CN110665249A - MVR high-salinity wastewater crystallization and salt discharge system and process method thereof - Google Patents
MVR high-salinity wastewater crystallization and salt discharge system and process method thereof Download PDFInfo
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- CN110665249A CN110665249A CN201911018922.4A CN201911018922A CN110665249A CN 110665249 A CN110665249 A CN 110665249A CN 201911018922 A CN201911018922 A CN 201911018922A CN 110665249 A CN110665249 A CN 110665249A
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- 150000003839 salts Chemical class 0.000 title claims abstract description 105
- 238000000034 method Methods 0.000 title claims abstract description 56
- 238000002425 crystallisation Methods 0.000 title claims abstract description 52
- 230000008025 crystallization Effects 0.000 title claims abstract description 52
- 239000002351 wastewater Substances 0.000 title claims abstract description 47
- 239000013078 crystal Substances 0.000 claims abstract description 40
- 238000007599 discharging Methods 0.000 claims abstract description 35
- 239000002002 slurry Substances 0.000 claims abstract description 31
- 239000000463 material Substances 0.000 claims abstract description 23
- 239000002893 slag Substances 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims description 41
- 239000012266 salt solution Substances 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 8
- 239000012452 mother liquor Substances 0.000 claims description 7
- 230000005540 biological transmission Effects 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000004140 cleaning Methods 0.000 description 3
- 239000002562 thickening agent Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 235000002639 sodium chloride Nutrition 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0031—Evaporation of components of the mixture to be separated by heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
- B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04B—CENTRIFUGES
- B04B11/00—Feeding, charging, or discharging bowls
- B04B11/02—Continuous feeding or discharging; Control arrangements therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Centrifugal Separators (AREA)
Abstract
The invention discloses an MVR high-salt wastewater crystallization and salt discharge system and a process method thereof, belonging to the technical field of evaporative crystallization systems and comprising the following steps: an MVR evaporator; an inlet of the crystallizer is connected with an outlet of the MVR evaporator; an inlet of the crystal slurry pump is connected with a first outlet of the crystallizer, and an outlet of the crystal slurry pump is connected with an inlet of the MVR evaporator; the inlet of the cantilever type spiral discharging centrifuge is connected with the second outlet of the crystallizer; and the fluidized bed dryer is connected with a slag outlet of the cantilever type spiral discharging centrifuge. The invention solves the problems of longer process chain of the crystallization centrifugal section and great influence of material concentration fluctuation on the salt production process and quality.
Description
Technical Field
The invention relates to the technical field of evaporative crystallization systems, in particular to an MVR high-salt wastewater crystallization and salt discharge system and a process method thereof.
Background
In the high-salt wastewater treatment industry, evaporation crystallization and salt discharge systems are often used for obtaining high-purity anhydrous sodium sulfate, sodium chloride, potassium sulfate, ammonium chloride and other products. Traditional MVR crystallization, play salt system need carry out multistage concentration with the high salt waste water that contains salt rate 3%, make its concentration reach more than 30%, just can get into doublestage piston centrifuge and filter classification, realize out salt (moisture content > 5%), its main equipment contains: MVR evaporator, crystallizer, crystal slurry pump, swirler, thickener, centrifuge (three-foot or two-stage piston type), drier, vibrating screen, pulverizer, packer, etc.
So far, the traditional MVR crystallization and salt-yielding system technology is mature and widely applied, but the defects are continuously exposed: the process chain is long, the equipment failure rate is high, the operation energy consumption is high, the automation level is low, and the dead bed of the drying machine tool is caused by the dilution of the two-stage piston centrifuge. The basic reason is that the double-stage piston centrifuge has strict requirements on material concentration (more than or equal to 30%) and relatively high requirements on material granularity stability in the application of the system.
Disclosure of Invention
Aiming at the problems of longer process chain, high equipment failure rate, high operation energy consumption, low automation level, dead bed of a drying machine tool caused by dilution of a two-stage piston centrifuge and the like of the conventional evaporative crystallization system, the MVR high-salt wastewater crystallization and salt discharge system and the process method thereof are provided, and the problems of longer process chain at the crystallization and centrifugation section and great influence of material concentration fluctuation on the salt discharge process and quality are solved.
The specific technical scheme is as follows:
a MVR (mechanical vapor recompression) high-salt wastewater crystallization and salt discharge system comprises:
an MVR evaporator;
an inlet of the crystallizer is connected with an outlet of the MVR evaporator;
an inlet of the crystal slurry pump is connected with a first outlet of the crystallizer, and an outlet of the crystal slurry pump is connected with an inlet of the MVR evaporator;
the inlet of the cantilever type spiral discharging centrifuge is connected with the second outlet of the crystallizer;
and the fluidized bed dryer is connected with a slag outlet of the cantilever type spiral discharging centrifuge.
The high salt waste water crystallization of above-mentioned MVR, play salt system wherein, still includes: and the mother liquor tank is connected with the liquid outlet of the cantilever type spiral discharging centrifuge.
The high salt waste water crystallization of above-mentioned MVR, play salt system wherein, still includes: the inlet of the flashboard reversing valve is connected with the slag outlet of the cantilever type spiral discharging centrifuge, the inlet of the fluidized bed dryer is connected with the first outlet of the flashboard reversing valve, and the mother liquor tank is connected with the second outlet of the flashboard reversing valve.
The high salt waste water crystallization of above-mentioned MVR, play salt system, wherein, cantilever type spiral discharge centrifuge includes:
a housing;
the motor group is arranged at one end outside the shell;
one end of the differential is in transmission connection with the motor set, and the other end of the differential extends into one end of the shell;
the rotary drum is arranged in the shell, the rotary drum is arranged at the other end of the differential mechanism, and one end of the rotary drum, which is far away from the differential mechanism, forms a screen;
the spiral discharger is arranged in the shell, is arranged at the other end of the differential mechanism and is positioned in the rotary drum;
the distributing cone is arranged in the shell, is arranged at the end part of the other end of the differential mechanism and is positioned in the spiral discharger;
the inlet pipe, install in of inlet pipe the other end of casing, the one end of inlet pipe stretches into in the screw discharger, and with the cloth awl is just right mutually.
The high salt waste water crystallization of foretell MVR, play salt system, wherein, cantilever type spiral discharge centrifuge still includes:
the rotating drum bottom is arranged at the other end of the differential mechanism, one end of the rotating drum is fixedly connected with the periphery of one end of the rotating drum bottom, and a plurality of through holes are formed in the rotating drum bottom and are arranged at equal intervals along the circumferential direction of the rotating drum bottom;
and the liquid adjusting devices are arranged at the other end of the rotary drum bottom and are respectively positioned between the through holes and the periphery of the rotary drum bottom.
The MVR high-salt wastewater crystallization and salt discharge system is characterized in that a stirrer is arranged at the bottom of the crystallizer.
Foretell MVR high salt waste water crystallization, salt system, wherein, cantilever type spiral discharge centrifuge's slag notch with cantilever type spiral discharge centrifuge's liquid outlet all locates the bottom of casing, the other end of inlet pipe does cantilever type spiral discharge centrifuge's entry, be equipped with air inlet and gas outlet on the casing.
The above MVR high-salt wastewater crystallization and salt discharge system, wherein the first outlet of the crystallizer is located on the sidewall of the crystallizer, and the second outlet of the crystallizer is located at the bottom of the crystallizer.
The MVR high-salt wastewater crystallization and salt discharge system is characterized in that a first outlet of the flashboard reversing valve is located at the bottom of the flashboard reversing valve, and a second outlet of the flashboard reversing valve is located on the side wall of the flashboard reversing valve.
A process method of an MVR high-salt wastewater crystallization and salt discharge system comprises any one of the above systems, and the process method comprises the following steps:
step S1: high-temperature steam enters a shell pass of the MVR evaporator and heats a salt solution in a tube pass of the MVR evaporator;
step S2: the salt solution rises from the bottom of the MVR evaporator to the top of the MVR evaporator under the action of the crystal slurry pump;
step S3: the salt solution is evaporated during the rising process, the concentration of the salt solution is continuously increased, a crystal slurry containing crystal salt with a first concentration is formed, the crystal slurry enters the crystallizer to continue to grow, and simultaneously, the step S4 and the step S5 are executed;
step S4: in the crystallizer, the small-grained crystallized salt located in the upper layer of the crystallizer is pumped into the tube pass of the MVR evaporator again from the MVR evaporator by the magma pump, and the process returns to step S2:
step S5: in the crystallizer, the large-particle crystallized salt in the crystallizer reaches a second concentration by gravity in the crystal salt in the crystal slurry settled and collected at the bottom layer of the crystallizer, and flows into the cantilever-type spiral discharge centrifuge to perform step S6;
step S6: the crystal slurry containing crystal salt with a second concentration enters the shell from the other end of the feeding pipe and is sprayed to the surface of the material distribution cone from one end of the feeding pipe, at the moment, the motor group drives the rotary drum, the spiral discharger and the material distribution cone to rotate at a high speed through the differential mechanism, the crystal slurry is thrown to the inner wall of the rotary drum by utilizing centrifugal force generated by high-speed rotation, and a material layer is formed according to the density;
step S7: after the material layer reaches a certain thickness, the material layer is scraped off by the spiral discharger and pushed to the screen mesh for filtering, the material layer is separated into wet salt and clear liquid, and the clear liquid with lower density is extruded to one end of the rotary drum to realize solid-liquid separation;
step S8: discharging the wet salt from a slag outlet of the cantilever type spiral discharge centrifuge, discharging the clear liquid from a liquid outlet of the cantilever type spiral discharge centrifuge, and executing the step S9 or the step S10;
step S9: the wet salt separated by the cantilever type spiral discharging centrifuge falls into the fluidized bed dryer through the flashboard reversing valve for drying to obtain finished salt, and the process is finished;
step S10: and returning the clear liquid separated by the cantilever type spiral discharging centrifuge into the mother liquid tank, and finishing.
In the above process method of the MVR high-salt wastewater crystallization and salt discharge system, in step S5, the crystal slurry containing the crystal salt with the second concentration flows into the cantilever-type spiral discharge centrifuge under the slow action of the stirrer.
The technical method of the MVR high-salt wastewater crystallization and salt discharge system is characterized in that the second concentration is 20%.
The above process method of the MVR high-salt wastewater crystallization and salt discharge system, wherein the first concentration is 10%.
In step S7, the moisture content of the wet salt is adjusted by the liquid conditioner.
The process method of the MVR high-salt wastewater crystallization and salt discharge system is characterized in that the moisture content of the wet salt is controlled within 3%.
Compared with the prior art, the technical scheme has the positive effects that:
(1) the cantilever type spiral discharging centrifuge provided by the invention is used for crystallizing the MVR high-salt wastewater and discharging salt from the salt system, the salt is not required to be further concentrated by a cyclone and a thickener, and the salt directly enters the cantilever type spiral discharging centrifuge to obtain wet salt with the water content of 2% -3%, so that the scale of a fluidized bed dryer is effectively reduced, and the use power consumption is reduced;
(2) the invention cancels a plurality of devices, so that the process chain is shorter and more stable, the maintenance cost, the operation cost and the management cost of the devices can be reduced, the arrangement of the devices can be optimized, and the floor area of a factory building can be reduced;
(3) the fluidized bed dryer has the advantages of reducing the specification, reducing the required power consumption and steam consumption, and solving the problem of dead bed of the fluidized bed dryer.
Drawings
FIG. 1 is a schematic diagram of the overall structure of an MVR high-salinity wastewater crystallization and salt discharge system and a process method thereof according to the present invention;
FIG. 2 is a schematic structural diagram of a cantilever type spiral discharge centrifuge in the MVR high-salt wastewater crystallization and salt discharge system and the process method thereof;
in the drawings: 1. an MVR evaporator; 2. a crystallizer; 3. a cantilever type spiral discharge centrifuge; 4. a fluidized bed dryer; 5. a mother liquor tank; 6. a crystal slurry pump; 7. a flashboard reversing valve; 31. a housing; 32. a motor unit; 33. a differential mechanism; 34. a drum; 35. a screw discharger; 36. a material distributing cone; 37. a feed pipe; 38. screening a screen; 39. rotating the drum bottom; 40. a through hole; 41. a liquid mixing device; 42. an air inlet; 43. an air outlet; 44. mechanical sealing; 45. a slag outlet; 46. a liquid outlet; 47. and a baffle plate.
Detailed Description
The invention is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
Fig. 1 is a schematic view of an overall structure of an MVR high-salt wastewater crystallization and salt discharge system and a process method thereof according to the present invention, fig. 2 is a schematic view of a cantilever-type spiral discharge centrifuge in an MVR high-salt wastewater crystallization and salt discharge system and a process method thereof according to the present invention, and as shown in fig. 1 and fig. 2, a preferred embodiment of an MVR high-salt wastewater crystallization and salt discharge system is shown, including: MVR evaporimeter 1, crystallizer 2, magma pump 6, cantilever type spiral discharge centrifuge 3 and fluidized bed drying machine 4, the entry of crystallizer 2 is connected with MVR evaporimeter 1's export, the entry of magma pump 6 is connected with the first export of crystallizer 2, the export of magma pump 6 is connected with MVR evaporimeter 1's entry, cantilever type spiral discharge centrifuge 3's entry is connected with the second export of crystallizer 2, fluidized bed drying machine 4 is connected with cantilever type spiral discharge centrifuge 3's slag notch.
Further, as a preferred embodiment, the MVR high-salt wastewater crystallization and salt discharge system further includes: and the mother liquor tank 5 is connected with the liquid outlet of the cantilever type spiral discharging centrifuge 3.
Further, as a preferred embodiment, the MVR high-salt wastewater crystallization and salt discharge system further includes: the inlet of the flashboard reversing valve 7 is connected with the slag outlet of the cantilever type spiral discharging centrifuge 3, the inlet of the fluidized bed dryer 4 is connected with the first outlet of the flashboard reversing valve 7, and the mother liquor tank 5 is connected with the second outlet of the flashboard reversing valve 7.
Further, as a preferred embodiment, the cantilever-type screw discharge centrifuge comprises: a machine shell 31, a motor group 32 and a differential gear 33, the device comprises a rotary drum 34, an auger discharger 35, a distributing cone 36 and a feeding pipe 37, wherein the motor group 32 is arranged at one end outside the machine shell 31, one end of the differential 33 is in transmission connection with the motor group 32, the other end of the differential 33 extends into one end of the machine shell 31, the rotary drum 34 is arranged in the machine shell 31, the rotary drum 34 is arranged at the other end of the differential 33, one end, far away from the differential 33, of the rotary drum 34 forms a screen 38, the auger discharger 35 is arranged in the machine shell 31, the auger discharger 35 is arranged at the other end of the differential 33, the auger discharger 35 is positioned in the rotary drum 34, the distributing cone 36 is arranged in the machine shell 31, the distributing cone 36 is arranged at the end part of the other end of the differential 33, the distributing cone 36 is positioned in the auger discharger 35, the feeding pipe 37 is arranged at the other end of the machine shell 31. Preferably, the electric machine set 32 comprises a main motor and an auxiliary motor, and the main motor and the auxiliary motor drive the rotary drum 34, the spiral discharger 35 and the distributing cone 36 to rotate at a high speed through a differential 33 connected with the main motor and the auxiliary motor.
Further, as a preferred embodiment, the cantilever-type screw discharge centrifuge further comprises: the rotating drum bottom 39 is arranged at the other end of the differential mechanism 33, one end of the rotating drum 34 is fixedly connected with the periphery of one end of the rotating drum bottom 39, a plurality of through holes 40 are formed in the rotating drum bottom 39, and the through holes 40 are arranged at equal intervals along the circumferential direction of the rotating drum 34 bottom.
Further, as a preferred embodiment, the cantilever-type screw discharge centrifuge further comprises: a plurality of liquid adjusting devices 41, wherein the liquid adjusting devices 41 are all arranged at the other end of the rotary drum bottom 39, and the liquid adjusting devices 41 are respectively arranged between the through holes 40 and the periphery of the rotary drum bottom 39.
Further, as a preferred embodiment, the bottom of the crystallizer 2 is provided with a stirrer.
The above are merely preferred embodiments of the present invention, and the embodiments and the protection scope of the present invention are not limited thereby.
The present invention also has the following embodiments in addition to the above:
in a further embodiment of the present invention, please refer to fig. 1 and fig. 2, a slag outlet 45 of the cantilever-type screw discharge centrifuge 3 and a liquid outlet 46 of the cantilever-type screw discharge centrifuge 3 are both disposed at the bottom of the casing 31, the other end of the feeding pipe 37 is an inlet of the cantilever-type screw discharge centrifuge 3, and the casing 31 is provided with an air inlet 42 and an air outlet 43.
In a further embodiment of the invention, the first outlet of the crystallizer 2 is located in the side wall of the crystallizer 2 and the second outlet of the crystallizer 2 is located in the bottom of the crystallizer 2.
In a further embodiment of the invention the first outlet of the flashboard reversing valve 7 is located at the bottom of the flashboard reversing valve 7 and the second outlet of the flashboard reversing valve 7 is located at the side wall of the flashboard reversing valve 7.
In a further embodiment of the present invention, the cantilevered spiral discharge centrifuge further comprises: and a mechanical seal 44, wherein the mechanical seal 44 is provided between the inner periphery of the drum bottom 39 and the other end of the differential 33.
In a further embodiment of the present invention, one end of the drum 34 has a larger diameter than the other end of the drum 34.
In a further embodiment of the present invention, the bottom of the casing 31 is disposed between the slag outlet 45 of the cantilever-type screw discharge centrifuge 3 and the liquid outlet 46 of the cantilever-type screw discharge centrifuge 3 in an inclined manner, and the end of the bottom of the casing 31 located at the slag outlet 45 of the cantilever-type screw discharge centrifuge 3 is higher than the end of the bottom of the casing 31 located at the liquid outlet 46 of the cantilever-type screw discharge centrifuge 3.
In a further embodiment of the present invention, a baffle 47 is disposed on the inner wall of the housing 31, the baffle 47 is located between the outer periphery of the drum 34 and the inner periphery of the housing 31, and the baffle 47 is flush with the end of the other end of the drum 34.
The process method of the MVR high-salt wastewater crystallization and salt discharge system is explained as follows:
step S1: high-temperature steam enters the shell pass of the MVR evaporator 1 and heats the salt solution in the tube pass of the MVR evaporator 1;
step S2: the salt solution rises from the bottom of the MVR evaporator 1 to the top of the MVR evaporator 1 under the action of the crystal slurry pump 6;
step S3: the water content of the salt solution is evaporated in the rising process, the concentration of the salt solution is continuously raised to form crystal slurry containing crystal salt with the first concentration, the crystal slurry enters the crystallizer 2 to continue to grow, and the step S4 and the step S5 are executed simultaneously;
step S4: in the crystallizer 2, the small-grained crystallized salt located in the upper layer in the crystallizer 2 is pumped into the tube pass of the MVR evaporator 1 again from the MVR evaporator 1 by the magma pump 6, and the process returns to step S2:
step S5: in the crystallizer 2, the large-particle crystallized salt in the crystallizer 2 settles at the bottom layer of the crystallizer 2 under the action of gravity, the concentration of the crystallized salt in the collected crystal slurry reaches a second concentration, the crystallized salt flows into the cantilever type spiral discharging centrifuge 3, and the step S6 is executed;
step S6: the crystal slurry containing the crystal salt with the second concentration enters the machine shell 31 from the other end of the feeding pipe 37 and is sprayed to the surface of the material distribution cone 36 from one end of the feeding pipe 37, at the moment, the motor group 32 drives the rotary drum 34, the spiral discharger 35 and the material distribution cone 36 to rotate at a high speed through the differential mechanism 33, the crystal slurry is thrown to the inner wall of the rotary drum 34 by utilizing the centrifugal force generated by the high-speed rotation, and a material layer is formed according to the density;
step S7: when the material layer reaches a certain thickness, the material layer is scraped off by a spiral discharger 35 and pushed to a screen 38 for filtering, the material layer is separated into wet salt and clear liquid, and the clear liquid with lower density is extruded to one end of a rotary drum 34 to realize solid-liquid separation;
step S8: discharging wet salt from a slag outlet 45 of the cantilever type spiral discharge centrifuge 3, discharging clear liquid from a liquid outlet 46 of the cantilever type spiral discharge centrifuge 3, and executing step S9 or step S10;
step S9: the wet salt separated by the cantilever type spiral discharging centrifuge 3 falls into a fluidized bed dryer 4 through a flashboard reversing valve 7 for drying to obtain finished salt, and the process is finished;
step S10: and returning the clear liquid separated by the cantilever type spiral discharging centrifuge 3 into the mother liquid tank 5, and finishing.
In a further embodiment of the invention, in step S5, the slurry containing the second concentration of the crystalline salt is flowed into a cantilevered screw discharge centrifuge under the slow action of the agitator.
In a further embodiment of the present invention, the second concentration is 20%.
In a further embodiment of the present invention, the first concentration is 10%.
In a further embodiment of the present invention, in step S7, the moisture content of the wet salt is adjusted by the liquid adjustor 41.
In a further embodiment of the invention, the moisture content of the wet salt is controlled to be within 3%.
Preferably, the MVR evaporator is vertically installed by a shell and tube heat exchanger.
Preferably, the 3% concentration high salt wastewater is passed through the tube side of the MVR evaporator and the 104 ℃ steam is passed through the shell side of the MVR evaporator.
Preferably, the concentration of the crystal slurry after the bottom layer sedimentation and collection of the crystallizer reaches 20%, and the crystal slurry has certain fluidity and can automatically flow into the cantilever type spiral discharging centrifuge 3.
Preferably, the discharge is achieved by the difference in rotational speed of the screw discharger 35 and the drum 34.
In consideration of the problems of cleaning of the cantilever type spiral discharging centrifuge 3 and the like, the flashboard reversing valve 7 is arranged near the slag outlet 45 of the cantilever type spiral discharging centrifuge 3, when the cantilever type spiral discharging centrifuge 3 stops cleaning, the valve of the flashboard reversing valve 7 is closed, and cleaning liquid is discharged from the side face of the valve of the flashboard reversing valve 7 to enter the mother liquid tank 5 and does not enter the fluidized bed dryer 4; when the cantilever type spiral discharging centrifuge 3 works normally, the valve of the inserting plate reversing valve 7 is opened, and the wet salt passes through the valve of the inserting plate reversing valve 7 and falls into the fluidized bed dryer 4 for drying.
The salt produced by the cantilever type spiral discharging centrifuge 3 in the MVR high-salt wastewater crystallization and salt discharge system does not need to be further concentrated by a cyclone and a thickener, and directly enters the cantilever type spiral discharging centrifuge 3 to obtain wet salt with the water content of 2-3%, so that the scale of the fluidized bed dryer 4 is effectively reduced, and the use power consumption is reduced.
The invention cancels a plurality of devices, makes the process chain shorter and more stable, not only can reduce the maintenance cost, the operation cost and the management cost of the devices, but also can optimize the device arrangement and reduce the floor area of the factory building.
The specification of the fluidized bed dryer 4 is reduced, the required power consumption and the steam consumption are reduced, and the problem that the fluidized bed dryer is dead is solved.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.
Claims (15)
1. The utility model provides a MVR high salt waste water crystallization, goes out salt system which characterized in that includes:
an MVR evaporator;
an inlet of the crystallizer is connected with an outlet of the MVR evaporator;
an inlet of the crystal slurry pump is connected with a first outlet of the crystallizer, and an outlet of the crystal slurry pump is connected with an inlet of the MVR evaporator;
the inlet of the cantilever type spiral discharging centrifuge is connected with the second outlet of the crystallizer;
and the fluidized bed dryer is connected with a slag outlet of the cantilever type spiral discharging centrifuge.
2. The MVR high-salt wastewater crystallization and salt discharge system according to claim 1, further comprising: and the mother liquor tank is connected with the liquid outlet of the cantilever type spiral discharging centrifuge.
3. The MVR high-salt wastewater crystallization and salt discharge system according to claim 3, further comprising: the inlet of the flashboard reversing valve is connected with the slag outlet of the cantilever type spiral discharging centrifuge, the inlet of the fluidized bed dryer is connected with the first outlet of the flashboard reversing valve, and the mother liquor tank is connected with the second outlet of the flashboard reversing valve.
4. The MVR high-salt wastewater crystallization and salt discharge system according to claim 3, wherein the cantilever-type spiral discharge centrifuge comprises:
a housing;
the motor group is arranged at one end outside the shell;
one end of the differential is in transmission connection with the motor set, and the other end of the differential extends into one end of the shell;
the rotary drum is arranged in the shell, the rotary drum is arranged at the other end of the differential mechanism, and one end of the rotary drum, which is far away from the differential mechanism, forms a screen;
the spiral discharger is arranged in the shell, is arranged at the other end of the differential mechanism and is positioned in the rotary drum;
the distributing cone is arranged in the shell, is arranged at the end part of the other end of the differential mechanism and is positioned in the spiral discharger;
the inlet pipe, install in of inlet pipe the other end of casing, the one end of inlet pipe stretches into in the screw discharger, and with the cloth awl is just right mutually.
5. The MVR high salt wastewater crystallization and salt discharge system of claim 4, wherein the cantilevered spiral discharge centrifuge further comprises:
the rotating drum bottom is arranged at the other end of the differential mechanism, one end of the rotating drum is fixedly connected with the periphery of one end of the rotating drum bottom, and a plurality of through holes are formed in the rotating drum bottom and are arranged at equal intervals along the circumferential direction of the rotating drum bottom;
and the liquid adjusting devices are arranged at the other end of the rotary drum bottom and are respectively positioned between the through holes and the periphery of the rotary drum bottom.
6. The MVR high-salt wastewater crystallization and salt discharge system according to claim 1, wherein a stirrer is arranged at the bottom of the crystallizer.
7. The MVR high-salt wastewater crystallization and salt discharge system according to claim 4, wherein the slag outlet of the cantilever-type spiral discharge centrifuge and the liquid outlet of the cantilever-type spiral discharge centrifuge are both disposed at the bottom of the casing, the other end of the feeding pipe is an inlet of the cantilever-type spiral discharge centrifuge, and the casing is provided with an air inlet and an air outlet.
8. The MVR high-salt wastewater crystallization and salt discharge system according to claim 1, wherein the first outlet of the crystallizer is located at a sidewall of the crystallizer, and the second outlet of the crystallizer is located at a bottom of the crystallizer.
9. The MVR high salt wastewater crystallization and salt discharge system according to claim 3, wherein the first outlet of the flashboard reversing valve is located at the bottom of the flashboard reversing valve, and the second outlet of the flashboard reversing valve is located at the side wall of the flashboard reversing valve.
10. A process method of an MVR high-salt wastewater crystallization and salt discharge system, which is characterized by comprising the MVR high-salt wastewater crystallization and salt discharge system of any one of claims 6 to 9, wherein the process method comprises:
step S1: high-temperature steam enters a shell pass of the MVR evaporator and heats a salt solution in a tube pass of the MVR evaporator;
step S2: the salt solution rises from the bottom of the MVR evaporator to the top of the MVR evaporator under the action of the crystal slurry pump;
step S3: the salt solution is evaporated during the rising process, the concentration of the salt solution is continuously increased, a crystal slurry containing crystal salt with a first concentration is formed, the crystal slurry enters the crystallizer to continue to grow, and simultaneously, the step S4 and the step S5 are executed;
step S4: in the crystallizer, the small-grained crystallized salt located in the upper layer of the crystallizer is pumped into the tube pass of the MVR evaporator again from the MVR evaporator by the magma pump, and the process returns to step S2:
step S5: in the crystallizer, the large-particle crystallized salt in the crystallizer reaches a second concentration by gravity in the crystal salt in the crystal slurry settled and collected at the bottom layer of the crystallizer, and flows into the cantilever-type spiral discharge centrifuge to perform step S6;
step S6: the crystal slurry containing crystal salt with a second concentration enters the shell from the other end of the feeding pipe and is sprayed to the surface of the material distribution cone from one end of the feeding pipe, at the moment, the motor group drives the rotary drum, the spiral discharger and the material distribution cone to rotate at a high speed through the differential mechanism, the crystal slurry is thrown to the inner wall of the rotary drum by utilizing centrifugal force generated by high-speed rotation, and a material layer is formed according to the density;
step S7: after the material layer reaches a certain thickness, the material layer is scraped off by the spiral discharger and pushed to the screen mesh for filtering, the material layer is separated into wet salt and clear liquid, and the clear liquid with lower density is extruded to one end of the rotary drum to realize solid-liquid separation;
step S8: discharging the wet salt from a slag outlet of the cantilever type spiral discharge centrifuge, discharging the clear liquid from a liquid outlet of the cantilever type spiral discharge centrifuge, and executing the step S9 or the step S10;
step S9: the wet salt separated by the cantilever type spiral discharging centrifuge falls into the fluidized bed dryer through the flashboard reversing valve for drying to obtain finished salt, and the process is finished;
step S10: and returning the clear liquid separated by the cantilever type spiral discharging centrifuge into the mother liquid tank, and finishing.
11. The process of the MVR high-salt wastewater crystallization and salt discharge system according to claim 10, wherein in step S5, the crystal slurry containing a second concentration of crystal salt flows into the cantilever-type screw discharge centrifuge under the slow action of the stirrer.
12. The process of the MVR high-salt wastewater crystallization and salt discharge system according to claim 10, wherein the second concentration is 20%.
13. The process of the MVR high-salt wastewater crystallization and salt discharge system according to claim 10, wherein the first concentration is 10%.
14. The process of the MVR high-salt wastewater crystallization and salt discharge system according to claim 10, wherein in step S7, the moisture content of the wet salt is adjusted by the liquid conditioner.
15. The process of the MVR high-salt wastewater crystallization and salt discharge system according to claim 14, wherein the moisture content of the wet salt is controlled within 3%.
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