treatment system and processing method of a kind of high-COD waste water | |
| CN113105138A (en) | Method and system for water washing dechlorination of waste incineration fly ash and evaporation mass-separation crystallization of water washing liquid | |
| CN209367818U (en) | A kind of brine waste sub-prime recovery system | |
| CN113880115B (en) | Waste salt separating and refining production method containing sodium chloride and sodium sulfate | |
| CN110577311A (en) | Method for treating and recycling waste mixed salt containing organic matters | |
| CN111153417B (en) | Comprehensive treatment device for separating salt from waste salt | |
| CN111977733A (en) | Complete device and process for recycling salt or nitrate from high-salinity wastewater through fractional crystallization | |
| CN212559531U (en) | Complete equipment for recycling salt or nitrate from high-salinity wastewater by means of fractional crystallization | |
| CN112456710A (en) | Method for recycling high-value materials from chemical wastewater | |
| CN109354041A (en) | A method of extracting potassium from flying dust water lotion | |
| CN212198525U (en) | Comprehensive treatment device for waste salt separation | |
| CN214570788U (en) | High basicity strong brine zero release processing system | |
| CN113493213A (en) | Process and equipment for recycling and zero discharge of wastewater containing sodium chloride and sodium sulfate | |
| CN111484180B (en) | Waste heat method recrystallization purification mode and system for zero-emission associated crystallization salt of sewage | |
| CN112299613A (en) | Zero-emission process system for sewage treatment | |
| CN107597795B (en) | System and method for recycling and treating household garbage incineration fly ash | |
| CN209507610U (en) | High-salt wastewater divides salt system | |
| CN112321048A (en) | Three-stage countercurrent evaporation salt separation system and method for high-salt-content wastewater | |
| CN113149058B (en) | Method for water washing and dechlorination of fly ash and recycling of water washing liquid and system for realizing method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |