CN215975369U - High salt waste water salt separation crystallization system that contains - Google Patents
High salt waste water salt separation crystallization system that contains Download PDFInfo
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- CN215975369U CN215975369U CN202120564953.6U CN202120564953U CN215975369U CN 215975369 U CN215975369 U CN 215975369U CN 202120564953 U CN202120564953 U CN 202120564953U CN 215975369 U CN215975369 U CN 215975369U
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Abstract
The utility model provides a high-salt-content waste water salt separation crystallization system which comprises a waste water adjusting tank, a sedimentation tank, a clarification tank, a filtering device, a salt separation system, a first concentration system, a second concentration system, a first purification system, a second purification system, an MVR evaporative crystallizer, a freezing crystallizer, a melting crystallizer and a mixed salt crystallizer; the wastewater adjusting tank, the sedimentation tank, the clarification tank, the filtering device and the salt separating system are sequentially connected, the salt separating system comprises a booster pump, a security filter, a salt separating high-pressure pump, an intersegmental booster pump and a nanofiltration membrane group, and the purification system comprises a wastewater CODcr removing device and a carbon and nitrogen removal reactor; according to the utility model, the water produced by the NF membrane of the wastewater and the concentrated water produced by the NF membrane can be obtained through a salt separation system, wherein the water produced by the NF membrane mainly comprises sodium chloride, and then the sodium chloride is obtained through concentration treatment, purification treatment and evaporative crystallization; and the NF membrane concentrated water sodium sulfate and sodium chloride are mainly used for obtaining sodium sulfate crystal salt after purification, concentration, freezing crystallization and melting crystallization.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a high-salt-content wastewater salt separation crystallization system.
Background
Desulfurization wastewater, mine tail water, coal chemical wastewater and the like generated in the industries of electric power, petrochemical industry, coal chemical industry and the like generally have the characteristics of high salt content, high hardness, complex components, high pollution and the like, and serious environmental pollution is caused if unreasonable treatment is carried out. In view of the fact that these industries are generally located in ecologically vulnerable areas, there is no pollutant to be discharged from the contained water, and there is no sufficient water source around the factory, and a high-recovery water treatment device is required to meet the production requirement, therefore, zero/near-zero discharge of wastewater has gradually become an industry trend in order to protect the external requirement of ecological environment and the self requirement of resource utilization.
The currently widely adopted ' near zero emission ' technical route of ' pretreatment-biochemical treatment (optional) ' -advanced treatment-high brine treatment ', the finally produced crystallized salt contains various inorganic salts and a large amount of organic matters. From the viewpoint of enhancing environmental protection, miscellaneous salts generated from high-salt-content wastewater are tentatively solid hazardous wastes. The cost for treating solid hazardous wastes in China is basically more than 3000 yuan/ton at present, and the cost is even higher than the sum of the costs of each working section such as front-stage pretreatment, membrane concentration, evaporative crystallization and the like. Therefore, in the design of the whole high-salinity wastewater treatment process, the final solid product can be sold as a product rather than solid hazardous waste, so that the method has great application value.
The current thinking of salt is basically resource utilization, namely quality-based and salt-based treatment. The most main components of salts in the high-salt wastewater are sodium chloride and sodium sulfate, and the sum of the two components can account for 90-95% of all the salts in the wastewater, so the current mainstream technical direction is to focus on realizing industrial purification and separation of sodium sulfate and sodium chloride in the evaporation crystallization process, so that the possibility of external sale of the manufactured industrial product is provided.
There are two main types of currently used quality-based and salt-based treatments: a pure hot crystallization salt separation process, a nanofiltration membrane method salt separation and hot/cold crystallization combined process.
Chinese patent application CN201610072782.9 discloses a high-salt-content industrial wastewater salt-separation zero-discharge system, in the method, after high-salt-content wastewater is treated by a precision pretreatment unit, a membrane separation concentration unit and a crystallization resource unit, produced water can be recycled, and sodium chloride, sodium sulfate, sodium nitrate crystal salt and miscellaneous salt are obtained.
Chinese patent application CN201520251103.5 discloses a low energy consumption coal chemical industry strong brine divides matter crystallization composite set, and the device includes: the device comprises a hardness-removing softening device, an NF separation membrane device, a high-salinity reverse osmosis device, a produced water ED membrane concentration device, a produced water evaporation crystallization device, a produced water mother liquor dryer, an AOP catalytic oxidation device, an activated carbon filtration device, a concentrated ED membrane concentration device, a concentrated water evaporation crystallization device and a concentrated water mother liquor dryer. Realize the whole recycle of coal industry strong brine through above-mentioned device, realize the zero release.
In the technical scheme, the separation of sodium chloride and sodium sulfate crystal salt can be realized, but the produced miscellaneous salt is large in amount, the salt recovery rate is low, the purity of the product salt is low, and the problems that the product salt is difficult to export, the hazardous waste disposal quantity of miscellaneous salt is high and the like exist. Therefore, it is an urgent need to solve the problem of providing a technique for completely separating salt and crystallizing high-salt wastewater.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model provides a high-salt-content waste water salt-separating crystallization system.
The technical scheme of the utility model is as follows: a high-salt-content waste water salt separation crystallization system comprises a waste water regulating tank, a sedimentation tank, a clarification tank, a filtering device, a salt separation system, a first concentration system, a second concentration system, a first purification system, a second purification system, an MVR evaporative crystallizer, a freezing crystallizer, a melting crystallizer and a mixed salt crystallizer which are sequentially connected;
the salt separation system comprises a booster pump, a filter, a salt separation high-pressure pump, an intersegmental booster pump and a nanofiltration membrane group which are connected in sequence, wherein a NF membrane water production port of the nanofiltration membrane group is connected with the first concentration system;
the first concentration system comprises a primary concentration unit and a secondary concentration unit, the primary concentration unit comprises a first high-pressure pump and a primary reverse osmosis membrane concentration device, the secondary concentration unit comprises a second high-pressure pump and a secondary reverse osmosis membrane concentration device, the input end of the first high-pressure pump is connected with a NF membrane water production port, the output end of the first high-pressure pump is connected with the input end of the primary reverse osmosis membrane concentration device, the input end of the second high-pressure pump is connected with a primary concentrated liquid outlet of the primary reverse osmosis membrane concentration device, and the output end of the second high-pressure pump is connected with the input end of the secondary reverse osmosis membrane concentration device;
the secondary reverse osmosis membrane concentration device is connected with the first purification system;
the first purification system comprises a wastewater CODcr removing device, a carbon and nitrogen removal reactor and a large-flux precision filter which are sequentially connected;
the large-flux precision filter is connected with the MVR evaporative crystallizer through a pipeline;
the NF membrane thick water port of the nanofiltration membrane group is connected with a second purification system;
the second purification system comprises a wastewater CODcr removing device and a large-flux precision filter which are sequentially connected;
the high-flux precision filter is connected with a second concentration system through a pipeline, the second concentration system comprises a third concentration unit and a fourth concentration unit, the third concentration unit comprises a third high-pressure pump and a third reverse osmosis membrane concentration device, and the fourth concentration unit comprises a fourth high-pressure pump and a fourth reverse osmosis membrane concentration device;
the high-flux precision filter is connected with the input end of a third high-pressure pump through a pipeline, and the output end of the third high-pressure pump is connected with the input end of a three-stage reverse osmosis membrane concentration device;
the output end of the third reverse osmosis membrane concentration device is connected with the input end of a fourth high-pressure pump through a pipeline, the output end of the fourth high-pressure pump is connected with the input end of a fourth-stage reverse osmosis membrane concentration device through a pipeline, the output end of the fourth-stage reverse osmosis membrane concentration device is connected with the input end of a shell-and-tube heat exchanger through a pipeline, the output end of the shell-and-tube heat exchanger is connected with a freezing crystallizer through a pipeline, the freezing crystallizer is connected with a melting crystallizer through a pipeline, and the freezing crystallizer and the melting crystallizer are further connected with a miscellaneous salt crystallizer through corresponding pipelines.
Preferably, the adjusting tank comprises a tank body and a stirrer arranged in the tank body, and the stirrer is a double-curved-surface stirrer.
Preferably, the sedimentation tank is a horizontal sedimentation tank, the clarification tank is a mechanical accelerated clarification tank, the filtering device adopts a tubular microfiltration membrane, and the filtrate filtered by the filtering device is subjected to ion exchange treatment by a resin softening device.
Preferably, the primary reverse osmosis membrane concentration device and the tertiary reverse osmosis membrane concentration device are micro-tubular reverse osmosis membrane modules MTRO, and the secondary reverse osmosis membrane concentration device and the quaternary reverse osmosis membrane concentration device are disc-tubular reverse osmosis membrane modules DTRO.
Preferably, the device for removing CODcr from wastewater comprises a device body, wherein a cover body is rotatably arranged on the upper part of the device body, a liquid inlet is fixedly arranged on the upper part of the cover body, the liquid inlet penetrates through the cover body to be communicated with the inner cavity of the device body, a filter plate is fixedly arranged on the upper part of the inner cavity of the device body, a rotating motor is fixedly arranged at the bottom of the device body, a stirring blade is rotatably arranged on the upper part of the rotating motor, a three-way valve is fixedly arranged on the upper part of the left side of the device body, the three-way valve penetrates through the side wall of the device body, an alkaline liquid bottle and an acid liquid bottle are fixedly arranged at one end of the three-way valve, which is positioned outside the device body, a heating block is fixedly arranged on the inner wall of the device body, a PH meter is fixedly arranged on the inner side of the heating block, a conduit is fixedly arranged on the inner wall of the right side of the device body, and a liquid quantitative meter is fixedly arranged at one end of the conduit, which is far away from the device body, the fixed drawing liquid pump that is provided with in liquid ration gauge lower part, drawing liquid pump left side is provided with the drawing liquid pipe, the fixed drawing liquid head that is provided with in drawing liquid pipe lower part, the fixed filter layer that is provided with in drawing liquid head lower part, and the fixed air chamber that is provided with in drawing liquid head outer lane, the fixed slider that is provided with of drawing liquid head side, slider and device body inner wall sliding connection.
Preferably, the carbon and nitrogen removal reactor consists of an outer cylinder and an inner cylinder which are coaxial, perforated partition plates are arranged in the middle parts of the outer cylinder and the inner cylinder to divide the outer cylinder and the inner cylinder into an upper chamber and a lower chamber, an aeration pipe is arranged above the perforated partition plate of the outer cylinder, a flow-off ball filler is distributed above the aeration pipe, and the flow-off ball filler is an aggregate of broken stones and PVC balls;
an ejector is arranged in the lower part of the outer barrel and is connected with a barrel wall below the outer barrel through a circulating pipeline and a circulating pump; biological fillers are arranged above the perforated clapboard of the inner cylinder, a plurality of water through holes are arranged at the upper end and the lower end of the wall of the inner cylinder and communicated with the outer cylinder,
preferably, the tube side of the shell-and-tube heat exchanger is concentrated water, the shell side is inlet water of frozen NF, the inlet temperature of the tube side is 20-25 ℃, and the outlet temperature of the tube side is 12-17 ℃; the shell side inlet temperature is 0-5 ℃, and the outlet temperature is 4-9 ℃.
Preferably, the MVR evaporative crystallizers are connected through a pipeline miscellaneous salt crystallizer.
Preferably, the magma port of the MVR evaporative crystallizer is further communicated with an inlet of a sodium chloride thickener, a magma outlet of the sodium chloride thickener is communicated with an inlet of a sodium chloride centrifuge, and a crystallized salt outlet of the sodium chloride centrifuge is communicated with an inlet of the sodium chloride drying bed.
Preferably, the magma outlet of the melt crystallizer is communicated with the inlet of the sodium sulfate thickener, the magma outlet of the sodium sulfate thickener is communicated with the inlet of the sodium sulfate centrifuge, and the crystallized salt outlet of the sodium sulfate centrifuge is communicated with the inlet of the sodium sulfate drying bed.
The utility model has the beneficial effects that:
1. the utility model can realize the regulation of the wastewater through the regulating tank, and can realize the sedimentation and clarification of the wastewater through the sedimentation tank and the clarification tank;
2. according to the utility model, the water produced by the NF membrane of the wastewater and the concentrated water produced by the NF membrane can be obtained through a salt separation system, wherein the water produced by the NF membrane mainly comprises sodium chloride, and then the sodium chloride is obtained through concentration treatment, purification treatment and evaporative crystallization; the NF membrane concentrated water sodium sulfate and sodium chloride are mainly used, and sodium sulfate crystal salt is obtained after purification, concentration, freezing crystallization and melting crystallization;
3. the mother liquor after the crystallization of the sodium chloride and the sodium sulfate is crystallized by a mixed salt crystallizer to obtain corresponding mixed salt.
Drawings
Fig. 1 is a structural frame diagram of the present invention.
FIG. 2 is a schematic structural view of a settling tank according to the present invention;
FIG. 3 is a schematic view of a wastewater CODcr removing apparatus according to the present invention;
FIG. 4 is a schematic structural view of a decarbonization and denitrification reactor of the present invention;
FIG. 5 is an enlarged view of the structure at A in FIG. 3 according to the present invention;
1-water inlet, 2-water outlet, 3-water inlet area, 4-sedimentation area, 5-advection area, 6-overflow area, 7-overflow groove and 8-water inlet;
11-device body, 12-liquid inlet, 13-filter plate, 14-rotating motor, 15-stirring blade, 16-three-way valve, 17-liquid pump, 18-liquid metering device, 19-alkaline liquid bottle, 20-acid liquid bottle, 21-PH meter, 22-liquid pumping tube, 23-slide block, 24-conduit, 25-liquid pumping head, 26-air chamber, 27-filtering layer;
31-outer cylinder, 32-inner cylinder, 33-aeration pipe, 34-flow ball filler, 35-ejector, 36-biological filler, 37-water hole, 38-circulating pump, and 39-perforated partition board.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, the embodiment provides a high-salt-content waste water salt-separating crystallization system, which includes a waste water adjusting tank, a sedimentation tank, a clarification tank, a filtering device, a salt-separating system, a first concentration system, a second concentration system, a first purification system, a second purification system, an MVR evaporative crystallizer, a freezing crystallizer, a melt crystallizer, and a miscellaneous salt crystallizer.
The waste water equalizing basin pass through the pipeline and be connected with former pond, carry sewage to the waste water equalizing basin through former pond and carry out the sewage regulation, the equalizing basin includes the cell body and sets up the waste water riser in the cell body, the waste water riser on be provided with the waste water elevator pump. The cell body in still be provided with water quality monitoring device and agitator, the agitator adopt the hyperboloid agitator to stir the medicine that adds the waste water equalizing basin through the agitator, for example be used for stirring the medicine of adjusting sewage pH value.
Preferably, the wastewater adjusting tank is communicated with the sedimentation tank through a wastewater lifting pipe, the sedimentation tank is a horizontal flow sedimentation tank, as shown in fig. 2, a water inlet 1 and a water outlet 2 are respectively arranged on two sides of the horizontal flow sedimentation tank, the tank body is internally divided into a water inlet area 3, a sedimentation area 4 and a horizontal flow area 5, wherein the water inlet area 4 is positioned in the tank body at one end of the water inlet 1 and is separated from the sedimentation area 4 on the lower side of the water inlet area and the horizontal flow area 5 on the side of the water inlet area by a partition plate, a water inlet hole 8 communicated with the sedimentation area 4 on the lower side of the water inlet area 3 is arranged on the partition plate at the bottom of the water inlet area 3, the water inlet area 3 and the sedimentation area 4 are positioned on the same side of the horizontal flow area 5, and a sludge discharge hole is arranged on the side wall of the sedimentation area 4. An overflow area 6 is arranged on the upper side of the advection area 5, an overflow groove 7 communicated with the water outlet 2 is arranged in the overflow area 6, when in use, a coagulant and a coagulant aid are uninterruptedly added in the water inlet area 3, heavy metal wastewater added with the coagulant and the coagulant aid falls into the sedimentation area 4 through a water inlet 8 under the action of gravity, during the descending process, the sediment in the wastewater continuously falls into the bottom end and is discharged through a sludge discharge hole, water flow continuously circulates and flows between the sedimentation area 4 and the advection area 5, the water in the advection area 5 is from clear to turbid from top to bottom, the turbid liquid continuously circulates to the sedimentation area 4 for sedimentation, and the supernatant liquid continuously overflows to the water outlet 2 from a weir port of the overflow groove 7 in the overflow area 6.
Preferably, the clarification tank is communicated with a water outlet of the sedimentation tank, the clarification tank is a mechanical accelerated clarification tank, the clarification tank is further connected with the filtering device, in the embodiment, the filtering device adopts a tubular microfiltration membrane, the tubular microfiltration membrane is further connected with a resin softening device, and in the embodiment, the resin softening device is a chelating resin bed.
Preferably, the salt separation system comprises a booster pump, a filter, a salt separation high-pressure pump, an intersegmental booster pump and a nanofiltration membrane group, the resin softening device is connected with the booster pump through a pipeline, the booster pump is connected with the filter through a pipeline, the booster pump is connected with the nanofiltration membrane group through the salt separation high-pressure pump and the intersegmental booster pump, and an NF membrane water production port of the nanofiltration membrane group is connected with the first concentration system; and the NF membrane concentrated water port of the nanofiltration membrane group is connected with a second purification system.
Preferably, the first concentration system comprises a primary concentration unit and a secondary concentration unit, the primary concentration unit comprises a first high-pressure pump and a primary reverse osmosis membrane concentration device, the secondary concentration unit comprises a second high-pressure pump and a secondary reverse osmosis membrane concentration device, the input end of the first high-pressure pump is connected with the NF membrane water production port, the output end of the first high-pressure pump is connected with the input end of the primary reverse osmosis membrane concentration device, the input end of the second high-pressure pump is connected with the primary concentrated liquid outlet of the primary reverse osmosis membrane concentration device, and the output end of the second high-pressure pump is connected with the input end of the secondary reverse osmosis membrane concentration device; the second-stage reverse osmosis membrane concentration device is connected with a first purification system, the first purification system is connected with an MVR evaporative crystallizer, a crystal slurry port of the MVR evaporative crystallizer is communicated with an inlet of a sodium chloride thickener, a crystal slurry outlet of the sodium chloride thickener is communicated with an inlet of a sodium chloride centrifugal machine, and a crystallized salt outlet of the sodium chloride centrifugal machine is communicated with an inlet of a sodium chloride drying bed. In this embodiment, the MVR evaporative crystallizer is connected by a pipe miscellaneous salt crystallizer.
Preferably, in this embodiment, the first purification system comprises a wastewater CODcr removing device, a carbon and nitrogen removal reactor, and a large flux connected in sequenceAnd the high-flux precision filter is connected with the MVR evaporative crystallizer through a pipeline. Wherein, referring to fig. 3, the device for removing CODcr from waste water comprises a device body 11, an inner cavity is provided in the device body 11, a cover is rotatably provided on the device body at the upper end of the inner cavity, a liquid inlet 12 is fixedly provided on the upper portion of the cover, the liquid inlet 12 penetrates through the cover to communicate with the inner cavity of the device body 11, a filter plate 13 is fixedly provided on the upper portion of the inner cavity of the device body 11, a rotating motor 14 is fixedly provided at the bottom of the device body 11, a stirring blade 15 is rotatably provided on the upper portion of the rotating motor 14, a three-way valve 16 is fixedly provided on the upper portion of the left side of the device body 11, the three-way valve 16 penetrates through the side wall of the device body 11, an alkali solution bottle 19 and an acid solution bottle 20 are fixedly provided at one end of the three-way valve 16 outside the device body 11, a heating block is fixedly provided on the inner wall of the device body 11, a PH meter 21 is fixedly provided on the inner side of the heating block, the fixed pipe 24 that is provided with of device body 11 right side inner wall, the fixed liquid quantitative meter 18 that is provided with of one end that device body 11 was kept away from to pipe 24, the fixed drawing liquid pump 17 that is provided with in liquid quantitative meter 18 lower part, drawing liquid pump 17 left side is provided with drawing liquid pipe 22, the fixed drawing liquid head 25 that is provided with in drawing liquid pipe 22 lower part, the fixed filter layer 27 that is provided with in drawing liquid head 25 lower part, and the fixed air chamber 26 that is provided with in drawing liquid head 25 outer lane, the fixed slider 23 that is provided with of drawing liquid head 25 side, slider 23 and device body 11 inner wall sliding connection refer to fig. 5. When using, inside sewage from inlet 12 inner chamber, filter 13 filters great impurity, drives stirring leaf 15 through rotating motor 14 and rotates for sewage is in by the stirring state, opens the heating piece, and PH meter 21 measures the pH value of sewage, according to the height of pH value, decides to open tee bend 16 valve release acidizing fluid or alkali lye, in order to reach suitable pH value, according to the content of the various elements of sewage, adjusts liquid ration meter 18, adds appropriate amount H2O2So that the whole mixed solution forms a Fenton-like oxidation atmosphere; when the CODcr value in the mixed system reaches the discharge standard, the liquid pump 17 is opened to discharge the treated sewage.
Preferably, as shown in FIG. 4, theThe carbon and nitrogen removal reactor consists of an outer cylinder 31 and an inner cylinder 32 which are coaxial, perforated clapboards 39 are arranged at the middle parts of the outer cylinder 31 and the inner cylinder 32 to divide the outer cylinder 31 and the inner cylinder 32 into an upper chamber and a lower chamber, an aeration pipe 33 is arranged above the perforated clapboard 39 of the outer cylinder 31, a flow-off ball filler 34 is distributed above the aeration pipe 33, and the flow-off ball filler 34 is an aggregate of crushed stones and PVC balls; an ejector 35 is arranged in the lower part of the outer cylinder 31 and is connected with the cylinder wall below the outer cylinder 31 through a circulating pipeline and a circulating pump 38; the biological filler 36 is arranged above the perforated clapboard 39 of the inner cylinder 32, and the upper end and the lower end of the cylinder wall of the inner cylinder 32 are both provided with a plurality of water through holes 37 which are communicated with the outer cylinder 31. When in use, DO (dissolved oxygen) in the inner cylinder 32 is controlled to be less than 0.2mg/L, DO in the outer cylinder 31 is controlled to be about 1.5mg/L, and DO control is performed by adjusting the amount of circulating water and the amount of aeration in the outer cylinder 31. Wastewater to be treated enters water from the upper part of the inner cylinder 32 of the reactor, flows downwards, passes through the biological filler 36 of the inner cylinder 32, and NO shunted by the outer cylinder 31 under the anoxic condition (DO is controlled to be less than 0.2mg/L)3 -Denitrifying to remove nitrogen, and the denitrification process can directly utilize organic carbon in the wastewater, so that an external carbon source is saved. The wastewater flows to the bottom of the inner cylinder 32, flows 37 to the outer cylinder 1 through the rectangular through holes at the bottom, flows upwards, enters the flow separation ball packing 34, and is subjected to nitration reaction, and organic carbon in the wastewater is further removed.
Preferably, the second purification system comprises a wastewater CODcr removing device and a large-flux precision filter which are connected in sequence; the high-flux precision filter is connected with a second concentration system through a pipeline, the second concentration system comprises a third concentration unit and a fourth concentration unit, the third concentration unit comprises a third high-pressure pump and a third reverse osmosis membrane concentration device, and the fourth concentration unit comprises a fourth high-pressure pump and a fourth reverse osmosis membrane concentration device; the high-flux precision filter is connected with the input end of a third high-pressure pump through a pipeline, and the output end of the third high-pressure pump is connected with the input end of a three-stage reverse osmosis membrane concentration device; the output end of the third reverse osmosis membrane concentration device is connected with the input end of a fourth high-pressure pump through a pipeline, the output end of the fourth high-pressure pump is connected with the input end of a fourth-stage reverse osmosis membrane concentration device through a pipeline, the output end of the fourth-stage reverse osmosis membrane concentration device is connected with the input end of a shell-and-tube heat exchanger through a pipeline, the output end of the shell-and-tube heat exchanger is connected with a freezing crystallizer through a pipeline, the freezing crystallizer is connected with a melting crystallizer through a pipeline, and the freezing crystallizer and the melting crystallizer are further connected with a miscellaneous salt crystallizer through corresponding pipelines.
Preferably, the primary reverse osmosis membrane concentration device and the tertiary reverse osmosis membrane concentration device are micro-tubular reverse osmosis membrane modules MTRO, and the secondary reverse osmosis membrane concentration device and the quaternary reverse osmosis membrane concentration device are disc-tubular reverse osmosis membrane modules DTRO.
Preferably, the tube side of the shell-and-tube heat exchanger is concentrated water, the shell side is inlet water of frozen NF, the inlet temperature of the tube side is 20-25 ℃, and the outlet temperature of the tube side is 12-17 ℃; the shell side inlet temperature is 0-5 ℃, and the outlet temperature is 4-9 ℃.
Preferably, the magma outlet of the melt crystallizer is communicated with the inlet of the sodium sulfate thickener, the magma outlet of the sodium sulfate thickener is communicated with the inlet of the sodium sulfate centrifuge, and the crystallized salt outlet of the sodium sulfate centrifuge is communicated with the inlet of the sodium sulfate drying bed.
The foregoing embodiments and description have been presented only to illustrate the principles and preferred embodiments of the utility model, and various changes and modifications may be made therein without departing from the spirit and scope of the utility model as hereinafter claimed.
Claims (10)
1. The high-salt-content waste water salt separation crystallization system is characterized by comprising a waste water adjusting tank, a sedimentation tank, a clarification tank, a filtering device, a salt separation system, a first concentration system, a second concentration system, a first purification system, a second purification system, an MVR evaporative crystallizer, a freezing crystallizer, a melting crystallizer and a mixed salt crystallizer;
the wastewater adjusting tank is connected with the sedimentation tank through a pipeline, the sedimentation tank is connected with the clarification tank through a pipeline, the clarification tank is connected with the filtering device through a pipeline, and the filtering device is connected with the resin softening device through a pipeline;
the salt separation system comprises a booster pump, a security filter, a salt separation high-pressure pump, an intersegmental booster pump and a nanofiltration membrane group which are sequentially connected, wherein the booster pump is connected with a resin softening device through a pipeline, the booster pump is connected with the security filter through a pipeline, the security filter is connected with the nanofiltration membrane group through the salt separation high-pressure pump and the intersegmental booster pump, and an NF membrane water production port of the nanofiltration membrane group is connected with a first concentration system; the NF membrane thick water port of the nanofiltration membrane group is connected with a second purification system;
the first concentration system comprises a primary concentration unit and a secondary concentration unit, the primary concentration unit comprises a first high-pressure pump and a primary reverse osmosis membrane concentration device, the secondary concentration unit comprises a second high-pressure pump and a secondary reverse osmosis membrane concentration device, the input end of the first high-pressure pump is connected with a NF membrane water production port, the output end of the first high-pressure pump is connected with the input end of the primary reverse osmosis membrane concentration device, the input end of the second high-pressure pump is connected with a primary concentrated liquid outlet of the primary reverse osmosis membrane concentration device, and the output end of the second high-pressure pump is connected with the input end of the secondary reverse osmosis membrane concentration device; the secondary reverse osmosis membrane concentration device is connected with the first purification system;
the first purification system comprises a wastewater CODcr removing device, a carbon and nitrogen removal reactor and a large-flux precision filter which are sequentially connected; the large-flux precision filter is connected with the MVR evaporative crystallizer through a pipeline;
the second purification system comprises a wastewater CODcr removing device and a large-flux precision filter which are sequentially connected; the high-flux precision filter is connected with a second concentration system through a pipeline, the second concentration system comprises a third concentration unit and a fourth concentration unit, the third concentration unit comprises a third high-pressure pump and a third reverse osmosis membrane concentration device, and the fourth concentration unit comprises a fourth high-pressure pump and a fourth reverse osmosis membrane concentration device; the high-flux precision filter is connected with the input end of a third high-pressure pump through a pipeline, and the output end of the third high-pressure pump is connected with the input end of a three-stage reverse osmosis membrane concentration device;
the output end of the third reverse osmosis membrane concentration device is connected with the input end of a fourth high-pressure pump through a pipeline, the output end of the fourth high-pressure pump is connected with the input end of a fourth-stage reverse osmosis membrane concentration device through a pipeline, the output end of the fourth-stage reverse osmosis membrane concentration device is connected with the input end of a shell-and-tube heat exchanger through a pipeline, the output end of the shell-and-tube heat exchanger is connected with a freezing crystallizer through a pipeline, the freezing crystallizer is connected with a melting crystallizer through a pipeline, and the freezing crystallizer and the melting crystallizer are further connected with a miscellaneous salt crystallizer through corresponding pipelines.
2. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the wastewater adjusting tank comprises a tank body and a wastewater lifting pipe arranged in the tank body, a wastewater lifting pump is arranged on the wastewater lifting pipe, and the wastewater adjusting tank is communicated with the sedimentation tank through the wastewater lifting pipe;
the waste water adjusting tank is characterized in that a water quality monitoring device and a stirrer are further arranged in the tank body of the waste water adjusting tank, and the stirrer is a hyperboloid stirrer.
3. The high-salinity waste water salinity crystallization system according to claim 2, characterized in that: the sedimentation tank is a horizontal flow sedimentation tank, a water inlet and a water outlet are respectively arranged on two sides of the horizontal flow sedimentation tank, and the inside of the tank body is divided into a water inlet area, a sedimentation area and a horizontal flow area;
the water inlet area is positioned in the tank body at one end of the water inlet and is separated from the sedimentation area at the lower side of the water inlet area and the horizontal flow area at the side of the water inlet area by a partition plate, a water inlet hole communicated with the sedimentation area at the lower side of the water inlet area is formed in the partition plate at the bottom of the water inlet area, the water inlet area and the sedimentation area are positioned at the same side of the horizontal flow area, and a sludge discharge hole is formed in the side wall of the sedimentation area;
an overflow area is arranged on the upper side of the advection area, and an overflow groove communicated with the water outlet is arranged in the overflow area.
4. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the clarification tank is a mechanical accelerated clarification tank;
the filtering device adopts a tubular microfiltration membrane, the tubular microfiltration membrane is also connected with a resin softening device, and the resin softening device is a chelating resin bed.
5. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the crystal slurry port of the MVR evaporation crystallizer is also communicated with the inlet of a sodium chloride thickener, the crystal slurry outlet of the sodium chloride thickener is communicated with the inlet of a sodium chloride centrifugal machine, and the crystallized salt outlet of the sodium chloride centrifugal machine is communicated with the inlet of a sodium chloride drying bed;
the MVR evaporation crystallizer is connected with the mixed salt crystallizer through a pipeline.
6. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the device for removing CODcr of waste water comprises a device body, wherein an inner cavity is arranged in the device body, a cover body is rotatably arranged on the device body at the upper end of the inner cavity, a liquid inlet is fixedly arranged at the upper part of the cover body, the liquid inlet penetrates through the cover body to be communicated with the inner cavity of the device body, a filter plate is fixedly arranged at the upper part of the inner cavity of the device body, a rotating motor is fixedly arranged at the bottom of the device body, a stirring blade is rotatably arranged at the upper part of the rotating motor, a three-way valve is fixedly arranged at the upper part of the left side of the device body, the three-way valve penetrates through the side wall of the device body, an alkali liquor bottle and an acid liquor bottle are fixedly arranged at one end of the three-way valve, which is positioned outside the device body, a heating block is fixedly arranged on the inner wall of the device body, a PH meter is fixedly arranged at the inner side of the heating block, a conduit is fixedly arranged on the inner wall of the right side of the device body, and a liquid quantitative meter is fixedly arranged at one end of the conduit, which is far away from the device body, the fixed drawing liquid pump that is provided with in liquid ration gauge lower part, drawing liquid pump left side is provided with the drawing liquid pipe, the fixed drawing liquid head that is provided with in drawing liquid pipe lower part, the fixed filter layer that is provided with in drawing liquid head lower part, and the fixed air chamber that is provided with in drawing liquid head outer lane, the fixed slider that is provided with of drawing liquid head side, slider and device body inner wall sliding connection.
7. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the carbon and nitrogen removal reactor consists of an outer cylinder and an inner cylinder which are coaxial, perforated partition plates are arranged in the middle parts of the outer cylinder and the inner cylinder to divide the outer cylinder and the inner cylinder into an upper chamber and a lower chamber, an aerator pipe is arranged above the perforated partition plates of the outer cylinder, flow-off ball fillers are distributed above the aerator pipe, an ejector is arranged in the lower part of the outer cylinder, and the ejector is connected with a cylinder wall below the outer cylinder through a circulating pipeline and a circulating pump; the biological filler is arranged above the perforated partition plate of the inner barrel, and the upper end and the lower end of the wall of the inner barrel are both provided with a plurality of water through holes communicated with the outer barrel.
8. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the primary reverse osmosis membrane concentration device and the tertiary reverse osmosis membrane concentration device are microtube type reverse osmosis membrane modules MTRO, and the secondary reverse osmosis membrane concentration device and the quaternary reverse osmosis membrane concentration device are disc tube type reverse osmosis membrane modules DTRO.
9. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: the tube pass of the shell-and-tube heat exchanger is concentrated water, the shell pass is inlet water of frozen NF, the inlet temperature of the tube pass is 20-25 ℃, and the outlet temperature of the tube pass is 12-17 ℃; the shell side inlet temperature is 0-5 ℃, and the outlet temperature is 4-9 ℃.
10. The high-salinity waste water salinity crystallization system according to claim 1, characterized in that: and a crystal slurry outlet of the melt crystallizer is communicated with an inlet of a sodium sulfate thickener, a crystal slurry outlet of the sodium sulfate thickener is communicated with an inlet of a sodium sulfate centrifuge, and a crystallized salt outlet of the sodium sulfate centrifuge is communicated with an inlet of a sodium sulfate drying bed.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202120564953.6U CN215975369U (en) | 2021-03-19 | 2021-03-19 | High salt waste water salt separation crystallization system that contains |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120564953.6U CN215975369U (en) | 2021-03-19 | 2021-03-19 | High salt waste water salt separation crystallization system that contains |
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| CN215975369U true CN215975369U (en) | 2022-03-08 |
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