CN115321559A - Device and method for producing high-concentration sodium sulfate solution by adopting nanofiltration membrane concentration technology - Google Patents
Device and method for producing high-concentration sodium sulfate solution by adopting nanofiltration membrane concentration technology Download PDFInfo
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- CN115321559A CN115321559A CN202211034447.1A CN202211034447A CN115321559A CN 115321559 A CN115321559 A CN 115321559A CN 202211034447 A CN202211034447 A CN 202211034447A CN 115321559 A CN115321559 A CN 115321559A
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- 238000001728 nano-filtration Methods 0.000 title claims abstract description 180
- 239000012528 membrane Substances 0.000 title claims abstract description 147
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims abstract description 42
- 229910052938 sodium sulfate Inorganic materials 0.000 title claims abstract description 38
- 235000011152 sodium sulphate Nutrition 0.000 title claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000005516 engineering process Methods 0.000 title claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 184
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 98
- 239000011780 sodium chloride Substances 0.000 claims abstract description 48
- 239000012267 brine Substances 0.000 claims abstract description 42
- 150000003839 salts Chemical class 0.000 claims abstract description 42
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 42
- 239000011734 sodium Substances 0.000 claims abstract description 30
- 239000000243 solution Substances 0.000 claims abstract description 21
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 11
- 150000002500 ions Chemical class 0.000 claims abstract description 11
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- 230000008020 evaporation Effects 0.000 claims abstract description 8
- 239000003513 alkali Substances 0.000 claims abstract description 7
- 238000002425 crystallisation Methods 0.000 claims abstract description 6
- 230000008025 crystallization Effects 0.000 claims abstract description 6
- 229910002651 NO3 Inorganic materials 0.000 claims description 22
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 11
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 10
- 230000004907 flux Effects 0.000 claims description 10
- 238000004064 recycling Methods 0.000 claims description 10
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 8
- 235000010265 sodium sulphite Nutrition 0.000 claims description 8
- 238000010612 desalination reaction Methods 0.000 claims description 7
- 238000006722 reduction reaction Methods 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 claims description 6
- 235000019345 sodium thiosulphate Nutrition 0.000 claims description 6
- 238000000502 dialysis Methods 0.000 claims description 4
- 239000010446 mirabilite Substances 0.000 claims description 4
- 239000003638 chemical reducing agent Substances 0.000 claims description 3
- 230000035699 permeability Effects 0.000 claims description 3
- 230000001502 supplementing effect Effects 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 238000001556 precipitation Methods 0.000 abstract description 3
- 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 abstract 1
- 229910052708 sodium Inorganic materials 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 239000013078 crystal Substances 0.000 description 4
- 238000004090 dissolution Methods 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 239000012466 permeate Substances 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 150000004691 decahydrates Chemical class 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000002823 nitrates Chemical class 0.000 description 2
- 235000010333 potassium nitrate Nutrition 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical group [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 239000007832 Na2SO4 Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- -1 manometer 7 Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- RSIJVJUOQBWMIM-UHFFFAOYSA-L sodium sulfate decahydrate Chemical compound O.O.O.O.O.O.O.O.O.O.[Na+].[Na+].[O-]S([O-])(=O)=O RSIJVJUOQBWMIM-UHFFFAOYSA-L 0.000 description 1
- XZPVPNZTYPUODG-UHFFFAOYSA-M sodium;chloride;dihydrate Chemical compound O.O.[Na+].[Cl-] XZPVPNZTYPUODG-UHFFFAOYSA-M 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 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
- C01D5/16—Purification
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/027—Nanofiltration
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Nanotechnology (AREA)
- Water Supply & Treatment (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the technical field of separation of sodium sulfate from weak brine after ionic membrane electrolysis in the chlor-alkali industry, in particular to a device and a method for producing a high-concentration sodium sulfate solution by adopting a nanofiltration membrane concentration technology. The invention increases Na content by concentrating section by arranging the first-section nanofiltration membrane device, the second-section nanofiltration membrane device and the third-section nanofiltration membrane device 2 SO 4 Concentration, by arranging a pure water tank, a pure water high-pressure pump and a special high-pressure nanofiltration membrane element and utilizing the separation characteristic of the nanofiltration membrane for intercepting ions with more than two valences, the total salt concentration of sodium sulfate and sodium chloride at the side of nanofiltration concentrated water is reduced, salt precipitation and scaling are reduced, the nanofiltration membrane element is blocked, and therefore, the high-concentration sodium sulfate is increased to 150-160g/L, the multi-effect evaporation and crystallization energy consumption is reduced by more than 50%, and the sodium sulfateThe yield is more than 88.4 percent. Meanwhile, the nanofiltration device is used for recovering energy, so that the energy consumption can be reduced by 35%.
Description
Technical Field
The invention relates to the technical field of sodium sulfate separation in dilute brine after ionic membrane electrolysis in the chlor-alkali industry, in particular to a device and a method for producing a high-concentration sodium sulfate solution by adopting a nanofiltration membrane concentration technology.
Background
In the chlor-alkali industry, raw salt is used as a raw material to produce industrial alkali, chlorine and other products, but the raw salt of a natural mine contains impurities such as associated mine sodium sulfate and the like, na 2 SO 4 Continuously enriching Na in brine in the production process of an ion membrane caustic soda device 2 SO 4 The accumulation of (a) can lead to the formation of deposits on the electrode surfaces in the electrolyzer, which increases the energy consumption (higher voltage) and reduces the service life of the very expensive electrodes and of the chloride ion exchange membranes in the membrane electrolysis process;
at present, na in weak brine (NaCl =210 +/-10 g/L) after ionic membrane electrolysis is removed by membrane method and freezing 2 SO 4 And the water produced by the nanofiltration membrane device (namely poor nitrate water, naCl =210 +/-10 g/L, na) 2 SO 4 Less than 1 g/L) to dissolve sodium chloride or injecting into mine for continuous production, and nanofiltration membrane concentrated water (namely high-nitrate water, naCl =205 +/-10 g/L, na) 2 SO 4 Content of 60g-88 g/L) Na after freezing a crystallizer 2 SO 4 Using sodium sulfate decahydrate crystal (Na) 2 SO 4 ·10H 2 O) settled down and the mother liquor after denitration (NaCl =205 ± g/L, na) 2 SO 4 Less than 5 g/L) and nanofiltration refined poor saltpeter water, and the decahydrate crystal slurry is centrifugally separated to obtain a decahydrate solid, but the mirabilite product contains crystal water, the application range is narrow, the saltpeter is not well sold, the industrial utilization value is not high, and the resource waste is serious.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a device and a method for producing a high-concentration sodium sulfate solution by adopting a nanofiltration membrane concentration technology, which solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme: the method for producing the high-concentration sodium sulfate solution by adopting the nanofiltration membrane concentration technology comprises the following steps:
the first step is as follows: the temperature of the light brine is reduced from 60-70 ℃ to 40 +/-3 ℃ by pretreating the light brine (the content of sodium chloride is controlled to be 210 +/-10 g/L and the content of sodium sulfate is less than 20 g/L) after the ion membrane electrolysis in the chlor-alkali industry;
the second step is that: adding a reducing agent (sodium thiosulfate or sodium sulfite) according to the content of the light brine (1 ton of brine and 0.1Kg of sodium thiosulfate or sodium sulfite), and removing the sodium hypochlorite remained in the electrolytic process by using a reduction reaction;
the third step: after passing through an activated carbon filter, the sodium hypochlorite enters a first-stage nanofiltration device (the nanofiltration membrane has selective permeability to divalent ions), the dilute brine component NaCl =210 +/-10 g/L and Na2SO4 is less than 20g/L, the operating pressure of the first-stage nanofiltration membrane device, the second-stage nanofiltration membrane device and the third-stage nanofiltration membrane device is 20-28Bar, the first-stage nanofiltration recovery rate is 60-85%, the flux of nanofiltration membrane elements is 18-25L/m2.H, the separated lean dilute brine NaCl =210 +/-10 g/L and Na is 2 SO 4 Less than 1g/L, directly entering a production process to dissolve raw salt or injecting the raw salt into an underground mine for recycling;
the fourth step: high-nitrate concentrated brine NaCl =205 +/-10 g/L and Na of primary nanofiltration device 2 SO 4 The concentration of 60-88g/L enters a super concentration nanofiltration device, the super concentration nanofiltration device comprises a first-stage nanofiltration membrane device, a second-stage nanofiltration membrane device and a third-stage nanofiltration membrane device, the operating pressure is 55-60Bar, the flux of a high-pressure nanofiltration membrane element is 12-18L/m2.H, 1/3 of pure water dialysis sodium chloride is supplemented during concentration to improve the mass ratio of sodium sulfate, the total salt concentration of the sodium sulfate and the sodium chloride at the nanofiltration concentrated water side is reduced, and therefore the high concentration of the sodium sulfate to 150-160g/L and the NaCl content to be less than 150g/L are achieved. After separation, the NaCl of the lean nitre dilute brine is more than 150g/L and Na 2 SO 4 Less than 5g/L, directly entering the production process to dissolve the original salt or injecting the original salt into an underground mine for recycling;
the fifth step: the concentrated solution high-nitrate water of the super concentration nanofiltration device enters direct MVR evaporation crystallization to produce high-purity Na 2 SO 4 Mirabilite product.
As a preferred technical scheme of the invention, the device for producing the high-concentration sodium sulfate solution by adopting the nanofiltration membrane concentration technology comprises a primary nanofiltration concentrated water tank, a high-pressure pump, a pure water tank and a pure water high-pressure pump, and is characterized in that: the device comprises a high-pressure pump, a valve behind the high-pressure pump, a pressure gauge, a low-nitrate water desalination tank, a high-pressure nanofiltration membrane element, a low-nitrate water desalination device, a high-pressure nanofiltration membrane element, a high-pressure water production flowmeter, a low-nitrate water desalination device, a low-nitrate water recovery device, a high-pressure nanofiltration membrane element, a high-pressure water recovery device and a high-pressure water recovery device.
As a preferred technical scheme of the invention, both ends of the primary nanofiltration concentrated water tank are provided with valves, the rear end of the valve far away from the water inlet of the primary nanofiltration concentrated water tank is provided with a water supply pump, the water outlet end of the water supply pump is provided with a security filter, both ends of the security filter are provided with pressure gauges, the water outlet end of the security filter is provided with a high-pressure pump, a valve is arranged between the high-pressure pump and the security filter, and the water outlet end of the high-pressure pump is provided with a valve.
As a preferable technical scheme of the invention, valves are arranged at two ends of the pure water tank, a pure water supply pump is arranged at the rear end of the valve far away from the water inlet end of the pure water tank, a security filter is arranged at the rear end of the pure water supply pump, pressure gauges are fixedly arranged at two ends of the security filter, a pure water high-pressure pump is arranged at the water outlet end of the security filter, and a valve is arranged at the water outlet end of the high-pressure pump.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention is provided with a first-stage nanofiltration membrane device, a second-stage nanofiltration membrane device and a third-stage nanofiltration membrane deviceThe nanofiltration membrane device is characterized in that pure water brine is respectively supplemented by three sections of feed inlets to ensure that concentrated water (NaCl =205 +/-10 g/L, na) of first-stage nanofiltration is obtained 2 SO 4 Content 60-88 g/L) is further concentrated, its Na 2 SO 4 The concentration can reach 150-160g/L, high-concentration Na 2 SO 4 The solution can be subjected to MVR evaporation crystallization to separate salt.
2. According to the invention, by arranging the nanofiltration membrane shell and the special high-pressure nanofiltration membrane element and utilizing the nanofiltration membrane to select separation performance, sodium chloride can enter a dilute brine side through the nanofiltration membrane, sodium sulfate is intercepted and retained at a concentrated brine side by nanofiltration, meanwhile, the content of sodium sulfate at the concentrated side is higher and lower, the content of sodium chloride is lower and lower, the total salt content of sodium sulfate, sodium chloride and the like is less than 300g/L and lower than the saturated solubility, the phenomenon that the nanofiltration membrane element is blocked by precipitation and fouling can not occur, the operation pressure is low in the nanofiltration membrane concentration process, and the one-divalent salt selection separation effect is good.
3. The invention aims to provide a pure water tank, a pure water high-pressure pump and an energy recoverer, which comprises the following components: firstly, reduce sodium sulfate and sodium chloride and separate out the dirty stifled risk of scaling that reduces the high pressure and receive the filter membrane, secondly adopt energy recuperation, dense water pressure of make full use of can save 35% energy consumption, the device operation is reliable and stable.
Drawings
FIG. 1 is a schematic view of the connection of the apparatus of the present invention;
FIG. 2 is a schematic view of the process of the present invention.
In the figure: 1. a first-stage nanofiltration concentrated water tank; 2. a water supply pump; 3. a cartridge filter; 4. a high pressure pump; 5. a valve; 6. nano-filtration membrane shell; 7. a pressure gauge; 8. a first stage water production flow meter; 9. a pure water tank; 10. a pure water supply pump; 11. a special high-pressure nanofiltration membrane element; 12. a high-pressure pump for pure water; 13. a dialysis water flow rate regulating valve; 14. a second stage water production flow meter; 15. a second stage nanofiltration membrane device; 16. a nanofiltration membrane device; 17. three sections of nanofiltration membrane devices; 18. a three-stage water production flowmeter; 19. removing low-nitrate water to a weak brine tank; 20. a permeate water flow regulating valve; 21. an energy recoverer; 22. a concentrate flowmeter; 23. high nitrate water is discharged into an MVR water tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
Examples
