CN209740903U - high-salinity wastewater treatment system for improving sodium chloride recycling rate - Google Patents
high-salinity wastewater treatment system for improving sodium chloride recycling rate Download PDFInfo
- Publication number
- CN209740903U CN209740903U CN201920443283.5U CN201920443283U CN209740903U CN 209740903 U CN209740903 U CN 209740903U CN 201920443283 U CN201920443283 U CN 201920443283U CN 209740903 U CN209740903 U CN 209740903U
- Authority
- CN
- China
- Prior art keywords
- sodium chloride
- communicated
- sodium sulfate
- water
- evaporation
- 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.)
- Active
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
the utility model discloses a high-salinity wastewater treatment system for improving the resource rate of sodium chloride, which comprises an adjusting tank, a primary nanofiltration membrane device, a sodium sulfate evaporative crystallization unit, an RO membrane device, an RO concentrated water tank, a sodium chloride evaporative crystallization unit, a secondary nanofiltration membrane device, a mother liquor mixing tank, a dosing tank, a filtering device and a miscellaneous salt evaporative crystallization unit; the utility model saves water resources, protects the environment, has stable operation, safety, reliability and lower operation cost, avoids the damage of high-salinity wastewater to the environment caused by external emission, and has great social benefit; the recycling of salt in the high-salinity wastewater is realized, the recycling rate of sodium chloride is improved, the obtained sodium chloride crystal salt and sodium sulfate crystal salt have higher purity, can reach the standard of selling, and the economic benefit of enterprises is improved.
Description
The technical field is as follows:
the utility model relates to a waste water treatment field especially relates to a high salt effluent disposal system who improves sodium chloride resource rate.
Background art:
Coal chemical industry enterprises can produce a large amount of high salt waste water in the production operation, and the high salt waste water has characteristics such as complicated composition, quality of water and quantity fluctuation are big, salinity content height, because at present china's coal chemical industry enterprises mostly concentrate on the fragile western region of ecological environment, do not have the dirty water body of receiving in the periphery, do not possess the waste water and arrange the condition outward, and direct arranging such high salt waste water outward can also cause the waste of sodium salt resource, consequently must handle the back and just can externally discharge.
at present, the high-salt wastewater is treated by adopting a nanofiltration salt separation mode, chloride ions and sulfate ions in the high-salt wastewater are separated by nanofiltration, and sodium chloride crystal salt and sodium sulfate crystal salt can be obtained by respectively carrying out evaporative crystallization treatment on nanofiltration produced water and nanofiltration concentrated water. However, because the content of chloride ions and sulfate ions in the high-salt wastewater is high, a certain amount of chloride ions and a certain amount of sulfate ions are contained in nanofiltration concentrated water obtained after nanofiltration treatment, and a certain amount of sulfate radicals are also contained in nanofiltration produced water, so that the purity of finally obtained sodium chloride crystal salt and sodium sulfate crystal salt is not high, the sodium chloride crystal salt and the sodium sulfate crystal salt are difficult to reach the standard of selling, and the chloride ions cannot be fully recovered, so that the resource rate of sodium chloride is low, and the economic production of enterprises is not facilitated.
the utility model has the following contents:
an object of the utility model is to provide a high salt effluent disposal system of improvement sodium chloride resourceful rate safe and reliable, that operate stably.
the utility model discloses by following technical scheme implement:
The high-salinity wastewater treatment system for improving the resource rate of sodium chloride comprises an adjusting tank, a primary nanofiltration membrane device, a sodium sulfate evaporative crystallization unit, an RO membrane device, an RO concentrated water tank, a sodium chloride evaporative crystallization unit, a secondary nanofiltration membrane device, a mother liquor mixing tank, a dosing tank, a filtering device and a miscellaneous salt evaporative crystallization unit;
The water outlet of the regulating tank is communicated with the water inlet of the primary nanofiltration membrane device, and the concentrated water outlet of the primary nanofiltration membrane device is communicated with the water inlet of the sodium sulfate evaporation raw water tank of the sodium sulfate evaporation crystallization unit;
the water outlet of the first-stage nanofiltration membrane device is communicated with the water inlet of the RO membrane device, the concentrated water outlet of the RO membrane device is communicated with the water inlet of the RO concentrated water tank, and the water outlet of the RO concentrated water tank is communicated with the water inlet of the sodium chloride evaporation raw water tank of the sodium chloride evaporation crystallization unit;
A mother liquor outlet of a sodium sulfate evaporative crystallizer of the sodium sulfate evaporative crystallization unit and a mother liquor outlet of a sodium chloride evaporative crystallizer of the sodium chloride evaporative crystallization unit are both communicated with a water inlet of the mother liquor mixing tank, a water outlet of the mother liquor mixing tank is communicated with a water inlet of the filtering device, a water outlet of the filtering device is communicated with a water inlet of the secondary nanofiltration membrane device, a water production outlet of the secondary nanofiltration membrane device is communicated with a water inlet of the RO concentrated water tank, and a concentrated water outlet of the secondary nanofiltration membrane device is communicated with a water inlet of an evaporative mother liquor mixing tank of the miscellaneous salt evaporative crystallization unit;
the water outlet of the RO membrane device is divided into two paths to be respectively communicated with the mother liquor mixing tank and the water inlet of the secondary nanofiltration membrane device;
and the medicine outlet of the medicine adding tank is communicated with the water inlet of the mother liquor mixing tank.
further, the sodium sulfate evaporation crystallization unit comprises a sodium sulfate evaporation raw water pool, a sodium sulfate evaporation crystallizer, a sodium sulfate thickener, a sodium sulfate centrifuge, a sodium sulfate drying bed and a sodium sulfate packaging machine;
The water outlet of the sodium sulfate evaporation raw water tank is communicated with the inlet of the sodium sulfate evaporation crystallizer, the crystal slurry outlet of the sodium sulfate evaporation crystallizer is communicated with the inlet of the sodium sulfate thickener, the crystal slurry outlet of the sodium sulfate thickener is communicated with the inlet of the sodium sulfate centrifugal machine, the crystallized salt outlet of the sodium sulfate centrifugal machine is communicated with the inlet of the sodium sulfate drying bed, and the outlet of the sodium sulfate drying bed is communicated with the inlet of the sodium sulfate packing machine.
further, the sodium chloride evaporation crystallization unit comprises a sodium chloride evaporation raw water pool, a sodium chloride evaporation crystallizer, a sodium chloride thickener, a sodium chloride centrifugal machine, a sodium chloride drying bed and a sodium chloride packing machine;
the water outlet of the sodium chloride evaporation raw water tank is communicated with the water inlet of the sodium chloride evaporation crystallizer, the crystal slurry port of the sodium chloride evaporation crystallizer is communicated with the inlet of the sodium chloride thickener, the crystal slurry outlet of the sodium chloride thickener is communicated with the inlet of the sodium chloride centrifugal machine, the crystal salt outlet of the sodium chloride centrifugal machine is communicated with the inlet of the sodium chloride drying bed, and the outlet of the sodium chloride drying bed is communicated with the inlet of the sodium chloride packing machine.
further, the mixed salt evaporation crystallization unit comprises an evaporation mother liquor mixing tank, a mixed salt evaporation crystallizer, a mixed salt centrifuge, a mixed salt dryer and a mixed salt packaging machine;
the water outlet of the evaporation mother liquor mixing tank is communicated with the water inlet of the miscellaneous salt evaporation crystallizer, the mother liquor outlet of the miscellaneous salt evaporation crystallizer is communicated with the inlet of the miscellaneous salt centrifuge, the crystallized salt outlet of the miscellaneous salt centrifuge is communicated with the inlet of the miscellaneous salt dryer, and the outlet of the miscellaneous salt dryer is communicated with the inlet of the miscellaneous salt packaging machine.
the utility model has the advantages that:
the utility model saves water resources, protects the environment, has stable operation, safety, reliability and lower operation cost, avoids the damage of high-salinity wastewater to the environment caused by external emission, and has great social benefit; the recycling of salt in the high-salinity wastewater is realized, the recycling rate of sodium chloride is improved, the obtained sodium chloride crystal salt and sodium sulfate crystal salt have higher purity, can reach the standard of selling, and the economic benefit of enterprises is improved.
the utility model intercepts divalent ions in high-salinity wastewater through the primary nanofiltration membrane device, and the obtained primary nanofiltration concentrated water is evaporated and crystallized to obtain anhydrous sodium sulfate; concentrating chloride ions in the obtained first-stage nanofiltration water through an RO membrane device, and evaporating and crystallizing the obtained RO concentrated water to obtain sodium chloride crystal salt; the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor enter a mother liquor mixing tank to be mixed and homogenized, and RO (reverse osmosis) production water is added into the mother liquor mixing tank to dilute the sodium chloride and the sodium sulfate, so that the crystallized salt is ensured not to be separated out; then adding a medicament into the mother liquor mixing tank through a medicament adding tank to adjust the pH value, so that the solubility of silicon in the wastewater in the mother liquor mixing tank is reduced to the minimum, and then filtering the precipitated silicon precipitate through a filtering device; then, nanofiltration treatment is carried out through a secondary nanofiltration membrane device, chloride ions are further separated, and the obtained secondary nanofiltration produced water is returned to a sodium chloride evaporation crystallization unit, so that the sodium chloride is fully recovered, and the resource utilization rate of the sodium chloride is improved; most of COD and sulfate ions are intercepted on the side of the secondary nanofiltration concentrated water, and finally enter a mixed salt evaporation crystallization unit to obtain mixed salt after evaporation crystallization.
The utility model further separates the salt from the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor by the two-stage nanofiltration salt separation process, thereby realizing the further recovery of chloride ions and improving the resource rate of sodium chloride; the pH value of the wastewater is adjusted by adding hydrochloric acid, the solubility of total silicon in the wastewater is reduced to the maximum extent, and the precipitated silicon is removed by core-type filtration, so that the problems of large sludge generation amount, large medicament addition amount and medicament cost caused in the process of removing silicon by adding sodium metaaluminate are avoided; dilute mixing the mother liquor in introducing the mother liquor mixing tank through producing water with RO, ensure that sodium chloride and sodium sulfate can not appear, produce water through producing RO and cause the second grade to receive the filter membrane device and dilute except that the silicon water, with the concentration of silicon concentration and each ion in the reduction aquatic, not only realized producing the effective utilization of water to RO, the restriction has been made to the retrieval and utilization volume of water is produced to RO simultaneously, avoided dilution multiple too high to make sodium chloride evaporation crystallization unit inflow too big and the higher problem of investment cost and working costs that causes.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic view of the system configuration of embodiment 1;
In the figure: an adjusting tank 1, a primary nanofiltration membrane device 2, a sodium sulfate evaporation crystallization unit 3, a sodium sulfate evaporation raw water tank 3-1, a sodium sulfate evaporation crystallizer 3-2, a sodium sulfate thickener 3-3, a sodium sulfate centrifuge 3-4, a sodium sulfate drying bed 3-5, a sodium sulfate packaging machine 3-6, an RO membrane device 4, a sodium chloride evaporation crystallization unit 5, a sodium chloride evaporation raw water tank 5-1, a sodium chloride evaporation crystallizer 5-2, a sodium chloride thickener 5-3, a sodium chloride centrifuge 5-4, a sodium chloride drying bed 5-5, a sodium chloride packaging machine 5-6, a secondary nanofiltration membrane device 6, a filtering device 7, a miscellaneous salt evaporation crystallization unit 8, an evaporation mother liquor mixing tank 8-1, a miscellaneous salt evaporation crystallizer 8-2, a miscellaneous salt centrifuge 8-3, a miscellaneous salt dryer 8-4, 8-5 parts of a miscellaneous salt packaging machine, 9 parts of an RO concentrated water tank, 10 parts of a mother liquor mixing tank and 11 parts of a medicine adding tank.
the specific implementation mode is as follows:
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
example 1:
The high-salinity wastewater treatment system for improving the resource utilization rate of sodium chloride shown in fig. 1 comprises an adjusting tank 1, a primary nanofiltration membrane device 2, a sodium sulfate evaporative crystallization unit 3, an RO membrane device 4, an RO concentrated water tank 9, a sodium chloride evaporative crystallization unit 5, a secondary nanofiltration membrane device 6, a mother liquor mixing tank 10, a drug adding tank 11, a filtering device 7 and a miscellaneous salt evaporative crystallization unit 8;
the water outlet of the regulating tank 1 is communicated with the water inlet of the primary nanofiltration membrane device 2, and the concentrated water outlet of the primary nanofiltration membrane device 2 is communicated with the water inlet of a sodium sulfate evaporation raw water tank 3-1 of a sodium sulfate evaporation crystallization unit 3;
a water outlet of the primary nanofiltration membrane device 2 is communicated with a water inlet of an RO membrane device 4, a concentrated water outlet of the RO membrane device 4 is communicated with a water inlet of an RO concentrated water tank 9, and a water outlet of the RO concentrated water tank 9 is communicated with a water inlet of a sodium chloride evaporation raw water tank 5-1 of a sodium chloride evaporation crystallization unit 5;
a mother liquor outlet of a sodium sulfate evaporative crystallizer 3-2 of a sodium sulfate evaporative crystallization unit 3 and a mother liquor outlet of a sodium chloride evaporative crystallizer 5-2 of a sodium chloride evaporative crystallization unit 5 are both communicated with a water inlet of a mother liquor mixing tank 10, a water outlet of the mother liquor mixing tank 10 is communicated with a water inlet of a filtering device 7, a water outlet of the filtering device 7 is communicated with a water inlet of a secondary nanofiltration membrane device 6, a water production outlet of the secondary nanofiltration membrane device 6 is communicated with a water inlet of an RO concentrated water tank 9, and a concentrated water outlet of the secondary nanofiltration membrane device 6 is communicated with a water inlet of an evaporative mother liquor mixing tank 8-1 of a miscellaneous salt evaporative crystallization unit 8;
The water outlet of the RO membrane device 4 is respectively communicated with the mother liquor mixing tank 10 and the water inlet of the secondary nanofiltration membrane device 6 in two ways;
the medicine outlet of the medicine adding tank 11 is communicated with the water inlet of the mother liquor mixing pool 10.
the sodium sulfate evaporation crystallization unit 3 comprises a sodium sulfate evaporation raw water pool 3-1, a sodium sulfate evaporation crystallizer 3-2, a sodium sulfate thickener 3-3, a sodium sulfate centrifuge 3-4, a sodium sulfate drying bed 3-5 and a sodium sulfate packing machine 3-6;
the water outlet of the sodium sulfate evaporation raw water tank 3-1 is communicated with the inlet of a sodium sulfate evaporation crystallizer 3-2, the magma outlet of the sodium sulfate evaporation crystallizer 3-2 is communicated with the inlet of a sodium sulfate thickener 3-3, the magma outlet of the sodium sulfate thickener 3-3 is communicated with the inlet of a sodium sulfate centrifuge 3-4, the crystallized salt outlet of the sodium sulfate centrifuge 3-4 is communicated with the inlet of a sodium sulfate drying bed 3-5, and the outlet of the sodium sulfate drying bed 3-5 is communicated with the inlet of a sodium sulfate packing machine 3-6.
the sodium chloride evaporation crystallization unit 5 comprises a sodium chloride evaporation raw water pool 5-1, a sodium chloride evaporation crystallizer 5-2, a sodium chloride thickener 5-3, a sodium chloride centrifuge 5-4, a sodium chloride drying bed 5-5 and a sodium chloride packing machine 5-6;
the water outlet of the sodium chloride evaporation raw water tank 5-1 is communicated with the water inlet of a sodium chloride evaporation crystallizer 5-2, the crystal slurry port of the sodium chloride evaporation crystallizer 5-2 is communicated with the inlet of a sodium chloride thickener 5-3, the crystal slurry outlet of the sodium chloride thickener 5-3 is communicated with the inlet of a sodium chloride centrifugal machine 5-4, the crystal salt outlet of the sodium chloride centrifugal machine 5-4 is communicated with the inlet of a sodium chloride drying bed 5-5, and the outlet of the sodium chloride drying bed 5-5 is communicated with the inlet of a sodium chloride packing machine 5-6.
the mixed salt evaporation crystallization unit 8 comprises an evaporation mother liquor mixing tank 8-1, a mixed salt evaporation crystallizer 8-2, a mixed salt centrifuge 8-3, a mixed salt dryer 8-4 and a mixed salt packaging machine 8-5;
The water outlet of the evaporation mother liquor mixing tank 8-1 is communicated with the water inlet of the miscellaneous salt evaporation crystallizer 8-2, the mother liquor outlet of the miscellaneous salt evaporation crystallizer 8-2 is communicated with the inlet of the miscellaneous salt centrifuge 8-3, the crystallized salt outlet of the miscellaneous salt centrifuge 8-3 is communicated with the inlet of the miscellaneous salt dryer 8-4, and the outlet of the miscellaneous salt dryer 8-4 is communicated with the inlet of the miscellaneous salt packaging machine 8-5.
in the embodiment, the sodium sulfate evaporative crystallizer 3-2, the sodium chloride evaporative crystallizer 5-2 and the miscellaneous salt evaporative crystallizer 8-2 can adopt OSLO type evaporators; the filter device 7 is a pleated filter.
after the high-salinity wastewater in the regulating tank 1 is subjected to salt separation by the primary nanofiltration membrane device 2, sodium sulfate is mainly retained on the concentrated water side of primary nanofiltration, sodium chloride is mainly concentrated on the water production side of the primary nanofiltration, and meanwhile, the concentrated water side of the primary nanofiltration still contains sodium chloride and the water production side of the primary nanofiltration also contains sodium sulfate; and (3) passing the concentrated water subjected to primary nanofiltration through a sodium sulfate evaporation crystallization unit 3, separating anhydrous sodium sulfate, drying and packaging, and selling. In the process of sodium sulfate evaporation crystallization, the discharge amount of sodium sulfate evaporation mother liquor is controlled, so that the concentration of sodium chloride in the sodium sulfate evaporation mother liquor is lower than 180000mg/L, and the sodium chloride in the sodium sulfate evaporation mother liquor is ensured not to be saturated and separated out; meanwhile, the amount of steam introduced into the sodium sulfate evaporation crystallizer 3-2 is controlled, COD is controlled to be lower than 20000mg/L, the concentration of silicon is controlled to be lower than 5000mg/L, silicon and COD are ensured not to be separated out, and the quality of the finally obtained anhydrous sodium sulfate reaches the qualified product standard of class II salt in the standard GB/T6009-2014. The discharged sodium sulfate evaporation mother liquor enters a mother liquor mixing tank 10, and the c (SO42-) in the discharged sodium sulfate evaporation mother liquor is 48000mg/L, the concentration of sodium sulfate is in a saturated state, the c (Cl-) is lower than 180000mg/L, and the concentration of sodium chloride is close to the saturated state.
The concentration of the water produced by the first-stage nanofiltration is further improved by an RO membrane device 4, so that the TDS is more than 50000mg/L, and the water inflow of a sodium chloride evaporation crystallization unit 5 is reduced; the RO concentrated water concentrated by the RO membrane device 4 enters a sodium chloride evaporation crystallization unit 5, sodium chloride is separated and crystallized, and the sodium chloride is dried, packaged and sold. In the process of sodium chloride evaporation crystallization, the discharge amount of sodium chloride evaporation mother liquor is controlled, so that the concentration of sodium sulfate in the sodium chloride evaporation mother liquor is lower than 48000mg/L, and the sodium sulfate in the sodium chloride evaporation mother liquor is ensured not to be saturated and separated out; meanwhile, the amount of steam introduced into the sodium chloride evaporative crystallizer 5-2 is controlled to control COD to be lower than 20000mg/L and the concentration of silicon to be lower than 5000mg/L, so that silicon and COD are not separated out, and the quality of the finally obtained sodium chloride crystal salt reaches the secondary standard of refined industrial dry salt in GB/T5462-2015 Industrial salt standard. The discharged sodium chloride evaporation mother liquor enters a mother liquor mixing tank 10, and in the discharged sodium chloride evaporation mother liquor, c (Cl-) is 180000mg/L, the concentration of sodium chloride is in a saturated state, c (SO42-) is less than or equal to 48000mg/L, and the concentration of sodium sulfate is close to the saturated state.
in the embodiment, RO produced water with the water quantity equal to that in the mother liquor mixing tank 10 is added into the mother liquor mixing tank 10 to dilute the sodium chloride and the sodium sulfate, so that the crystallized salt is ensured not to be separated out. Then adding a medicament (hydrochloric acid or sulfuric acid) into the mother liquor mixing tank 10 through a medicament adding tank 11 to control the pH value of the wastewater in the mother liquor mixing tank 10 to be 8-8.5, further minimizing the solubility of silicon in the wastewater in the mother liquor mixing tank 10 to reduce the silicon concentration in the water to be below 150mg/L, then filtering the precipitated silicon precipitate through a filtering device 7, then entering a secondary nanofiltration membrane device 6, simultaneously adding RO produced water with the same water amount as that in the secondary nanofiltration membrane device 6 into the secondary nanofiltration membrane device 6 to dilute sodium chloride and sodium sulfate so as to reduce the silicon concentration in the water to be below 75mg/L, performing nanofiltration salt separation treatment through the secondary nanofiltration membrane device 6 after dilution so that chloride ions pass through a nanofiltration membrane, namely the nanofiltration membrane is enriched at the secondary nanofiltration water production side, and returning to a sodium chloride evaporative crystallization unit 5 to realize the full recovery of sodium chloride, thereby improving the resource utilization rate of the sodium chloride; most of COD and sulfate ions are intercepted on the side of the secondary nanofiltration concentrated water and finally enter a mixed salt evaporation crystallization unit 8 to obtain mixed salt after evaporation and crystallization.
example 2:
The process for treating high-salinity wastewater by using the high-salinity wastewater treatment system for improving the sodium chloride recycling rate in embodiment 1 comprises the following steps of: the process comprises the steps of one-stage nanofiltration salt separation; reverse osmosis filtration in the second procedure; step (3) sodium trithione crystallization and sodium chloride crystallization; step four, mixing and adding medicine; step five, filtering and removing silicon; the sixth step of secondary nanofiltration salt separation; step seven, crystallizing miscellaneous salt; wherein:
The process comprises the following steps of (1) one-stage nanofiltration salt separation: sending the high-salinity wastewater with the pH value of 6, the TDS of 47000mg/L, the c (SO42-) of 5000mg/L, c (SO42-), (Cl-) of 0.7 and the c (Si) of 10mg/L, COD of 300mg/L into a first-stage nanofiltration membrane device 2 of a high-salinity wastewater treatment system for improving the resource rate of sodium chloride, and carrying out first-stage nanofiltration treatment to obtain first-stage nanofiltration product water and first-stage nanofiltration concentrated water SO as to enrich sulfate ions in the first-stage nanofiltration concentrated water, wherein the c (SO42-) in the first-stage nanofiltration concentrated water is 86000mg/L, and the c (Cl-) in the first-stage nanofiltration product water is 15000 mg/L;
And (2) reverse osmosis filtration: sending the primary nanofiltration product water obtained in the primary nanofiltration salt separation in the procedure into an RO membrane device 4, and carrying out reverse osmosis filtration treatment to further concentrate ions in the primary nanofiltration product water to obtain RO concentrated water and RO product water, wherein the TDS in the RO concentrated water is 55000mg/L, and the c (Cl-) in the RO concentrated water is 25000 mg/L;
step (2), sodium trithionate crystallization and sodium chloride crystallization: feeding the first-stage nanofiltration concentrated water obtained in the first-stage nanofiltration salt separation process into a sodium sulfate evaporation crystallizer 3-2 for evaporation crystallization to obtain sodium sulfate crystalline salt and sodium sulfate evaporation mother liquor, wherein c (SO42-) in the sodium sulfate evaporation mother liquor is 48000mg/L, and c (Cl-) in the sodium sulfate evaporation mother liquor is 175000 mg/L;
Feeding the RO concentrated water obtained in the reverse osmosis filtration in the second procedure into a sodium chloride evaporation crystallizer 5-2 for evaporation crystallization to obtain sodium chloride crystal salt and sodium chloride evaporation mother liquor, wherein c (Cl-) in the sodium chloride evaporation mother liquor is 180000mg/L, and c (SO42-) is 47000 mg/L;
and step four, mixing and adding medicine: feeding sodium sulfate evaporation mother liquor and sodium chloride evaporation mother liquor obtained in the sodium sulfate crystal and sodium chloride crystal in the working procedure and RO product water obtained in reverse osmosis filtration in the working procedure II into a mother liquor mixing tank 10 for mixing and homogenizing, wherein the RO product water amount entering the mother liquor mixing tank 10 is equal to the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor entering the mother liquor mixing tank 10, and the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor are diluted to prevent the sodium sulfate and the sodium chloride from being separated out due to the temperature reduction of the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor after entering the mother liquor mixing tank 10; adding hydrochloric acid into the mother liquor mixing tank 10 from a medicine adding tank 11 to obtain a mixed solution with the pH maintained at 8.1 so as to reduce the solubility of silicon in the mixed solution;
and a fifth step of filtering and removing silicon: sending the mixed solution obtained in the mixing and adding of the step four into a filtering device 7, filtering, removing silicon precipitates separated out from the mixed solution, and obtaining silicon-removed water, wherein c (Si) in the silicon-removed water is 120 mg/L;
and (3) carrying out secondary nanofiltration salt separation: feeding RO produced water obtained in the reverse osmosis filtration in the second procedure and silicon-removed water obtained in the silicon removal filtration in the fifth procedure into a secondary nanofiltration membrane device 6, and performing secondary nanofiltration treatment to obtain secondary nanofiltration produced water and secondary nanofiltration concentrated water; the RO water yield entering the secondary nanofiltration membrane device 6 is equal to the silicon removal water yield entering the secondary nanofiltration membrane device 6, and the RO water yield is used for diluting the silicon concentration, so that the c (Si) in the water entering the secondary nanofiltration membrane device 6 is 60mg/L, and the water inlet requirement of the secondary nanofiltration membrane device 6 is met; c (SO42-) in the secondary nanofiltration concentrated water is 90000mg/L, and the secondary nanofiltration produced water is returned to the sodium trithionate crystal and the sodium chloride crystal in the working procedure for sodium chloride crystallization treatment;
step seven miscellaneous salt crystallization: and (3) feeding the secondary nanofiltration concentrated water obtained in the sixth secondary nanofiltration into a mixed salt evaporative crystallizer 8-2 for evaporative crystallization to obtain mixed salt.
example 3:
the process for treating high-salinity wastewater by using the high-salinity wastewater treatment system for improving the sodium chloride recycling rate in embodiment 1 comprises the following steps of: the process comprises the steps of one-stage nanofiltration salt separation; reverse osmosis filtration in the second procedure; step (3) sodium trithione crystallization and sodium chloride crystallization; step four, mixing and adding medicine; step five, filtering and removing silicon; the sixth step of secondary nanofiltration salt separation; step seven, crystallizing miscellaneous salt; wherein:
The process comprises the following steps of (1) one-stage nanofiltration salt separation: sending the high-salinity wastewater with the pH value of 7, the TDS of 45000mg/L, the c (SO42-) of 5500mg/L, c (SO42-), (Cl-) of 0.8 and the c (Si) of 15mg/L, COD of 250mg/L in the regulating tank 1 into a first-stage nanofiltration membrane device 2 of a high-salinity wastewater treatment system for improving the resource rate of sodium chloride, and carrying out first-stage nanofiltration treatment to obtain first-stage nanofiltration product water and first-stage nanofiltration concentrated water SO as to enrich sulfate ions in the first-stage nanofiltration concentrated water, wherein the c (SO42-) in the first-stage nanofiltration concentrated water is 96000mg/L, and the c (Cl-) in the first-stage nanofiltration product water is 13000 mg/L;
and (2) reverse osmosis filtration: sending the primary nanofiltration product water obtained in the primary nanofiltration salt separation of the working procedure into an RO membrane device 4, and carrying out reverse osmosis filtration treatment to further concentrate ions in the primary nanofiltration product water to obtain RO concentrated water and RO product water, wherein the TDS in the RO concentrated water is 54000mg/L, and the c (Cl-) in the RO concentrated water is 21000 mg/L;
step (2), sodium trithionate crystallization and sodium chloride crystallization: feeding the primary nanofiltration concentrated water obtained in the primary nanofiltration salt separation in the working procedure into a sodium sulfate evaporation crystallizer 3-2 for evaporation crystallization to obtain sodium sulfate crystalline salt and sodium sulfate evaporation mother liquor, wherein c (SO42-) in the sodium sulfate evaporation mother liquor is 48000mg/L, and c (Cl-) in the sodium sulfate evaporation mother liquor is 172000 mg/L;
feeding the RO concentrated water obtained in the reverse osmosis filtration in the second procedure into a sodium chloride evaporation crystallizer 5-2 for evaporation crystallization to obtain sodium chloride crystal salt and sodium chloride evaporation mother liquor, wherein c (Cl-) in the sodium chloride evaporation mother liquor is 180000mg/L, and c (SO42-) is 46000 mg/L;
And step four, mixing and adding medicine: feeding sodium sulfate evaporation mother liquor and sodium chloride evaporation mother liquor obtained in the sodium sulfate crystal and sodium chloride crystal in the working procedure and RO product water obtained in reverse osmosis filtration in the working procedure II into a mother liquor mixing tank 10 for mixing and homogenizing, wherein the RO product water amount entering the mother liquor mixing tank 10 is equal to the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor entering the mother liquor mixing tank 10, and the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor are diluted to prevent the sodium sulfate and the sodium chloride from being separated out due to the temperature reduction of the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor after entering the mother liquor mixing tank 10; adding hydrochloric acid into the mother liquor mixing tank 10 from a medicine adding tank 11 to obtain a mixed solution with the pH maintained at 8.2 so as to reduce the solubility of silicon in the mixed solution;
And a fifth step of filtering and removing silicon: sending the mixed solution obtained in the mixing and adding of the step four into a filtering device 7, filtering, removing silicon precipitates separated out from the mixed solution, and obtaining silicon-removed water, wherein c (Si) in the silicon-removed water is 130 mg/L;
and (3) carrying out secondary nanofiltration salt separation: feeding RO produced water obtained in the reverse osmosis filtration in the second procedure and silicon-removed water obtained in the silicon removal filtration in the fifth procedure into a secondary nanofiltration membrane device 6, and performing secondary nanofiltration treatment to obtain secondary nanofiltration produced water and secondary nanofiltration concentrated water; the RO water yield entering the secondary nanofiltration membrane device 6 is equal to the silicon removal water yield entering the secondary nanofiltration membrane device 6, and the RO water yield is used for diluting the silicon concentration, so that the c (Si) in the water entering the secondary nanofiltration membrane device 6 is 65mg/L, and the water inlet requirement of the secondary nanofiltration membrane device 6 is met; c (SO42-) in the secondary nanofiltration concentrated water is 85000mg/L, and the secondary nanofiltration produced water is returned to the sodium trithionate crystal and the sodium chloride crystal in the working procedure for sodium chloride crystallization treatment;
Step seven miscellaneous salt crystallization: and (3) feeding the secondary nanofiltration concentrated water obtained in the secondary nanofiltration salt separation in the step six into a mixed salt evaporation crystallizer 8-2 of a system for improving the recycling rate of sodium chloride in the nanofiltration salt separation to perform evaporation crystallization to obtain mixed salt.
example 4:
the process for treating high-salinity wastewater by using the high-salinity wastewater treatment system for improving the sodium chloride recycling rate in embodiment 1 comprises the following steps of: the process comprises the steps of one-stage nanofiltration salt separation; reverse osmosis filtration in the second procedure; step (3) sodium trithione crystallization and sodium chloride crystallization; step four, mixing and adding medicine; step five, filtering and removing silicon; the sixth step of secondary nanofiltration salt separation; step seven, crystallizing miscellaneous salt; wherein:
the process comprises the following steps of (1) one-stage nanofiltration salt separation: sending the high-salinity wastewater with the pH value of 8, the TDS of 50000mg/L, the c (SO42-) of 5000mg/L, c (SO42-), (Cl-) of 0.9 and the c (Si) of 20mg/L, COD of 200mg/L into a first-stage nanofiltration membrane device 2 of a high-salinity wastewater treatment system for improving the resource rate of sodium chloride, and carrying out first-stage nanofiltration treatment to obtain first-stage nanofiltration product water and first-stage nanofiltration concentrated water SO as to enrich sulfate ions in the first-stage nanofiltration concentrated water, wherein c (SO42-) in the first-stage nanofiltration concentrated water is 90000mg/L, and c (Cl-) in the first-stage nanofiltration product water is 12000 mg/L;
And (2) reverse osmosis filtration: sending the primary nanofiltration product water obtained in the primary nanofiltration salt separation of the procedure into an RO membrane device 4, and carrying out reverse osmosis filtration treatment to further concentrate ions in the primary nanofiltration product water to obtain RO concentrated water and RO product water, wherein TDS in the RO concentrated water is 52000mg/L, and c (Cl-) in the RO concentrated water is 23000 mg/L;
Step (2), sodium trithionate crystallization and sodium chloride crystallization: feeding the first-stage nanofiltration concentrated water obtained in the first-stage nanofiltration salt separation process into a sodium sulfate evaporation crystallizer 3-2 for evaporation crystallization to obtain sodium sulfate crystalline salt and sodium sulfate evaporation mother liquor, wherein c (SO42-) in the sodium sulfate evaporation mother liquor is 48000mg/L, and c (Cl-) in the sodium sulfate evaporation mother liquor is 170000 mg/L;
feeding the RO concentrated water obtained in the reverse osmosis filtration in the second procedure into a sodium chloride evaporation crystallizer 5-2 for evaporation crystallization to obtain sodium chloride crystal salt and sodium chloride evaporation mother liquor, wherein c (Cl-) in the sodium chloride evaporation mother liquor is 180000mg/L, and c (SO42-) is 45000 mg/L;
And step four, mixing and adding medicine: feeding sodium sulfate evaporation mother liquor and sodium chloride evaporation mother liquor obtained in the sodium sulfate crystal and sodium chloride crystal in the working procedure and RO product water obtained in reverse osmosis filtration in the working procedure II into a mother liquor mixing tank 10 for mixing and homogenizing, wherein the RO product water amount entering the mother liquor mixing tank 10 is equal to the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor entering the mother liquor mixing tank 10, and the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor are diluted to prevent the sodium sulfate and the sodium chloride from being separated out due to the temperature reduction of the sodium sulfate evaporation mother liquor and the sodium chloride evaporation mother liquor after entering the mother liquor mixing tank 10; adding hydrochloric acid into the mother liquor mixing tank 10 from a medicine adding tank 11 to obtain a mixed solution with the pH maintained at 8.3 so as to reduce the solubility of silicon in the mixed solution;
And a fifth step of filtering and removing silicon: sending the mixed solution obtained in the mixing and adding of the step four into a filtering device 7, filtering, removing silicon precipitates separated out from the mixed solution, and obtaining silicon-removed water, wherein c (Si) in the silicon-removed water is 140 mg/L;
And (3) carrying out secondary nanofiltration salt separation: feeding RO produced water obtained in the reverse osmosis filtration in the second procedure and silicon-removed water obtained in the silicon removal filtration in the fifth procedure into a secondary nanofiltration membrane device 6, and performing secondary nanofiltration treatment to obtain secondary nanofiltration produced water and secondary nanofiltration concentrated water; the RO water yield entering the secondary nanofiltration membrane device 6 is equal to the silicon removal water yield entering the secondary nanofiltration membrane device 6, and the RO water yield is used for diluting the silicon concentration, so that the c (Si) in the water entering the secondary nanofiltration membrane device 6 is 70mg/L, and the water inlet requirement of the secondary nanofiltration membrane device 6 is met; c (SO42-) in the secondary nanofiltration concentrated water is 95000mg/L, and the secondary nanofiltration produced water is returned to the sodium trithionate crystal and the sodium chloride crystal in the working procedure for sodium chloride crystallization treatment;
Step seven miscellaneous salt crystallization: and (3) feeding the secondary nanofiltration concentrated water obtained in the secondary nanofiltration salt separation in the sixth procedure into a mixed salt evaporative crystallizer 8-2 for evaporative crystallization to obtain mixed salt.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. 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 high-salinity wastewater treatment system for improving the resource utilization rate of sodium chloride is characterized by comprising an adjusting tank, a primary nanofiltration membrane device, a sodium sulfate evaporative crystallization unit, an RO membrane device, an RO concentrated water tank, a sodium chloride evaporative crystallization unit, a secondary nanofiltration membrane device, a mother liquor mixing tank, a dosing tank, a filtering device and a miscellaneous salt evaporative crystallization unit;
the water outlet of the regulating tank is communicated with the water inlet of the primary nanofiltration membrane device, and the concentrated water outlet of the primary nanofiltration membrane device is communicated with the water inlet of the sodium sulfate evaporation raw water tank of the sodium sulfate evaporation crystallization unit;
the water outlet of the first-stage nanofiltration membrane device is communicated with the water inlet of the RO membrane device, the concentrated water outlet of the RO membrane device is communicated with the water inlet of the RO concentrated water tank, and the water outlet of the RO concentrated water tank is communicated with the water inlet of the sodium chloride evaporation raw water tank of the sodium chloride evaporation crystallization unit;
a mother liquor outlet of a sodium sulfate evaporative crystallizer of the sodium sulfate evaporative crystallization unit and a mother liquor outlet of a sodium chloride evaporative crystallizer of the sodium chloride evaporative crystallization unit are both communicated with a water inlet of the mother liquor mixing tank, a water outlet of the mother liquor mixing tank is communicated with a water inlet of the filtering device, a water outlet of the filtering device is communicated with a water inlet of the secondary nanofiltration membrane device, a water production outlet of the secondary nanofiltration membrane device is communicated with a water inlet of the RO concentrated water tank, and a concentrated water outlet of the secondary nanofiltration membrane device is communicated with a water inlet of an evaporative mother liquor mixing tank of the miscellaneous salt evaporative crystallization unit;
The water outlet of the RO membrane device is divided into two paths to be respectively communicated with the mother liquor mixing tank and the water inlet of the secondary nanofiltration membrane device;
and the medicine outlet of the medicine adding tank is communicated with the water inlet of the mother liquor mixing tank.
2. The high-salinity wastewater treatment system for improving the resource utilization rate of sodium chloride according to claim 1, wherein the sodium sulfate evaporative crystallization unit comprises a sodium sulfate evaporative raw water tank, the sodium sulfate evaporative crystallizer, a sodium sulfate thickener, a sodium sulfate centrifuge, a sodium sulfate drying bed and a sodium sulfate packing machine;
the water outlet of the sodium sulfate evaporation raw water tank is communicated with the inlet of the sodium sulfate evaporation crystallizer, the crystal slurry outlet of the sodium sulfate evaporation crystallizer is communicated with the inlet of the sodium sulfate thickener, the crystal slurry outlet of the sodium sulfate thickener is communicated with the inlet of the sodium sulfate centrifugal machine, the crystallized salt outlet of the sodium sulfate centrifugal machine is communicated with the inlet of the sodium sulfate drying bed, and the outlet of the sodium sulfate drying bed is communicated with the inlet of the sodium sulfate packing machine.
3. the high-salinity wastewater treatment system for improving the resource utilization rate of sodium chloride according to claim 1, wherein the sodium chloride evaporative crystallization unit comprises a sodium chloride evaporative raw water tank, a sodium chloride evaporative crystallizer, a sodium chloride thickener, a sodium chloride centrifuge, a sodium chloride drying bed and a sodium chloride packing machine;
the water outlet of the sodium chloride evaporation raw water tank is communicated with the water inlet of the sodium chloride evaporation crystallizer, the crystal slurry port of the sodium chloride evaporation crystallizer is communicated with the inlet of the sodium chloride thickener, the crystal slurry outlet of the sodium chloride thickener is communicated with the inlet of the sodium chloride centrifugal machine, the crystal salt outlet of the sodium chloride centrifugal machine is communicated with the inlet of the sodium chloride drying bed, and the outlet of the sodium chloride drying bed is communicated with the inlet of the sodium chloride packing machine.
4. the high-salinity wastewater treatment system for improving the resource utilization rate of sodium chloride according to claim 1, wherein the miscellaneous salt evaporation and crystallization unit comprises an evaporation mother liquor mixing tank, a miscellaneous salt evaporation crystallizer, a miscellaneous salt centrifuge, a miscellaneous salt dryer and a miscellaneous salt packaging machine;
The water outlet of the evaporation mother liquor mixing tank is communicated with the water inlet of the miscellaneous salt evaporation crystallizer, the mother liquor outlet of the miscellaneous salt evaporation crystallizer is communicated with the inlet of the miscellaneous salt centrifuge, the crystallized salt outlet of the miscellaneous salt centrifuge is communicated with the inlet of the miscellaneous salt dryer, and the outlet of the miscellaneous salt dryer is communicated with the inlet of the miscellaneous salt packaging machine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920443283.5U CN209740903U (en) | 2019-04-02 | 2019-04-02 | high-salinity wastewater treatment system for improving sodium chloride recycling rate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920443283.5U CN209740903U (en) | 2019-04-02 | 2019-04-02 | high-salinity wastewater treatment system for improving sodium chloride recycling rate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209740903U true CN209740903U (en) | 2019-12-06 |
Family
ID=68719541
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920443283.5U Active CN209740903U (en) | 2019-04-02 | 2019-04-02 | high-salinity wastewater treatment system for improving sodium chloride recycling rate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209740903U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111153537A (en) * | 2019-04-02 | 2020-05-15 | 内蒙古晶泰环境科技有限责任公司 | High-salinity wastewater treatment system and process for improving sodium chloride recycling rate |
| CN113912231A (en) * | 2021-07-13 | 2022-01-11 | 北京航天环境工程有限公司 | System and method for recycling and co-processing wastewater |
-
2019
- 2019-04-02 CN CN201920443283.5U patent/CN209740903U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111153537A (en) * | 2019-04-02 | 2020-05-15 | 内蒙古晶泰环境科技有限责任公司 | High-salinity wastewater treatment system and process for improving sodium chloride recycling rate |
| CN111153537B (en) * | 2019-04-02 | 2023-10-31 | 内蒙古晶泰环境科技有限责任公司 | High-salt wastewater treatment system and process for improving sodium chloride recycling rate |
| CN113912231A (en) * | 2021-07-13 | 2022-01-11 | 北京航天环境工程有限公司 | System and method for recycling and co-processing wastewater |
| CN113912231B (en) * | 2021-07-13 | 2023-09-26 | 北京航天环境工程有限公司 | System and method for resource co-processing of wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108623054B (en) | Multi-membrane integrated pulping and papermaking wastewater zero-discharge treatment method and device | |
| CN111153537B (en) | High-salt wastewater treatment system and process for improving sodium chloride recycling rate | |
| CN209276303U (en) | Coal water slurry gasification waste water divides salt to crystallize zero-discharge treatment system | |
| CN109250856A (en) | It is a kind of low cost ferric phosphate nitrogen-containing wastewater processing and recovery method as resource | |
| CN109250857A (en) | A kind of low cost ferric phosphate nitrogen-containing wastewater processing method | |
| CN104140174A (en) | Combined treatment method for ammonia chloride waste water through rare earth extraction separation | |
| CN209740903U (en) | high-salinity wastewater treatment system for improving sodium chloride recycling rate | |
| CN110342545A (en) | High-salt wastewater divides salt system and its technique | |
| CN113716772A (en) | Recycling and zero-discharge process for divalent salt in organic wastewater of synthetic ammonia | |
| CN108862353B (en) | Process method for preparing and purifying calcium chloride by using chlor-alkali waste salt mud | |
| CN208667421U (en) | A kind of high-salinity wastewater zero-emission processing unit based on nanofiltration membrane allotment | |
| CN106082516A (en) | A kind of point of salt-pepper noise technique and device | |
| CN104649494B (en) | A kind of method of processing of Ludox waste water and coproduction sodium salt | |
| CN104261443A (en) | Process for calcium-method production of magnesium hydrate by using nanofiltration membrane | |
| CN209507610U (en) | High-salt wastewater divides salt system | |
| CN209940738U (en) | Salt separation and crystallization system for high-salinity wastewater containing organic matters | |
| CN105481160B (en) | Method and device for preparing industrial salt by strong brine with zero discharge | |
| CN110436679B (en) | Device and method for recycling and comprehensively utilizing washing water of lithium carbonate | |
| CN214611993U (en) | Mine strong brine zero release processing system | |
| CN110451529A (en) | A kind of method of purification of sodium chloride for injection | |
| CN209778557U (en) | High-salinity wastewater treatment system capable of ensuring stable operation of salt and nitrate co-production | |
| CN209940737U (en) | Salt separation system for ensuring quality of high-salinity wastewater crystal salt | |
| CN214936736U (en) | Salt dissolving system for seawater desalination concentrated seawater for chlor-alkali industry | |
| CN111153540B (en) | Salt separation system and technology for guaranteeing quality of high-salt wastewater crystalline salt | |
| CN111153538B (en) | High-salt wastewater treatment system capable of guaranteeing stable operation of salt and nitrate co-production and process thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |