CN210117311U - Mine water upgrading treatment system - Google Patents
Mine water upgrading treatment system Download PDFInfo
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- CN210117311U CN210117311U CN201920832719.XU CN201920832719U CN210117311U CN 210117311 U CN210117311 U CN 210117311U CN 201920832719 U CN201920832719 U CN 201920832719U CN 210117311 U CN210117311 U CN 210117311U
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Abstract
The utility model belongs to the environmental protection field especially relates to a mine water carries mark governing system, and this system includes: a V-shaped filter chamber; the ultrafiltration device is connected with the V-shaped filter tank; the first-stage reverse osmosis device is connected with a water production outlet of the ultrafiltration device; the first tubular microfiltration device is connected with a concentrated water outlet of the first-stage reverse osmosis device; the second-stage reverse osmosis device is connected with a water production outlet of the first tubular microfiltration device; the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device; the ion exchange device is connected with the water production outlet of the second tubular microfiltration device; a third-stage reverse osmosis device connected with the ion exchange device; and the evaporation crystallization salt separation equipment is connected with a concentrated water outlet of the third-stage reverse osmosis device. The system provided by the utility model can further reduce the pollutant content of mine aquatic, retrieves resources such as sodium sulfate and sodium chloride of mine aquatic simultaneously, realizes the "zero release" of waste water.
Description
Technical Field
The utility model belongs to the environmental protection field especially relates to a mine water carries mark governing system.
Background
The country intensively produces a series of environmental regulations and policies in recent two years, and requires that the mine water discharge part meets the requirements of III-class standard of surface water environmental quality standard (GB3838-2002), and the requirements on environmental protection are higher and higher. The original mine water treatment equipment and process cannot meet the existing environmental protection requirement, and the original facilities must be reconstructed and expanded to meet the condition of further resource utilization. Therefore, from the viewpoint of environmental protection, the upgrading treatment of mine water is urgent.
China coal mines are mainly concentrated in northern and northwest areas, industrial water consumption of many coal mine areas is large, annual rainfall is small, space-time distribution is extremely uneven, evaporation capacity is large, and water resources are very deficient. The agricultural and greening water basically depends on irrigation, and the water demand is large. The mine water standard improvement treatment can bring clean water sources for production and agriculture, and relieve the contradiction between water resource shortage and increasing water demand, so the mine water standard improvement treatment is in urgent need from the perspective of water resource utilization.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a mine water carries mark treatment system adopts the utility model provides a system carries mark to the mine water through conventional processing and administers the back, can obviously reduce the content of total solid of dissolubility (TDS), chloride and fluoride in the mine water, retrieves resources such as sodium sulfate and sodium chloride in the mine water simultaneously, realizes "zero release" of waste water.
The utility model provides a mark improvement governing system is carried to mine water, include:
a V-shaped filter chamber;
the ultrafiltration device is connected with the water outlet of the V-shaped filter tank;
the primary reverse osmosis device is connected with a water production outlet of the ultrafiltration device, and a membrane element arranged in the primary reverse osmosis device is a BW reverse osmosis membrane;
the first tubular microfiltration device is connected with a concentrated water outlet of the first-stage reverse osmosis device, and a first softener dosing port is arranged on a connecting pipeline of the first tubular microfiltration device and the concentrated water outlet of the first-stage reverse osmosis device;
the second-stage reverse osmosis device is connected with a water production outlet of the first tubular microfiltration device, and a membrane element arranged in the second-stage reverse osmosis device is a BW reverse osmosis membrane;
the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device, and a second softener dosing port is arranged on a connecting pipeline between the second tubular microfiltration device and the concentrated water outlet of the second-stage reverse osmosis device;
the ion exchange device is connected with the water production outlet of the second tubular microfiltration device;
the three-stage reverse osmosis device is connected with a water outlet of the ion exchange device, and a membrane element arranged in the three-stage reverse osmosis device is a SW reverse osmosis membrane;
and the evaporation crystallization salt separation equipment is connected with a concentrated water outlet of the third-stage reverse osmosis device.
Preferably, the device also comprises a self-cleaning filter, wherein the self-cleaning filter is arranged between the V-shaped filter pool and the ultrafiltration device, a water inlet of the self-cleaning filter is connected with a water outlet of the V-shaped filter pool, and a water outlet of the self-cleaning filter is connected with a water inlet of the ultrafiltration device.
Preferably, the system also comprises a concentrated brine tank, wherein the concentrated brine is arranged between the third-level reverse osmosis device and the evaporation crystallization salt separation equipment, a water inlet of the concentrated brine is connected with a concentrated water outlet of the third-level reverse osmosis device, and a water outlet of the concentrated brine is connected with a water inlet of the evaporation crystallization salt separation equipment.
Preferably, still include third tubular micro-filtration device, third tubular micro-filtration device sets up tertiary reverse osmosis unit with between the strong brine pond, the water inlet of third tubular micro-filtration device with tertiary reverse osmosis unit's dense water export links to each other, is provided with third softener dosing port on its connecting line, the product water outlet of third tubular micro-filtration device with the water inlet of strong brine links to each other.
Preferably, a reducing agent dosing port is arranged on a connecting pipeline between a water production outlet of the ultrafiltration device and the primary reverse osmosis device.
Preferably, the evaporative crystallization salt separation device comprises:
the preheater is connected with a concentrated water outlet of the third-stage reverse osmosis device;
the MVR falling film evaporator is connected with a water outlet of the preheater;
the MVR nitrate analysis device is connected with a concentrated solution outlet of the MVR falling film evaporator;
and the salt separating device is connected with a supernatant outlet of the MVR nitrate separating device.
Preferably, the device also comprises a sodium sulfate crystal slurry centrifuge, a sodium sulfate dryer, a sodium chloride crystal slurry centrifuge and a sodium chloride dryer;
a feed port of the sodium sulfate crystal slurry centrifuge is connected with a crystal slurry outlet of the MVR nitrate separating device, and a wet crystal discharge port of the sodium sulfate crystal slurry centrifuge is connected with a feed port of the sodium sulfate dryer;
the feed inlet of the sodium chloride crystal slurry centrifuge is connected with a crystal slurry outlet of the salt precipitation device, and the wet crystal discharge port of the sodium chloride crystal slurry centrifuge is connected with the feed inlet of the sodium chloride dryer.
Compared with the prior art, the utility model provides a mine water carries mark governing system. The utility model provides a mine water carries mark governing system includes: a V-shaped filter chamber; the ultrafiltration device is connected with the water outlet of the V-shaped filter tank; the primary reverse osmosis device is connected with a water production outlet of the ultrafiltration device, and a membrane element arranged in the primary reverse osmosis device is a BW reverse osmosis membrane; the first tubular microfiltration device is connected with a concentrated water outlet of the first-stage reverse osmosis device, and a first softener dosing port is arranged on a connecting pipeline of the first tubular microfiltration device and the concentrated water outlet of the first-stage reverse osmosis device; the second-stage reverse osmosis device is connected with a water production outlet of the first tubular microfiltration device, and a membrane element arranged in the second-stage reverse osmosis device is a BW reverse osmosis membrane; the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device, and a second softener dosing port is arranged on a connecting pipeline between the second tubular microfiltration device and the concentrated water outlet of the second-stage reverse osmosis device; the ion exchange device is connected with the water production outlet of the second tubular microfiltration device; the three-stage reverse osmosis device is connected with a water outlet of the ion exchange device, and a membrane element arranged in the three-stage reverse osmosis device is a SW reverse osmosis membrane; and the evaporation crystallization salt separation equipment is connected with a concentrated water outlet of the third-stage reverse osmosis device. In the utility model, conventionally treated mine water sequentially flows through a V-shaped filter tank, an ultrafiltration device, a first-stage reverse osmosis device, a first tubular microfiltration device, a second-stage reverse osmosis device, a second tubular microfiltration device, an ion exchange device and a third-stage reverse osmosis device, and first-stage product water, second-stage product water and third-stage product water are respectively obtained at water production outlets of the first-stage reverse osmosis device, the second-stage reverse osmosis device and the third-stage reverse osmosis device; and (4) treating concentrated water generated by the third-stage reverse osmosis device in evaporation crystallization salt separation equipment to obtain a crystallization product (sodium sulfate, sodium chloride and the like). The utility model provides a carry mark treatment system can obviously reduce the content of mine aquatic Suspended Solid (SS), dissolubility total solid (TDS), chloride and fluoride, retrieves resources such as sodium sulfate and sodium chloride in the mine aquatic simultaneously, realizes "zero release" of waste water. The utility model provides a carry mark processing system engineering investment province, running cost low, treatment effect stable, have very wide market prospect.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be 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 embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a process flow diagram of a mine water upgrading treatment system provided by an embodiment of the utility model;
FIG. 2 is a process flow diagram of an evaporative crystallization salt separation device provided by the embodiment of the present invention.
Detailed Description
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.
The utility model provides a mark improvement governing system is carried to mine water, include:
a V-shaped filter chamber;
the ultrafiltration device is connected with the water outlet of the V-shaped filter tank;
the primary reverse osmosis device is connected with a water production outlet of the ultrafiltration device, and a membrane element arranged in the primary reverse osmosis device is a BW reverse osmosis membrane;
the first tubular microfiltration device is connected with a concentrated water outlet of the first-stage reverse osmosis device, and a first softener dosing port is arranged on a connecting pipeline of the first tubular microfiltration device and the concentrated water outlet of the first-stage reverse osmosis device;
the second-stage reverse osmosis device is connected with a water production outlet of the first tubular microfiltration device, and a membrane element arranged in the second-stage reverse osmosis device is a BW reverse osmosis membrane;
the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device, and a second softener dosing port is arranged on a connecting pipeline between the second tubular microfiltration device and the concentrated water outlet of the second-stage reverse osmosis device;
the ion exchange device is connected with the water production outlet of the second tubular microfiltration device;
the three-stage reverse osmosis device is connected with a water outlet of the ion exchange device, and a membrane element arranged in the three-stage reverse osmosis device is a SW reverse osmosis membrane;
and the evaporation crystallization salt separation equipment is connected with a concentrated water outlet of the third-stage reverse osmosis device.
Referring to fig. 1 and fig. 2, fig. 1 is a process flow diagram of a mine water upgrading treatment system provided by an embodiment of the present invention, and fig. 2 is a process flow diagram of an evaporation crystallization salt separation device provided by an embodiment of the present invention.
The utility model provides a carry mark treatment system includes V type filtering pond, ultrafiltration device, one-level reverse osmosis unit, first tubular micro-filtration device, second grade reverse osmosis unit, second tubular micro-filtration device, ion exchange device, tertiary reverse osmosis unit and evaporation crystallization and divides salt equipment. The V-shaped filter chamber is provided with a water inlet and a water outlet, and the water inlet of the V-shaped filter chamber is connected with a production port of a conventional treatment system and used for filtering SS in mine water to enable indexes of the SS to meet requirements of a subsequent desalting system on suspended matters.
The utility model discloses in, ultrafiltration device is provided with the water inlet, produces water export and dense water export, ultrafiltration device's water inlet with the delivery port in V type filtering pond links to each other for further improve the quality of water in mine water, reduce the membrane pollution when the sequent reverse osmosis treatment and block up, prolong reverse osmosis membrane's life. In one embodiment of the present invention, the ultrafiltration membrane element installed in the ultrafiltration device is SPF-2880.
In an embodiment of the present invention, the system further comprises a self-cleaning filter, the self-cleaning filter is disposed between the V-shaped filter chamber and the ultrafiltration apparatus, the water inlet of the self-cleaning filter is connected to the water outlet of the V-shaped filter chamber, and the water outlet of the self-cleaning filter is connected to the water inlet of the ultrafiltration apparatus, so as to pre-treat the ultrafiltration influent water, reduce the workload of the ultrafiltration apparatus, and prolong the service life of the ultrafiltration membrane.
The utility model discloses in, one-level reverse osmosis unit is provided with the water inlet, produces the water export and the export of dense water, one-level reverse osmosis unit's water inlet with ultrafiltration device's product water export links to each other for produce water to the ultrafiltration and carry out deep purification, obtain the product water that satisfies the demands. In the present invention, the membrane element installed in the first-stage reverse osmosis apparatus is a Brackish Water (BW) reverse osmosis membrane. In one embodiment of the present invention, the BW reverse osmosis membrane model is BW30 FR-400/34.
In one embodiment provided by the utility model, a reducing agent dosing port is arranged on a connecting pipeline between the produced water outlet of the ultrafiltration device and the water inlet of the primary reverse osmosis device. In the utility model, an oxidant (such as NaHSO) is added in the ultrafiltration generation3) The oxidation-reduction potential generated by ultrafiltration can be reduced, and the subsequent treatment effect is improved.
In one embodiment provided by the utility model, a first scale inhibitor dosing port is arranged on a connecting pipeline between a water outlet of the ultrafiltration device and a water inlet of the primary reverse osmosis device. The utility model discloses in, through throwing the antisludging agent to reverse osmosis into water, preventable and control membrane surface scale deposit, effective control sulphate, carbonate and SiO2And the like.
The utility model discloses in, first tubular micro-filtration device is provided with water inlet, product water export and dense water export. The water inlet of the first tubular microfiltration device is connected with the concentrated water outlet of the first-stage reverse osmosis device, and a first softener dosing port is arranged on a connecting pipeline of the water inlet of the first tubular microfiltration device and the concentrated water outlet of the first-stage reverse osmosis device. The utility model discloses in, can make calcium, magnesium, silicon, fluorine etc. in the reverse osmosis dense water form the sediment through throwing softener to one-level reverse osmosis dense water in, later through first tubular micro-filtration with these precipitate filtering to reach the easy scale deposit ion content of reduction aquatic, reduce the purpose of water hardness. In one embodiment of the present invention, the microfiltration membrane element installed in the first tubular microfiltration device is NT-400.
The utility model provides an embodiment, the system still includes first micro-filtration sludge tank and first sludge filter pressing device, first micro-filtration sludge tank is provided with import, mud drain and supernatant backward flow mouth, first sludge filter pressing device is provided with import and mud drain, the import of first micro-filtration sludge tank with the dense water export of first tubular micro-filtration device links to each other, the mud drain of first micro-filtration sludge tank with first sludge filter pressing device's import links to each other, the supernatant backward flow mouth of first micro-filtration sludge tank with first tubular micro-filtration device links to each other. The utility model discloses in, the dense water that first tubular microfiltration device produced deposits in getting into first microfiltration sludge tank, solid, liquid layering gradually in the dense water of sedimentation process forms supernatant and end mud, and wherein, the supernatant returns to handle in the first tubular microfiltration device through supernatant backward flow mouth, and end mud carries out the filter-pressing in getting into first sludge filter-pressing device through the outer mouth of arranging of mud, and the mud sediment that the filter-pressing produced is outside the outer mouth discharge system of arranging of mud.
The utility model discloses in, second grade reverse osmosis unit is provided with the water inlet, produces water export and dense water export, second grade reverse osmosis unit's water inlet with first tubular micro-filtration device's product water export links to each other for carry out deep purification to tubular micro-filtration product water, obtain the product water that satisfies the demands. In the utility model, the membrane element installed in the second-stage reverse osmosis device is a Brackish Water (BW) reverse osmosis membrane. In one embodiment provided by the present invention, the BW reverse osmosis membrane model is FORTILFECR 100.
In one embodiment provided by the utility model, a second antisludging agent dosing port is arranged on a connecting pipeline between the produced water outlet of the first tubular microfiltration device and the water inlet of the second-stage reverse osmosis device.
The utility model discloses in, second tubular micro-filtration device is provided with water inlet, product water export and dense water export. And a water inlet of the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device, and a second softener dosing port is arranged on a connecting pipeline between the water inlet of the second tubular microfiltration device and the concentrated water outlet of the second-stage reverse osmosis device. The utility model discloses in, can make calcium, magnesium etc. in the reverse osmosis dense water deposit through throwing the softener to adding in the second grade reverse osmosis dense water, later through the filtration of second tubular micro-filtration with these precipitates to reach the easy scale deposit ion content of reduction aquatic, reduce the purpose of water hardness. In one embodiment of the present invention, the microfiltration membrane element installed in the second tubular microfiltration device has the same type as the first tubular microfiltration device.
In an embodiment of the utility model provides an, the system still includes second micro-filtration sludge tank and second sludge filter pressing device, second micro-filtration sludge tank is provided with import, mud drain and supernatant backward flow mouth, second sludge filter pressing device is provided with import and mud drain, the import of second micro-filtration sludge tank with the dense water export of second tubular micro-filtration device links to each other, the mud drain of second micro-filtration sludge tank with second sludge filter pressing device's import links to each other, the supernatant backward flow mouth of second micro-filtration sludge tank with second tubular micro-filtration device links to each other. The utility model discloses in, the working process reference of second micro-filtration sludge groove and second sludge filter pressing device first micro-filtration sludge groove and first sludge filter pressing device are no longer repeated here.
The utility model discloses in, ion exchange unit includes water inlet and delivery port, ion exchange unit's water inlet with the product water export of second tubular micro-filtration device links to each other for further get rid of Ca in the second tubular micro-filtration product water2+、Mg2+、Ba2+、Sr2+And ions which are easy to scale are generated, so that the aim of further softening the second tubular microfiltration produced water is fulfilled.
The utility model discloses in, tertiary reverse osmosis unit is provided with the water inlet, produces water export and dense water export, tertiary reverse osmosis unit's water inlet with ion exchange unit's play water export links to each other for go out the ion exchange and carry out deep purification, obtain the product water that satisfies the demands. In the utility model, the membrane element installed in the third-stage reverse osmosis device is a Seawater (SW) reverse osmosis membrane. In one embodiment provided herein, the SW reverse osmosis membrane model is FORTILFEXC 70.
The utility model discloses in, the water inlet of evaporation crystallization salt separating equipment with tertiary reverse osmosis unit's dense water export links to each other for carry out the evaporation crystallization to tertiary reverse osmosis concentration, realize the zero release of waste water.
In one embodiment of the present invention, the system further comprises a concentrated brine tank, wherein the concentrated brine tank is provided with a water inlet and a water outlet. The utility model discloses in, the strong brine sets up tertiary reverse osmosis unit with between the evaporation crystallization salt equipment, the water inlet of strong brine with tertiary reverse osmosis unit's dense water export links to each other, the delivery port of strong brine with the evaporation crystallization salt equipment is divided the water inlet of water equipment and is linked to each other. The utility model discloses in, the strong brine pond is used for treating the evaporation crystal water and carries out homogeneity, equal volume.
In one embodiment provided by the present invention, the system further comprises a third tubular microfiltration device, the third tubular microfiltration device is provided with a water inlet, a produced water outlet and a concentrated water outlet. The utility model discloses in, third tubular micro-filtration device sets up tertiary reverse osmosis unit with between the thick brine pond, third tubular micro-filtration device's water inlet with tertiary reverse osmosis unit's dense water export links to each other, is provided with third softener dosing port on its connecting pipeline, third tubular micro-filtration device produce the water export with the water inlet of strong brine links to each other. The utility model discloses in, can make calcium, magnesium etc. in the tertiary reverse osmosis dense water deposit through throwing softener to tertiary reverse osmosis dense water in, later through the filtering of third tubular microfiltration with these precipitates to reach the easy scale deposit ion content of reduction aquatic, reduce the purpose of water hardness. In one embodiment of the present invention, the microfiltration membrane element installed in the third tubular microfiltration device is the same type as the first tubular microfiltration device.
In an embodiment of the utility model provides an, the system still includes third micro-filtration sludge tank and third sludge filter pressing device, third micro-filtration sludge tank is provided with import, mud drain and supernatant backward flow mouth, third sludge filter pressing device is provided with import and mud drain, the import of third micro-filtration sludge tank with the dense water export of third tubular micro-filtration device links to each other, the mud drain of third micro-filtration sludge tank with third sludge filter pressing device's import links to each other, the supernatant backward flow mouth of third micro-filtration sludge tank with third tubular micro-filtration device links to each other. The utility model discloses in, third microfiltration sludge tank and third sludge filter pressing device's working process reference first microfiltration sludge tank and first sludge filter pressing device are no longer repeated here.
In one embodiment provided by the utility model, the evaporation crystallization divides salt equipment to include: the device comprises a preheater, an MVR falling film evaporator, an MVR nitrate separating device and a salt separating device. The preheater is provided with a water inlet and a water outlet, and the water inlet of the preheater is connected with the concentrated water outlet of the third-stage reverse osmosis device and is used for preheating the waste water to be evaporated and crystallized. The utility model provides an in the embodiment of being provided with concentrated brine pond, the water inlet of pre-heater with the delivery port in concentrated brine pond links to each other.
The utility model discloses in, MVR falling film evaporator is provided with water inlet, concentrate export and falling film evaporator compression fan, MVR falling film evaporator's water inlet with the delivery port of pre-heater links to each other. The utility model discloses in, the waste water after preheating carries out evaporative concentration in getting into MVR falling film evaporator through the water inlet, and the waste water after the concentration passes through the concentrate export and gets into the epilogue technology, and among the evaporative concentration process, the flash evaporation that the falling film evaporator produced converts the heating steam of high quality as the heating heat source of falling film evaporator into after falling film evaporator compression fan acting.
The utility model discloses in, MVR analyses nitre device is provided with water inlet, supernatant export, magma export and analyses nitre device compression fan, MVR analyses the water inlet of nitre device with MVR falling film evaporator's concentrate export links to each other. In the utility model, the concentrated solution generated by the MVR falling film evaporator enters the MVR saltpeter analysis device through the water inlet for further evaporation and concentration, and sodium sulfate crystals (mirabilite) are separated out; then discharging the base solution containing a large amount of sodium sulfate crystals through a crystal mush outlet for subsequent processing, and discharging the supernatant through a supernatant outlet to enter a salt precipitation device; in the evaporation concentration process, secondary steam generated by the nitrate separating device is converted into high-quality heating steam as a heating heat source of the nitrate separating device after acting through a compression fan of the nitrate separating device.
The utility model discloses in, the salting device is provided with water inlet and magma export, the water inlet of salting device with MVR analyses nitre device's supernatant export and links to each other for further evaporative concentration is carried out to the clear liquid that MVR analyzed nitre device to produce, appears out the sodium chloride crystal.
In an embodiment of the utility model provides an, the evaporation crystallization divides salt equipment still includes sodium sulfate magma centrifuge, sodium sulfate desicator, sodium chloride magma centrifuge and sodium chloride desicator. Wherein, sodium sulfate magma centrifuge is provided with feed inlet, wet crystal bin outlet and mother liquor export, the sodium sulfate desicator is provided with feed inlet and discharge gate, sodium sulfate magma centrifuge's feed inlet with the crystal thick liquid export of MVR saltpeter precipitation device links to each other, sodium sulfate magma centrifuge's wet crystal bin outlet with the feed inlet of sodium sulfate desicator links to each other. In the utility model, the crystal mush generated by the MVR nitrate separating device enters a sodium sulfate crystal mush centrifuge for solid-liquid separation, and the solid phase (sodium sulfate wet crystal) obtained by the solid-liquid separation enters a sodium sulfate dryer for drying, so as to obtain an anhydrous sodium sulfate product; the liquid phase (mother liquor) obtained by the solid-liquid separation can be returned to the MVR nitrate analysis device for continuous treatment.
The utility model discloses in, sodium chloride magma centrifuge is provided with feed inlet, wet crystal bin outlet and mother liquor export, the sodium chloride desicator is provided with feed inlet and discharge gate, sodium chloride magma centrifuge's feed inlet with the magma export of salting-out device links to each other, sodium chloride magma centrifuge's wet crystal bin outlet with the feed inlet of sodium chloride desicator links to each other. In the utility model, the crystal mush generated by the salt precipitation device enters a sodium chloride crystal mush centrifuge for solid-liquid separation, and a solid phase (sodium chloride wet crystal) obtained by the solid-liquid separation enters a sodium chloride drier for drying, so as to obtain an anhydrous sodium chloride product; the liquid phase (mother liquor) obtained by the solid-liquid separation can be returned to the salt precipitation device for continuous treatment.
The utility model discloses in, the mine water through conventional treatment flows through above-mentioned each processing apparatus in proper order, obtains one-level product water, second grade product water, tertiary product water in one-level reverse osmosis unit, second grade reverse osmosis unit, tertiary reverse osmosis unit's product water export respectively, obtains crystallization product (sodium sulfate, sodium chloride etc.) in evaporation crystallization salt separating equipment. The utility model provides a carry mark treatment system can obviously reduce the content of mine aquatic Suspended Solid (SS), dissolubility total solid (TDS), chloride and fluoride, retrieves resources such as sodium sulfate and sodium chloride in the mine aquatic simultaneously, realizes "zero release" of waste water. The utility model provides a carry mark processing system engineering investment province, running cost low, treatment effect stable, have very wide market prospect.
The utility model also provides a mine water carries mark treatment method, including following step:
a) treating mine water to be subjected to extraction in a V-shaped filter to obtain outlet water of the V-shaped filter;
b) performing ultrafiltration on the outlet water of the V-shaped filter tank to obtain ultrafiltration product water;
c) performing primary reverse osmosis on the ultrafiltration produced water to obtain primary product water and primary reverse osmosis concentrated water; the membrane element adopted by the first-stage reverse osmosis is a BW reverse osmosis membrane;
d) adding a softening agent into the first-stage reverse osmosis concentrated water, and then carrying out primary tubular microfiltration to obtain primary tubular microfiltration produced water;
e) performing secondary reverse osmosis on the primary tubular microfiltration produced water to obtain secondary product water and secondary reverse osmosis concentrated water; the membrane element adopted by the secondary reverse osmosis is a BW reverse osmosis membrane;
f) adding a softening agent into the secondary reverse osmosis concentrated water, and then performing secondary tubular microfiltration to obtain secondary tubular microfiltration produced water;
g) performing ion exchange treatment on the secondary tubular microfiltration produced water, and then performing third-stage reverse osmosis to obtain third-stage product water and third-stage reverse osmosis concentrated water; the membrane element adopted by the third-stage reverse osmosis is a SW reverse osmosis membrane;
h) and evaporating and crystallizing the third-stage reverse osmosis concentrated water to obtain a crystallized product.
The utility model provides a carry mark treatment method, treat that the mine water of carrying mark is handled at first in V type filtering pond, obtain V type filtering pond and go out water. The mine water to be extracted is mine water treated by a conventional mine water treatment process. The utility model provides an embodiment, treat the pH value of mark mine water and be 6 ~ 9, treat the SS of mark mine water and be less than or equal to 50mg/L, treat the content of petroleum class pollutant in the mark mine water and be less than or equal to 0.05mg/L, treat the TDS of mark mine water and be less than or equal to 1680mg/L, treat the SO of mark mine water4 2-The content is less than or equal to 90mg/L, and the Cl of the mine water to be extracted-The content is less than or equal to 576mg/L, and F of the mine water to be extracted-The content is less than or equal to 7.9 mg/L. The utility model discloses in, the filtration speed of V type filtering pond is preferred 5 ~ 10m/h, specifically can be 5m/h, 6m/h, 7m/h, 8m/h, 9m/h or 10 m/h.
The utility model provides a carry mark treatment method, after obtaining V type filtering pond effluent, V type filtering pond effluent is carried out the ultrafiltration. In the utility model discloses in V type filtering pond effluent is preferably earlier filtered through self-cleaning filter before carrying out the ultrafiltration, the filter fineness of self-cleaning filter is preferably 50 ~ 200 μm, specifically can be 50 μm, 100 μm, 150 μm or 200 μm. In the present invention, the ultrafiltration is preferably carried out in the ultrafiltration device described above, and the recovery rate during operation of the ultrafiltration device is preferably not less than 90%, and specifically may be 95%. The utility model discloses in, V type filtering pond goes out water and after the ultrafiltration, obtains the ultrafiltration and produces water, the turbidity of ultrafiltration production water is preferred to be less than or equal to 1 NTU.
The utility model provides a standard-lifting treatment method, after obtaining the ultrafiltration water production, theAnd performing primary reverse osmosis on the ultrafiltration produced water. In the utility model discloses in, the ultrafiltration product water is preferably earlier to before carrying out one-level reverse osmosis throw reducing agent and/or antisludging agent in the ultrafiltration product water. Wherein the reducing agent includes, but is not limited to NaHSO3The adding amount of the reducing agent is preferably 5-20 g/t of water, and specifically can be 5g/t of water, 10g/t of water, 15g/t of water or 20g/t of water; the scale inhibitor is preferably MDC 220; the adding amount of the scale inhibitor is preferably 1-10 g/t water, and specifically can be 1g/t water, 3g/t water, 5g/t water, 7g/t water or 10g/t water. In the present invention, the first-stage reverse osmosis is preferably performed in the first-stage reverse osmosis apparatus described above, and the recovery rate of the first-stage reverse osmosis apparatus during operation is preferably not less than 60%, and specifically may be 70%; the desalination rate of the first-stage reverse osmosis device during operation is preferably more than or equal to 95%, and more preferably more than or equal to 98.5%. The utility model discloses in, the ultrafiltration is produced water and is obtained one-level product water and the dense water of one-level reverse osmosis after one-level reverse osmosis, wherein, the TDS of one-level product water is preferred to be less than or equal to 100mg/L, the TDS of one-level reverse osmosis dense water is preferred to be more than or equal to 3500 mg/L.
The utility model provides a carry mark treatment method, after obtaining one-level reverse osmosis dense water, to add the softener in the one-level reverse osmosis dense water, later carry out once tubular micro-filtration. Wherein the softening agent includes, but is not limited to, one or more of magnesium agent, sodium hydroxide and sodium carbonate; the addition amount of the magnesium agent is preferably 10-20 g/t of water, and specifically can be 10g/t of water, 12g/t of water, 15g/t of water, 17g/t of water or 20g/t of water; the adding amount of the sodium hydroxide is preferably 50-200 g/t of water, and specifically can be 50g/t of water, 80g/t of water, 100g/t of water, 120g/t of water, 150g/t of water or 200g/t of water; the adding amount of the sodium carbonate is preferably 10-50 g/t of water, and specifically can be 10g/t of water, 20g/t of water, 30g/t of water, 40g/t of water or 50g/t of water. In the present invention, the first tubular microfiltration device is preferably performed in the first tubular microfiltration device described above, the filtration mode when the first tubular microfiltration device is operated is preferably large-cycle filtration, and the cycle rate is preferably not less than 4 times; the recovery rate of the first tubular microfiltration device during operation is preferably more than or equal to 95 percent, and can be 98 percent. The utility model discloses in, the concentrated water of one-level reverse osmosis is through once tubular micro-filtration back, obtains once tubular micro-filtration product water and once tubular micro-filtration concentrated water. Wherein, the primary tubular microfiltration concentrated water is preferably treated according to the following modes: precipitating the primary tubular microfiltration concentrated water to form supernatant and bottom slurry; the supernatant is returned to the primary tubular microfiltration process, and the bottom slurry is discharged after being subjected to filter pressing.
The utility model provides a carry mark treatment method, after obtaining tubular microfiltration product water of once, tubular microfiltration product water of once carries out second grade reverse osmosis. The utility model discloses in, once tubular microfiltration produces water before carrying out second grade reverse osmosis, preferably earlier to once tubular microfiltration produces water and adds the antisludging agent. Wherein the scale inhibitor is preferably MDC 220; the adding amount of the scale inhibitor is preferably 1-10 g/t water, and specifically can be 1g/t water, 3g/t water, 5g/t water, 7g/t water or 10g/t water. In the present invention, the second-stage reverse osmosis is preferably performed in the second-stage reverse osmosis apparatus described above, and the recovery rate of the second-stage reverse osmosis apparatus during operation is preferably not less than 65%, and specifically may be 75%; the salt rejection rate of the secondary reverse osmosis device during operation is preferably more than or equal to 95 percent, and more preferably more than or equal to 98 percent. The utility model discloses in, once tubular microfiltration produces water behind second grade reverse osmosis, obtains second grade product water and second grade reverse osmosis dense water, wherein, the TDS of second grade product water is preferred to be less than or equal to 200mg/L, the TDS of second grade reverse osmosis dense water is preferred to be more than or equal to 18000 mg/L.
The utility model provides a carry mark treatment method, after obtaining second grade reverse osmosis dense water, to throw the softener into in the second grade reverse osmosis dense water, later carry out secondary tubular micro-filtration. Wherein the softening agent includes, but is not limited to, one or more of magnesium agent, sodium hydroxide and sodium carbonate; the addition amount of the magnesium agent is preferably 10-20 g/t of water, and specifically can be 10g/t of water, 12g/t of water, 15g/t of water, 17g/t of water or 20g/t of water; the adding amount of the sodium hydroxide is preferably 50-200 g/t of water, and specifically can be 50g/t of water, 80g/t of water, 100g/t of water, 120g/t of water, 150g/t of water or 200g/t of water; the adding amount of the sodium carbonate is preferably 10-50 g/t of water, and specifically can be 10g/t of water, 20g/t of water, 30g/t of water, 40g/t of water or 50g/t of water. In the present invention, the second tubular microfiltration device is preferably performed in the second tubular microfiltration device described above, the filtration mode when the second tubular microfiltration device is operated is preferably large-cycle filtration, and the cycle rate is preferably not less than 4 times; the recovery rate of the second tubular microfiltration device during operation is preferably more than or equal to 95 percent, and can be 98 percent. The utility model discloses in, the concentrated water of second grade reverse osmosis obtains secondary tubular micro-filtration product water and the concentrated water of secondary tubular micro-filtration after the secondary tubular micro-filtration. Wherein, the secondary tubular microfiltration concentrated water is preferably treated according to the following modes: precipitating the secondary tubular microfiltration concentrated water to form supernatant and bottom slurry; and returning the supernatant to the secondary tubular microfiltration process, and discharging the bottom slurry after filter pressing.
The utility model provides a carry mark treatment method, after obtaining secondary tubular microfiltration product water, secondary tubular microfiltration product water carries out ion exchange treatment. Wherein, the ion exchange is preferably carried out in the ion exchange device described above, and is not described in detail herein. And after ion exchange is completed, obtaining ion exchange effluent.
The utility model provides a carry mark treatment method, after obtaining ion exchange effluent, ion exchange effluent carries out tertiary reverse osmosis. Wherein, the three-stage reverse osmosis is preferably carried out in the three-stage reverse osmosis device introduced above, and the recovery rate of the three-stage reverse osmosis device during operation is preferably more than or equal to 65 percent, and particularly can be 75 percent; the salt rejection rate of the secondary reverse osmosis device during operation is preferably more than or equal to 95 percent, and more preferably more than or equal to 98 percent. The utility model discloses in, ion exchange goes out the water and after tertiary reverse osmosis, obtains tertiary product water and tertiary reverse osmosis dense water, wherein, the TDS of tertiary product water is preferred to be less than or equal to 500mg/L, the TDS of tertiary reverse osmosis dense water is preferred to be more than or equal to 70000 mg/L.
The utility model provides a carry mark treatment method, after obtaining tertiary reverse osmosis dense water, tertiary reverse osmosis dense water evaporates the crystallization. In the present invention, the third-stage reverse osmosis concentrated water is preferably homogenized and equalized in the concentrated brine tank described above before being subjected to evaporative crystallization. The utility model discloses in, tertiary reverse osmosis dense water is carried out the homogeneity and before the even volume, preferably earlier to add the softener in the tertiary reverse osmosis dense water to carry out cubic tubular micro-filtration. Wherein the softening agent includes, but is not limited to, one or more of magnesium agent, sodium hydroxide and sodium carbonate; the addition amount of the magnesium agent is preferably 10-20 g/t of water, and specifically can be 10g/t of water, 12g/t of water, 15g/t of water, 17g/t of water or 20g/t of water; the adding amount of the sodium hydroxide is preferably 50-200 g/t of water, and specifically can be 50g/t of water, 80g/t of water, 100g/t of water, 120g/t of water, 150g/t of water or 200g/t of water; the adding amount of the sodium carbonate is preferably 10-50 g/t of water, and specifically can be 10g/t of water, 20g/t of water, 30g/t of water, 40g/t of water or 50g/t of water. In the present invention, the third tubular microfiltration device is preferably performed in the third tubular microfiltration device described above, the filtration mode when the third tubular microfiltration device is operated is preferably large-cycle filtration, and the cycle rate is preferably not less than 4 times; the recovery rate of the third tubular microfiltration device during operation is preferably more than or equal to 95 percent, and can be 98 percent. The utility model discloses in, tertiary reverse osmosis dense water obtains cubic tubular micro-filtration product water and cubic tubular micro-filtration dense water after secondary tubular micro-filtration. Wherein, the triple tubular microfiltration produced water is conveyed to the concentrated brine pond for homogenization and quantity equalization; the tertiary tubular microfiltration concentrate is preferably treated in the following manner: precipitating the tertiary tubular microfiltration concentrated water to form supernatant and bottom mud; and returning the supernatant to the tertiary tubular microfiltration process, and discharging the bottom slurry after filter pressing.
The utility model provides a carry mark treatment method, the technology that the evaporation crystallization adopted is preferably mechanical vapor recompression evaporation technology (MVR). The utility model discloses in, preferably in the evaporation crystallization preferably go on in the evaporation crystallization divides salt equipment that introduces above, this equipment includes preheater, MVR falling film evaporator, MVR and analyse nitre device, sodium sulfate crystal slurry centrifuge, sodium sulfate desicator, salt separating device, sodium chloride crystal slurry centrifuge and sodium chloride desicator. In the utility model, the feeding temperature when the MVR falling film evaporator operates is preferably 75-85 ℃, and specifically can be 75 ℃, 80 ℃, 80.6 ℃ or 85 ℃; the temperature of heating steam during the operation of the MVR falling-film evaporator is preferably 95-100 ℃, and specifically can be 95 ℃, 97 ℃, 98.3 ℃ or 100 ℃; the secondary steam temperature of the MVR falling-film evaporator during operation is preferably 85-90 ℃, and particularlyCan be 85 deg.C, 87 deg.C, 87.8 deg.C or 90 deg.C; the total heat transfer coefficient of the MVR falling film evaporator during operation is preferably 5000-7000W/(m)2DEG C) of 5000W/(m)2·℃)、5500W/(m2·℃)、6000W/(m2·℃)、6500W/(m2DEG C) or 7000W/(m2℃); the shell pass pressure of the MVR falling film evaporator during operation is preferably 4-8 barg/FV, and specifically can be 4barg/FV, 4.5barg/FV, 5barg/FV, 5.5barg/FV, 6barg/FV, 6.5barg/FV, 7barg/FV, 7.5barg/FV or 8 barg/FV; the tube pass pressure of the MVR falling film evaporator during operation is preferably 1-2 barg/FV, and specifically can be 1barg/FV, 1.2barg/FV, 1.5barg/FV, 1.7barg/FV or 2 barg/FV. In the utility model, the concentrated water of tertiary reverse osmosis is evaporated and crystallized to obtain crystallized products (sodium sulfate, sodium chloride, etc.).
The utility model provides a carry mark treatment method carries out a series of processings through the mine water after handling the conventionality, can obviously reduce the content of mine aquatic Suspended Solid (SS), dissolubility total solid (TDS), chloride and fluoride, retrieves resources such as sodium sulfate and sodium chloride in the mine aquatic simultaneously, realizes "zero release" of waste water. The utility model provides a carry mark processing method engineering investment province, running cost are low, the treatment effect is stable, has very wide market prospect.
For the sake of clarity, the following examples are given in detail.
Examples
The mine water upgrading treatment system provided by the embodiment is shown in fig. 1 and comprises: v type filtering pond, self-cleaning filter, ultrafiltration device, one-level reverse osmosis unit, first tubular micro-filtration device, first micro-filtration sludge tank, first mud filter pressing device, second grade reverse osmosis unit, second tubular micro-filtration device, second micro-filtration sludge tank, second mud filter pressing device, ion exchange device, tertiary reverse osmosis unit, third tubular micro-filtration device, third micro-filtration sludge tank, third mud filter pressing device, concentrated salt pond and evaporation crystallization divide salt equipment. The specific connection relationship between the devices and the equipment is introduced above, and is not described herein again.
In this embodiment, the evaporative crystallization salt separation device is shown in fig. 2, and includes: the system comprises a preheater, an MVR falling film evaporator, an MVR nitrate separating device, a sodium sulfate crystal slurry centrifuge, a sodium sulfate dryer, a salt separating device, a sodium chloride crystal slurry centrifuge and a sodium chloride dryer, wherein the specific connection relationship among the devices is described above and is not described herein again.
In this embodiment, the specification parameters and operating conditions of the key devices are as follows:
(1) v-shaped filter tank
Semi-underground type steel concrete structure with filtering speed of 8m/h and 1 seat of 3 lattices
(2) Self-cleaning filter
Parameters are as follows: q is 240t/h, the power is 0.5kW, and the filtering precision is 100 mu m; quantity: 4, the device is used.
(3) Ultrafiltration device
Parameters are as follows: an imported ultrafiltration membrane (the model is SPF-2880), the single set of treatment capacity is 240t/h, the turbidity of produced water is less than or equal to 1NTU, and the recovery rate is 95 percent;
quantity: 4 sets of the medicine are prepared;
adding reducing agent NaHSO into ultrafiltration water3(10g/t water) the redox potential was lowered.
(4) First-stage reverse osmosis device
Parameters are as follows: adopting a BW reverse osmosis membrane (the model is BW30FR-400/34) with lower osmotic pressure, wherein the single set of treatment capacity is 225t/h, the recovery rate is 70 percent, and the desalination rate is more than or equal to 98.5 percent;
quantity: 4 sets of the medicine are prepared;
adding a scale inhibitor MDC220(5g/t water) before the ultrafiltration water enters a first-stage reverse osmosis device; the TDS of the produced water (first-grade product water) of the first-grade reverse osmosis device is less than or equal to 100mg/L, and the TDS of the concentrated water is more than or equal to 3500 mg/L.
(5) First tubular microfiltration device
Parameters are as follows: the type of the micro-filtration membrane is NT-400, the single set of processing capacity is 135t/h, the recovery rate is 98 percent, a large circulation filtration mode is adopted, and the circulation multiplying power is more than or equal to 4 times;
quantity: 2, sleeving;
before the first-stage reverse osmosis concentrated water enters a first tubular microfiltration device, magnesium agent (15g/t water), sodium hydroxide (100g/t water) and sodium carbonate (30g/t water) are added.
(6) Two-stage reverse osmosis device
Parameters are as follows: adopting a BW reverse osmosis membrane (the model is FORTILFECR100) with lower osmotic pressure, wherein the single set of treatment capacity is 135t/h, the recovery rate is 75 percent, and the desalination rate is more than or equal to 98 percent;
quantity: 2, sleeving;
before the first tubular microfiltration produced water enters a second-stage reverse osmosis device, adding a scale inhibitor MDC220(5g/t water); the TDS of the produced water (secondary product water) of the secondary reverse osmosis device is less than or equal to 200mg/L, and the TDS of the concentrated water is more than or equal to 18000 mg/L.
(7) Second pipe type microfiltration device
Parameters are as follows: the type of the micro-filtration membrane is NT-400, the single set of processing capacity is 35t/h, the recovery rate is more than or equal to 98 percent, a large circulation filtration mode is adopted, and the circulation multiplying power is more than or equal to 4 times;
quantity: 2, sleeving;
before the second-stage reverse osmosis concentrated water enters the second tubular microfiltration device, magnesium agent (15g/t water), sodium hydroxide (100g/t water) and sodium carbonate (30g/t water) are added.
(8) Three-stage reverse osmosis device
Parameters are as follows: the single set of treatment capacity is 35t/h by adopting an SWRO reverse osmosis membrane (the model is FORTILFEXC70), the recovery rate is 75 percent, and the desalination rate is more than or equal to 98 percent;
quantity: 2, sleeving;
the TDS of the produced water (third-stage product water) of the third-stage reverse osmosis device is less than or equal to 500mg/L, and the TDS of the concentrated water is more than or equal to 70000 mg/L.
(9) MVR falling film evaporator
The feed temperature was 80.6 ℃, the temperature of the heating steam was 98.3 ℃, the temperature of the secondary steam was 87.8 ℃, the temperature difference loss was 1.5 ℃, the total heat transfer coefficient was 6000W/(m2 · ℃), the shell-side pressure was 6barg/FV, and the tube-side pressure was 1.5 barg/FV.
In this example, the main water quality indexes of raw water entering the V-shaped filter are shown in table 1:
TABLE 1 Main Water quality index of mine Water after conventional treatment
The detection results of the primary product water, the secondary product water and the tertiary product water obtained by the treatment of the embodiment show that the three product waters all meet the III-class standard of the quality standard of surface water environment (GB 3838-2002).
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (7)
1. A mine water upgrading treatment system is characterized by comprising:
a V-shaped filter chamber;
the ultrafiltration device is connected with the water outlet of the V-shaped filter tank;
the primary reverse osmosis device is connected with a water production outlet of the ultrafiltration device, and a membrane element arranged in the primary reverse osmosis device is a BW reverse osmosis membrane;
the first tubular microfiltration device is connected with a concentrated water outlet of the first-stage reverse osmosis device, and a first softener dosing port is arranged on a connecting pipeline of the first tubular microfiltration device and the concentrated water outlet of the first-stage reverse osmosis device;
the second-stage reverse osmosis device is connected with a water production outlet of the first tubular microfiltration device, and a membrane element arranged in the second-stage reverse osmosis device is a BW reverse osmosis membrane;
the second tubular microfiltration device is connected with a concentrated water outlet of the second-stage reverse osmosis device, and a second softener dosing port is arranged on a connecting pipeline between the second tubular microfiltration device and the concentrated water outlet of the second-stage reverse osmosis device;
the ion exchange device is connected with the water production outlet of the second tubular microfiltration device;
the three-stage reverse osmosis device is connected with a water outlet of the ion exchange device, and a membrane element arranged in the three-stage reverse osmosis device is a SW reverse osmosis membrane;
and the evaporation crystallization salt separation equipment is connected with a concentrated water outlet of the third-stage reverse osmosis device.
2. The mine water upgrading treatment system according to claim 1, further comprising a self-cleaning filter, wherein the self-cleaning filter is arranged between the V-shaped filter pool and the ultrafiltration device, a water inlet of the self-cleaning filter is connected with a water outlet of the V-shaped filter pool, and a water outlet of the self-cleaning filter is connected with a water inlet of the ultrafiltration device.
3. The mine water upgrading treatment system according to claim 1, further comprising a concentrated brine tank, wherein the concentrated brine is arranged between the third-stage reverse osmosis device and the evaporation crystallization salt separation equipment, a water inlet of the concentrated brine is connected with a concentrated water outlet of the third-stage reverse osmosis device, and a water outlet of the concentrated brine is connected with a water inlet of the evaporation crystallization salt separation equipment.
4. The mine water upgrading treatment system according to claim 3, further comprising a third tubular microfiltration device, wherein the third tubular microfiltration device is arranged between the third-stage reverse osmosis device and the concentrated brine pond, a water inlet of the third tubular microfiltration device is connected with a concentrated water outlet of the third-stage reverse osmosis device, a third softening agent dosing port is arranged on a connecting pipeline of the third tubular microfiltration device, and a water production outlet of the third tubular microfiltration device is connected with a water inlet of the concentrated brine.
5. The mine water upgrading treatment system according to claim 1, wherein a reducing agent dosing port is arranged on a connecting pipeline between a water production outlet of the ultrafiltration device and the primary reverse osmosis device.
6. The mine water upgrading system according to claim 1, wherein the evaporative crystallization salt separation equipment comprises:
the preheater is connected with a concentrated water outlet of the third-stage reverse osmosis device;
the MVR falling film evaporator is connected with a water outlet of the preheater;
the MVR nitrate analysis device is connected with a concentrated solution outlet of the MVR falling film evaporator;
and the salt separating device is connected with a supernatant outlet of the MVR nitrate separating device.
7. The mine water upgrading treatment system according to claim 6, further comprising a sodium sulfate crystal slurry centrifuge, a sodium sulfate dryer, a sodium chloride crystal slurry centrifuge and a sodium chloride dryer;
a feed port of the sodium sulfate crystal slurry centrifuge is connected with a crystal slurry outlet of the MVR nitrate separating device, and a wet crystal discharge port of the sodium sulfate crystal slurry centrifuge is connected with a feed port of the sodium sulfate dryer;
the feed inlet of the sodium chloride crystal slurry centrifuge is connected with a crystal slurry outlet of the salt precipitation device, and the wet crystal discharge port of the sodium chloride crystal slurry centrifuge is connected with the feed inlet of the sodium chloride dryer.
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