Referring to fig. 1-2, the present invention provides the following technical solutions: adopt and receive device of concentrated technique production high concentration sodium sulfate solution of filter membrane, receive concentrated water tank 1, high-pressure pump 4, pure water case 9 and pure water high-pressure pump 12, its characterized in that including the one-level nanofiltration: a pressure gauge 7 is arranged behind a valve 5 behind the high-pressure pump 4, a section of nanofiltration membrane device 16 is arranged at the water outlet end of the high-pressure pump 4, the section of nanofiltration membrane device 16 consists of a nanofiltration membrane shell 6, the pressure gauge 7 and a special high-pressure nanofiltration membrane element 11, a section of produced water flowmeter 8 is arranged at the rear end of the section of nanofiltration membrane device 16, a low-saltwater desalting tank 19 is arranged at the rear end of the section of produced water flowmeter 8, the water outlet end of the pure water high-pressure pump 12 is divided into three pipelines, a dialysis water flow regulating valve 13 is arranged on each pipeline, the three pipelines at the water outlet end of the pure water high-pressure pump 12 are respectively communicated with the section of nanofiltration membrane device 16, the section of nanofiltration membrane device 15 and the section of nanofiltration membrane device 17, the section of nanofiltration membrane device 16 is communicated with the section of nanofiltration membrane device 15, the device is provided with a pressure gauge 7, a two-section nanofiltration membrane device 15 is communicated with a three-section nanofiltration membrane device 17, the pressure gauge 7 is arranged, the two-section nanofiltration membrane device 15 is communicated with a low-nitrate-water desalination salt water tank 19 and is provided with a two-section water production flow meter 14, the three-section nanofiltration membrane device 17 is communicated with the low-nitrate-water desalination salt water tank 19 and is provided with a three-section water production flow meter 18, the two-section nanofiltration membrane device 15 and the three-section nanofiltration membrane are both composed of a nanofiltration membrane shell 6 and a special high-pressure nanofiltration membrane element 11, the three-section nanofiltration membrane device 17 is communicated with a high-nitrate-water MVR removal water tank 23, and the pressure gauge 7, a concentrate permeation flow regulating valve 20, an energy recoverer 21 and a concentrate flow meter 22 are sequentially arranged between the high-nitrate-water MVR water tank 23 and the three-section nanofiltration membrane device 17.
In this embodiment, the high-pressure pump 4 and the pure water high-pressure pump 12 are both used for increasing the pressure of the liquid in the delivery pipeThe nanofiltration membrane shell 6 and the nanofiltration membrane element 11 both utilize the working principle of nanofiltration membranes, and under a certain pressure, when liquid raw liquid flows through the membrane surface, a plurality of capillary pores densely distributed on the surface of the nanofiltration membrane can enable water and Cl to flow through the special pores, so that the applicability of the device is improved, and the operation principle of the nanofiltration membranes is utilized under a certain pressure, and when the liquid raw liquid flows through the membrane surface, the special pores are densely distributed on the surface of the nanofiltration membrane - The small molecular substances are permeated into a permeation liquid, and the volume of SO in the stock solution is larger than the nanofiltration pore diameter on the surface of the membrane 4 2- The low-nitrate water is intercepted on the concentrated solution side of the membrane to form concentrated solution, so that the purposes of purifying, separating and concentrating the stock solution are realized, the low-nitrate water is sent to the dilute salt water tank 19 to play a role of temporary storage, the high-nitrate water is sent to the MVR water tank 23 to enable the entering liquid to be subjected to MVR thermal salt separation process, and Na is produced 2 SO 4 The product, manometer 7, permeate dense water flow control valve 20 and dense water flowmeter 22, the three all play the detection to whole device running state, make the staff carry out corresponding adjustment in the actual conditions, energy recuperation 21 adopts the mode of energy recuperation, the dense water pressure of reuse, can save 35% energy, make whole device operation reliable and stable, one section nanofiltration membrane device 16, two-stage segment nanofiltration membrane device 15 and the inside of three-stage nanofiltration membrane device 17 all can be according to the condition of difference, install additional in the quantity of inside nanofiltration membrane shell 6, manometer 7 and special high pressure nanofiltration membrane component 11, respond to different actual production conditions.
Specifically, both ends of the one-stage nanofiltration concentrated water tank 1 are provided with valves 5, the rear end of the valve 5 far away from a water inlet of the one-stage nanofiltration concentrated water tank 1 is provided with a water supply pump 2, a water outlet end of the water supply pump 2 is provided with a security filter 3, both ends of the security filter 3 are provided with pressure gauges 7, a water outlet end of the security filter 3 is provided with a high-pressure pump 4, a valve 5 is arranged between the high-pressure pump 4 and the security filter 3, and a water outlet end of the high-pressure pump 4 is provided with a valve 5.
In the embodiment, the primary nanofiltration concentrated water tank 1 is used for temporarily storing the primary nanofiltration concentrated solution of the light brine after the electrolysis of the ionic membrane, the water supply pump 2 is used for supplying the primary nanofiltration concentrated water in the primary nanofiltration concentrated water tank 1 to the high-pressure pump 4, the high-pressure pump 4 is used for enhancing the pressure of the primary nanofiltration concentrated water and sending the pressure to the next process for related treatment, and the 5-micron PP cotton filter element adopted by the security filter 3 is used for protecting a nanofiltration membrane element from mechanical damage caused by the entry of tiny solid particles.
Specifically, both ends of the pure water tank 9 are provided with valves 5, the rear end of the valve 5 far away from the water inlet end of the pure water tank 9 is provided with a pure water supply pump 10, the rear end of the pure water supply pump 10 is provided with a security filter 3, both ends of the security filter 3 are fixedly provided with pressure gauges 7, the water outlet end of the security filter 3 is provided with a pure water high-pressure pump 12, and the water outlet end of the high-pressure pump 4 is provided with the valve 5.
In this embodiment, the pure water tank 9 supplies a temporary pure water storage, the pure water supply pump 10 supplies the pure water temporarily stored in the pure water tank 9 to the pure water high-pressure pump 12, and the pure water high-pressure pump 12 is pressurized and supplied to the next process, and the relevant operations are performed.
Specifically, the method for producing the high-concentration sodium sulfate solution by adopting the nanofiltration membrane concentration technology comprises the following steps:
the first step is as follows: the temperature of the light brine is reduced from 60-70 ℃ to 40 +/-3 ℃ by pretreating the light brine (the content of sodium chloride is controlled to be 210 +/-10 g/L and the content of sodium sulfate is less than 20 g/L) after the ion membrane electrolysis in the chlor-alkali industry;
the second step: adding a reducing agent (sodium thiosulfate or sodium sulfite) according to the content of the light brine (1 ton of brine and 0.1Kg of sodium thiosulfate or sodium sulfite), and removing the sodium hypochlorite remained in the electrolytic process by using a reduction reaction;
the third step: after passing through the residual sodium hypochlorite of the activated carbon filter, the sodium hypochlorite enters a primary nanofiltration device (the nanofiltration membrane has selective permeability to divalent ions), and the components NaCl =210 +/-10 g/L and Na of the dilute brine are controlled 2 SO 4 Less than 20g/L, the operating pressure of the first-stage nanofiltration membrane device, the second-stage nanofiltration membrane device and the third-stage nanofiltration membrane device is 20-28Bar, the first-stage nanofiltration recovery rate is 60-85 percent, and the flux of nanofiltration membrane elements is 18-25L/m 2 H, separated nitre-depleted brackish water NaCl =210 ± 10g/L, na 2 SO 4 Less than 1g/L, directly entering the production process to dissolve the original salt or injecting the original salt into an underground mine for recycling;
the fourth step: high-nitrate concentrated brine NaCl =205 +/-10 g/L and Na of primary nanofiltration device 2 SO 4 The content of 60-88g/L enters a super concentration nanofiltration device, which comprises a first-stage nanofiltration membrane device, a second-stage nanofiltration membrane device and a third-stage nanofiltration membrane device, the operating pressure is 55-60Bar, the flux of a high-pressure nanofiltration membrane element is 12-18L/m 2 And h, supplementing 1/3 of pure water for dialyzing sodium chloride during concentration to improve the mass ratio of sodium sulfate, and reducing the total salt concentration of the sodium sulfate and the sodium chloride at the nanofiltration concentrated water side, thereby realizing high-power concentration of the sodium sulfate to 150-160g/L and the NaCl content less than 150g/L. After separation, the NaCl of the lean nitre dilute brine is more than 150g/L and Na 2 SO 4 Less than 5g/L, directly entering the production process to dissolve the original salt or injecting the original salt into an underground mine for recycling;
the fifth step: the concentrated solution high-nitrate water of the super concentration nanofiltration device enters direct MVR evaporation crystallization to produce high-purity Na 2 SO 4 Mirabilite product.
The first condition is as follows:
the first step is as follows: 100 tons of fresh brine (the content of sodium chloride is 213.2g/L, the content of sodium sulfate is 8.60 g/L) after the ion membrane electrolysis is taken, and the flow of the fresh brine is 20.0m 3 Cooling by condensed water from 65 ℃ to 41 ℃;
the second step is that: adding 10.0 kg of sodium sulfite, and removing the residual sodium hypochlorite in the electrolytic process by using a reduction reaction;
the third step: after passing through an active carbon filter, entering a first-stage nanofiltration device, and controlling the components of the dilute brine to be NaCl =213.2g/L and Na 2 SO 4 At 8.60g/L, the operating pressure of the first-stage nanofiltration and nanofiltration device is 24.8Bar, and the flux of the nanofiltration membrane element is 20.4L/m 2 H, separated nitrate-poor dilute brine 89.8m 3 ,NaCl=214.1g/L，Na 2 SO 4 =0.63g/L, directly enters into a production and dissolution crude salt or is injected into an underground mine for recycling;
the fourth step: first-stage nanofiltration high-nitrate strong brine of 10.2m 3 ,NaCl=205.4g/L，Na 2 SO 4 =78.86g/L, enters a super concentration nanofiltration device, the operating pressure of the super concentration nanofiltration device is 58.6Bar, and the water production flux is 14.7L/m 2 H, continuously supplying pure water to total 3.0m 3 The device produces 8.2m of light salt water 3 Its composition NaCl =167.2g/L, na 2 SO 4 =4.54g/L, directly enters a production and dissolution crude salt or is injected into an underground mine for recycling;
the fifth step: super concentration nanofiltration device high nitrate salt water 5.0m 3 The component NaCl =144.9g/L, na 2 SO 4 =153.1g/L, high-nitre concentrated brine MVR evaporates the crystal to separate salt, and 760Kg of Na is obtained 2 SO 4 Product, yield 88.4%. Reduction by 5.2m 3 The evaporation capacity is saved by 50.98 percent, the sodium chloride and the nanofiltration membrane are completely returned to the production process after penetrating through the light salt water, and the utilization rate is 100 percent.
Case two:
the first step is as follows: taking 100 tons of light brine (the content of sodium chloride is 209.7g/L, and the content of sodium sulfate is 13.86 g/L) after the ion membrane electrolysis, wherein the flow rate of the light brine is 20.0m3/h, and the temperature is reduced to 41.7 ℃ from 65 ℃ by cooling through condensed water;
the second step is that: adding 10.0 kg of sodium sulfite, and removing the residual sodium hypochlorite in the electrolytic process by using a reduction reaction;
the third step: after passing through an activated carbon filter, the mixture enters a primary nanofiltration device, and the components of the dilute brine, namely NaCl =209.7g/L and Na, are controlled 2 SO 4 At 13.86g/L, the operating pressure of the first-stage nanofiltration and nanofiltration device is 27.8Bar, and the flux of the nanofiltration membrane element is 18.2L/m 2 H, separated nitrate-poor dilute brine 83.4m 3 ,NaCl=210.9g/L，Na 2 SO 4 =0.68g/L, directly enters into a production and dissolution crude salt or is injected into an underground mine for recycling;
the fourth step: first-stage nanofiltration high-nitrate strong brine of 16.6m 3 ,NaCl=203.7g/L，Na 2 SO 4 =79.08g/L, enters a super concentration nanofiltration device, the operating pressure of the super concentration nanofiltration device is 59.2Bar, and the water production flux is 14.2L/m 2 H, continuously supplying pure water to 5.4m in total 3 The device produces 14.0m of light salt water 3 The component NaCl =162.3g/L, na 2 SO 4 =4.47g/L, directly enters a production and dissolution crude salt or is injected into an underground mine for recycling;
the fifth step: super concentration nanofiltration device high nitrate salt water 8.0m 3 The component NaCl =139.6g/L, na 2 SO 4 =156.0g/L, high-nitrate concentrated brine MVR evaporation crystallization salt separation, 1236.4Kg of Na is obtained 2 SO 4 Product, yield 89.2%. Reduction by 8.6m 3 The evaporation capacity is saved by 51.8 percent, the sodium chloride and the nanofiltration membrane permeate the dilute brine and are all returned to the production process, and the utilization rate is 100 percent.
The working principle and the using process of the invention are as follows: after the equipment is started, the light salt water after the ion membrane electrolysis is temporarily stored in a primary nanofiltration concentrated water tank 1, pure water enters a pure water tank 9 for temporarily storing, the light salt water is supplied to a high-pressure pump 4 through a water supply pump 2 for pressurization and conveying, the pressure in the pipeline is ensured, the pressurized light salt water is subjected to denitration and concentration through a first-section nanofiltration membrane device 16, a second-section nanofiltration membrane device 15 and a third-section nanofiltration membrane device 17, and then respectively enters a low-saltwater light salt water removal tank 19 and a high-saltwater MVR water removal tank 23 for temporarily storing, the pure water is supplied to a pure water high-pressure pump 12 through a pure water supply pump 10 for pressurization, the pressurized pure water is respectively conveyed to the first-section nanofiltration membrane device 16, the second-section nanofiltration membrane device 15 and the third-section nanofiltration membrane device 17, the precipitation of sodium sulfate and sodium chloride is reduced, the scaling, pollution and blockage risks of the high-pressure nanofiltration membranes are reduced, and the liquid entering the high-saltwater MVR water tank 23 is subjected to a salt separation process through an MVR thermal method, and then the Na powder (Na) is produced 2 SO 4 ) And (5) producing the product.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. The method for producing the high-concentration sodium sulfate solution by adopting the nanofiltration membrane concentration technology comprises the following steps:
the first step is as follows: the temperature of the light brine is reduced from 60-70 ℃ to 40 +/-3 ℃ by pretreating the light brine (the content of sodium chloride is controlled to be 210 +/-10 g/L and the content of sodium sulfate is less than 20 g/L) after the ion membrane electrolysis in the chlor-alkali industry;
the second step is that: adding a reducing agent (sodium thiosulfate or sodium sulfite) according to the content of the light brine (1 ton of brine and 0.1Kg of sodium thiosulfate or sodium sulfite), and removing the sodium hypochlorite remained in the electrolytic process by using a reduction reaction;
the third step: after passing through the residual sodium hypochlorite of the activated carbon filter, the sodium hypochlorite enters a primary nanofiltration device (the nanofiltration membrane has selective permeability to divalent ions), and the components NaCl =210 +/-10 g/L and Na of the dilute brine are controlled 2 SO 4 Less than 20g/L, the operating pressure of the first-stage nanofiltration membrane device, the second-stage nanofiltration membrane device and the third-stage nanofiltration membrane device is 20-28Bar, the first-stage nanofiltration recovery rate is 60-85%, and the flux of nanofiltration membrane elements is 18-25L/m 2 H, separated nitre-depleted brackish water NaCl =210 ± 10g/L, na 2 SO 4 Less than 1g/L, directly entering the production process to dissolve the original salt or injecting the original salt into an underground mine for recycling;
the fourth step: high-nitrate concentrated brine NaCl =205 +/-10 g/L and Na of primary nanofiltration device 2 SO 4 The content of 60-88g/L enters a super concentration nanofiltration device which comprises a first section nanofiltration membrane device, a second section nanofiltration membrane device and a third section nanofiltration membrane device, the operating pressure is 55-60Bar, the flux of a high-pressure nanofiltration membrane element is 12-18L/m 2 H, supplementing 1/3 of pure water to dialyze sodium chloride during concentration to improve the mass ratio of sodium sulfate and reduce the total salt concentration of the sodium sulfate and the sodium chloride at the nanofiltration concentrated water side, thereby realizing high-concentration sodium sulfate to 150-160g/L, the NaCl content is less than 150g/L, the NaCl of the separated poor-nitrate light-salt water is more than 150g/L, and the Na 2 SO 4 Less than 5g/L, directly entering the production process to dissolve the original salt or injecting the original salt into an underground mine for recycling;
the fifth step: the concentrated solution high-nitrate water of the super concentration nanofiltration device enters direct MVR evaporation crystallization to produce high-purity Na 2 SO 4 Mirabilite product.
2. Adopt device of concentrated technique production high concentration sodium sulfate solution of receive filter membrane, receive concentrated water tank (1), high-pressure pump (4), pure water case (9) and pure water high-pressure pump (12) including the one-level nanofiltration, its characterized in that: a pressure gauge (7) is arranged behind a valve (5) behind the high-pressure pump (4), a section of nanofiltration membrane device (16) is arranged at the water outlet end of the high-pressure pump (4), the section of nanofiltration membrane device (16) consists of a nanofiltration membrane shell (6), the pressure gauge (7) and a special high-pressure nanofiltration membrane element (11), a section of produced water flow meter (8) is arranged at the rear end of the section of nanofiltration membrane device (16), a low-nitrate water desalination salt water tank (19) is arranged at the rear end of the section of produced water flow meter (8), the water outlet end of the pure water high-pressure pump (12) is divided into three pipelines and is respectively provided with a dialysis water flow regulating valve (13), three pipelines at the water outlet end of the pure water pump (12) are respectively communicated with the section of nanofiltration membrane device (16), the section of nanofiltration membrane device (15) and the section of nanofiltration membrane device (17), the section of nanofiltration membrane device (16) and the section of nanofiltration membrane device (17), the section of nanofiltration membrane device (15) and is provided with the nanofiltration membrane device (7), the section of nanofiltration membrane device (15) is communicated with the low-pressure pump device (19), the section of nanofiltration membrane device (14) and is provided with the pressure gauge flow meter (18) and is arranged on the produced water desalination salt water flow meter, the two-section nanofiltration membrane device (15) and the three-section nanofiltration membrane are both composed of a nanofiltration membrane shell (6) and a special high-pressure nanofiltration membrane element (11), the three-section nanofiltration membrane device (17) is communicated with the high-nitrate-water-removal MVR water tank (23), and a pressure gauge (7), a concentrated water flow regulating valve (20), an energy recoverer (21) and a concentrated water flowmeter (22) are sequentially arranged between the high-nitrate-water-removal MVR water tank (23) and the three-section nanofiltration membrane device (17).
3. The apparatus for producing a sodium sulfate solution with a high concentration by using a nanofiltration membrane concentration technology according to claim 2, wherein: the one-level is received and is strained both ends of thick water tank (1) and all is provided with valve (5) keep away from the one-level and receive the rear end of valve (5) of thick water tank (1) water inlet and be provided with water supply pump (2), the play water end of water supply pump (2) is provided with safety filter ware (3), the both ends of safety filter ware (3) all are provided with manometer (7), the play water end of safety filter ware (3) is provided with high-pressure pump (4), be provided with valve (5) between high-pressure pump (4) and safety filter ware (3), the play water end of high-pressure pump (4) is provided with valve (5).
4. The apparatus for producing a sodium sulfate solution with a high concentration by using a nanofiltration membrane concentration technology according to claim 2, wherein: the water purifier is characterized in that valves (5) are arranged at two ends of the pure water tank (9), a pure water supply pump (10) is arranged at the rear end of the valve (5) far away from the water inlet end of the pure water tank (9), a security filter (3) is arranged at the rear end of the pure water supply pump (10), pressure gauges (7) are fixedly arranged at two ends of the security filter (3), a pure water high-pressure pump (12) is arranged at the water outlet end of the security filter (3), and the valve (5) is arranged at the water outlet end of the high-pressure pump (4).
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116354456A (en) * | 2023-02-21 | 2023-06-30 | 杭州天创环境科技股份有限公司 | Concentration method of sulfate-containing solution |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320625A (en) * | 2011-06-01 | 2012-01-18 | 杭州天创净水设备有限公司 | Treatment method of sodium chloride solution containing sodium sulfate |
| CN107304090A (en) * | 2016-04-21 | 2017-10-31 | 广州市心德实业有限公司 | A kind of Resourceful treatment method for high-salinity wastewater of sodium chloride-containing and sodium sulphate |
| CN206799345U (en) * | 2017-03-30 | 2017-12-26 | 杭州水处理技术研究开发中心有限公司 | A kind of system of high-salt wastewater purified salt |
| CN207158994U (en) * | 2017-06-13 | 2018-03-30 | 陕西省石油化工研究设计院 | A kind of two-way concentrating and separating device of high-salt wastewater for sulfur acid sodium and sodium chloride |
| CA3103575A1 (en) * | 2016-12-12 | 2018-06-12 | Veolia Water Technologies, Inc. | Methods for producing potassium sulfate and sodium chloride from wastewater |
| CN108658345A (en) * | 2017-03-30 | 2018-10-16 | 杭州水处理技术研究开发中心有限公司 | A kind of method and system of high-salt wastewater purified salt |
| CN210559423U (en) * | 2019-09-25 | 2020-05-19 | 天津科技大学 | Thermal denitration system for dechlorination light salt brine |
| CN112679014A (en) * | 2020-12-14 | 2021-04-20 | 江苏卓博环保科技有限公司 | Power plant concentrated wastewater zero-emission treatment device and treatment method |
| CN112830618A (en) * | 2021-02-18 | 2021-05-25 | 科盛环保科技股份有限公司 | Many grades of salt purification processing system of chlor-alkali trade waste water |
| CN214088118U (en) * | 2020-12-14 | 2021-08-31 | 江苏卓博环保科技有限公司 | Power plant concentrated wastewater zero-emission treatment device |
-
2022
- 2022-08-26 CN CN202211034447.1A patent/CN115321559B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102320625A (en) * | 2011-06-01 | 2012-01-18 | 杭州天创净水设备有限公司 | Treatment method of sodium chloride solution containing sodium sulfate |
| CN107304090A (en) * | 2016-04-21 | 2017-10-31 | 广州市心德实业有限公司 | A kind of Resourceful treatment method for high-salinity wastewater of sodium chloride-containing and sodium sulphate |
| CA3103575A1 (en) * | 2016-12-12 | 2018-06-12 | Veolia Water Technologies, Inc. | Methods for producing potassium sulfate and sodium chloride from wastewater |
| CN206799345U (en) * | 2017-03-30 | 2017-12-26 | 杭州水处理技术研究开发中心有限公司 | A kind of system of high-salt wastewater purified salt |
| CN108658345A (en) * | 2017-03-30 | 2018-10-16 | 杭州水处理技术研究开发中心有限公司 | A kind of method and system of high-salt wastewater purified salt |
| CN207158994U (en) * | 2017-06-13 | 2018-03-30 | 陕西省石油化工研究设计院 | A kind of two-way concentrating and separating device of high-salt wastewater for sulfur acid sodium and sodium chloride |
| CN210559423U (en) * | 2019-09-25 | 2020-05-19 | 天津科技大学 | Thermal denitration system for dechlorination light salt brine |
| CN112679014A (en) * | 2020-12-14 | 2021-04-20 | 江苏卓博环保科技有限公司 | Power plant concentrated wastewater zero-emission treatment device and treatment method |
| CN214088118U (en) * | 2020-12-14 | 2021-08-31 | 江苏卓博环保科技有限公司 | Power plant concentrated wastewater zero-emission treatment device |
| CN112830618A (en) * | 2021-02-18 | 2021-05-25 | 科盛环保科技股份有限公司 | Many grades of salt purification processing system of chlor-alkali trade waste water |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116354456A (en) * | 2023-02-21 | 2023-06-30 | 杭州天创环境科技股份有限公司 | Concentration method of sulfate-containing solution |
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