CN220345128U - Continuous freezing crystallization potassium chloride separation system - Google Patents
Continuous freezing crystallization potassium chloride separation system Download PDFInfo
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- CN220345128U CN220345128U CN202321463319.9U CN202321463319U CN220345128U CN 220345128 U CN220345128 U CN 220345128U CN 202321463319 U CN202321463319 U CN 202321463319U CN 220345128 U CN220345128 U CN 220345128U
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- 238000007710 freezing Methods 0.000 title claims abstract description 90
- 230000008014 freezing Effects 0.000 title claims abstract description 90
- 238000002425 crystallisation Methods 0.000 title claims abstract description 62
- 230000008025 crystallization Effects 0.000 title claims abstract description 62
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 title claims abstract description 61
- 238000000926 separation method Methods 0.000 title claims abstract description 35
- 239000001103 potassium chloride Substances 0.000 title claims abstract description 30
- 235000011164 potassium chloride Nutrition 0.000 title claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 80
- 239000002562 thickening agent Substances 0.000 claims abstract description 16
- 239000012452 mother liquor Substances 0.000 claims description 25
- 230000007704 transition Effects 0.000 claims description 21
- 239000003507 refrigerant Substances 0.000 claims description 17
- 239000006228 supernatant Substances 0.000 claims description 9
- 230000008719 thickening Effects 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 7
- 239000011521 glass Substances 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 3
- 238000010992 reflux Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 14
- 238000000034 method Methods 0.000 description 13
- 239000002351 wastewater Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 239000002994 raw material Substances 0.000 description 10
- 238000007599 discharging Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 239000011780 sodium chloride Substances 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 210000003298 dental enamel Anatomy 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 238000011161 development Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000011549 crystallization solution Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000002688 persistence Effects 0.000 description 1
- 229940072033 potash Drugs 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Physical Water Treatments (AREA)
Abstract
The embodiment of the utility model discloses a continuous freezing crystallization potassium chloride separation system, which comprises a material tank, a freezing crystallizer, a thickener, a centrifugal machine and a circulating freezing system, wherein the material tank is connected with a feed inlet of the freezing crystallizer through a feed pump, a discharge outlet of the freezing crystallizer is connected with a feed end of the thickener through a discharge pump, the discharge end of the thickener is connected with the centrifugal machine, a forced circulating pump is arranged on the freezing crystallizer and is connected with the circulating freezing system, a circulating liquid lifting pump and a circulating liquid buffer tank are arranged between a shell side inlet and a shell side outlet of the freezing crystallizer, and a reflux end of the circulating freezing system is connected with a circulating pipe inlet of the freezing crystallizer.
Description
Technical Field
The embodiment of the utility model relates to the technical field of industrial salt separation, in particular to a continuous freezing crystallization potassium chloride separation system.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the utility model and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
With the rapid development of the economy and the continuous growth of basic industry in China, the environmental pollution problem caused by the inadequate discharge of the waste water of the three industrial wastes is more and more serious, and the proper treatment of the industrial waste water is imperative. High-salt wastewater is a toxic and difficult-to-degrade industrial wastewater. The industrial fields of printing and dyeing, papermaking, chemical industry, oil refining, seawater utilization and the like can produce a large amount of high-salt wastewater. If the high-salt wastewater is directly or diluted and discharged, on one hand, the water resource waste is caused; on the other hand, the method can cause adverse effect on the environment, namely accelerating eutrophication of rivers and lakes, causing the collapse of a soil ecosystem, generating malodor to affect the water quality, changing the color and the visibility of water, forming a large amount of water suspended matters and the like.
With the development of industry, the generated high-salt wastewater is more and more complex in components and higher in concentration, so that the research on an effective treatment method of the high-salt wastewater is urgent.
Most of hydrometallurgical wastewater contains high salt content, contains components of potassium chloride and sodium chloride, and in China, the potassium chloride is a scarce resource, and the economic benefit generated by recycling the potash fertilizer can well complement the cost of wastewater treatment, so that the method is in line with the concept of circular economy. The evaporative crystallization technology is concerned by the chemical industry as a water treatment process for treating high-salt wastewater, and is widely applied to the field of wastewater zero emission and wastewater reclamation.
In the sodium chloride and potassium chloride salt separation technology, sodium chloride and potassium chloride are separated by utilizing different solubilities of the sodium chloride and the potassium chloride in water at different temperatures, firstly evaporating and crystallizing to separate sodium chloride, and then sending mother liquor into an enamel kettle for cooling and crystallizing to separate potassium chloride; because the enamel kettles are cooled intermittently, continuous production cannot be realized, and for wastewater containing more potassium chloride, a plurality of enamel kettles are needed, so that the occupied area is overlarge, and the running cost is increased; a continuous freezing crystallization system is used for separating sodium chloride and potassium chloride.
Disclosure of Invention
Therefore, the embodiment of the utility model provides a continuous freezing crystallization potassium chloride separation system, which solves the problems that in the prior art, the working process cannot be continuously carried out, the cost is increased and the efficiency is low because the low-temperature separation of potassium chloride is performed in an intermittent separation mode.
In order to achieve the above object, the embodiments of the present utility model provide the following technical solutions:
in a first aspect of the embodiment of the utility model, a continuous freezing crystallization potassium chloride separation system is provided, which comprises a raw material tank, a freezing crystallizer, a thickener, a centrifugal machine and a circulating freezing system, wherein the raw material tank is connected with a feed inlet of the freezing crystallizer through a feed pump, a discharge outlet of the freezing crystallizer is connected with a feed end of the thickener through a discharge pump, a discharge end of the thickener is connected with the centrifugal machine, a forced circulating pump is arranged on the freezing crystallizer and is connected with the circulating freezing system, a circulating liquid lifting pump and a circulating liquid buffer tank are arranged between a shell side inlet and a shell side outlet of the freezing crystallizer, and a reflux end of the circulating freezing system is connected with a circulating pipe inlet of the freezing crystallizer.
Further, the circulating refrigeration system comprises a circulating refrigerator and a refrigeration unit, wherein the outlet end of the forced circulating pump is connected with the tube side inlet of the circulating refrigerator, the tube side outlet of the circulating refrigerator is connected with the circulating tube inlet of the freezing crystallizer, the outlet end of the refrigeration unit is connected with the shell side inlet of the circulating refrigerator, and the shell side outlet of the circulating refrigerator is connected with the inlet end of the refrigeration unit.
Further, a refrigerant heat exchanger is further arranged between the circulating refrigerator and the refrigerating unit, an outlet end of the refrigerating unit is connected with a cold liquid inlet of the refrigerant heat exchanger, a circulating outlet of the refrigerant heat exchanger is connected with an inlet end of the refrigerating unit, a cold liquid outlet of the refrigerant heat exchanger is connected with a shell side inlet end of the circulating refrigerator through an auxiliary circulating pump, and a shell side outlet end of the circulating refrigerator is connected with a circulating inlet of the refrigerant heat exchanger through a circulating liquid pump.
Further, the shell side outlet end of the circulating refrigerator is also connected with the inlet end of the auxiliary circulating pump.
Further, the crystallization barrel of the freezing crystallizer comprises a solid-liquid separation zone, a transition zone, a thickening zone and a crystallization zone, the pipe diameter from the solid-liquid separation zone to the crystallization zone is gradually reduced, a circulating pipe extending to the outside of the crystallization barrel is arranged in the crystallization barrel, an inlet of the circulating pipe is positioned at the solid-liquid separation zone, an inner outlet of the circulating pipe extends to the crystallization zone and has a gap with the bottom surface of the crystallization zone, a feed liquid circulation outlet is arranged at the transition zone, a discharge port of the freezing crystallizer is arranged on the crystallization zone, and an exhaust port and a plurality of viewing mirrors are arranged on the crystallization barrel.
Further, the transition area and the crystallization area are inverted round table type cylinder bodies, the diameter of the upper bottom surface of the transition area is the same as that of the lower bottom surface of the crystallization area, and the upper bottom surface of the crystallization area is of an outwards protruding arc-shaped structure.
Further, a round bottom protruding inwards is arranged in the middle of the bottom surface of the crystallization area, and the round bottom is opposite to the inner outlet of the circulating pipe.
Further, the sight glass is respectively arranged on the cylinder walls of the solid-liquid separation area, the transition area, the thickening area and the crystallization area, and the feed liquid circulation outlet is at right angles with the outer wall of the transition area.
Further, the solid phase outlet of centrifuge is connected with the aggregate unit, the liquid phase outlet of centrifuge is connected with the mother liquor tank, the upper outlet of mother liquor tank is connected with the supernatant tank, the lower outlet of mother liquor tank is connected with the feed inlet of the freezing crystallizer through the mother liquor pump.
Further, the overflow port of the thickener is connected with the liquid inlet of the mother liquid tank, and the height of one end of the inner lower outlet of the mother liquid tank is lower than that of the other opposite side.
According to an embodiment of the utility model, the system has the following advantages: the device comprises a raw material tank, a freezing crystallizer, a thickener, a centrifugal machine and a circulating freezing system, wherein the raw material tank is connected with a feeding port of the freezing crystallizer through a feeding pump, a discharging port of the freezing crystallizer is connected with a feeding end of the thickener through a discharging pump, the discharging end of the thickener is connected with the centrifugal machine, a forced circulating pump is arranged on the freezing crystallizer and is connected with the circulating freezing system, a circulating liquid lifting pump and a circulating liquid buffer tank are arranged between a shell side inlet and a shell side outlet of the freezing crystallizer, a reflux end of the circulating freezing system is connected with a circulating pipe inlet of the freezing crystallizer, and the system crystallizes raw material liquid at a lower temperature through a circulating cooling refrigerating liquid circulating structure and a circulating freezing system in the implementation process, so that the crystallization efficiency is improved and the labor cost is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It will be apparent to those skilled in the art from this disclosure that the drawings described below are merely exemplary and that other embodiments may be derived from the drawings provided without undue effort.
The structures, proportions, sizes, etc. shown in the present specification are shown only for the purposes of illustration and description, and are not intended to limit the scope of the utility model, which is defined by the claims, so that any structural modifications, changes in proportions, or adjustments of sizes, which do not affect the efficacy or the achievement of the present utility model, should fall within the ambit of the technical disclosure.
FIG. 1 is a schematic diagram of a system architecture of a continuous freezing and crystallizing potassium chloride separation system according to an embodiment of the present utility model;
fig. 2 is a schematic structural diagram of a freezing crystallizer in a continuous freezing crystallization potassium chloride separation system according to an embodiment of the present utility model.
In the figure: 1. a raw material tank; 2. freezing the crystallizer; 3. a thickener; 4. a centrifuge; 5. a feed pump; 6. a discharge pump; 7. a forced circulation pump; 8. a circulating liquid lifting pump; 9. a circulating liquid buffer tank; 10. a circulation freezer; 11. a refrigerating unit; 12. a refrigerant heat exchanger; 13. an auxiliary circulation pump; 14. a circulation liquid pump; 15. a separation zone; 16. a transition zone; 17. a thickening zone; 18. a crystallization zone; 19. a circulation pipe; 20. a feed liquid circulation outlet; 21. a viewing mirror; 22. round bottom; 23. a mother liquor tank; 24. a supernatant tank; 25. mother liquor pump.
Detailed Description
Other advantages and advantages of the present utility model will become apparent to those skilled in the art from the following detailed description, which, by way of illustration, is to be read in connection with certain specific embodiments, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The terms such as "upper", "lower", "left", "right", "middle" and the like are also used in the present specification for convenience of description, but are not intended to limit the scope of the present utility model, and the changes or modifications of the relative relationship thereof are considered to be within the scope of the present utility model without substantial modification of the technical content.
Fig. 1 is a schematic diagram showing a system structure of a continuous freezing crystallization potassium chloride separation system according to an embodiment of the present utility model. In this embodiment, this system includes head tank 1, freezing crystallizer 2, thick ware 3, centrifuge 4 and circulation refrigerating system, head tank 1 passes through feed pump 5 and connects the feed inlet of freezing crystallizer 2, the feed end of thick ware 3 is connected through discharge pump 6 to the discharge gate of freezing crystallizer 2, centrifuge 4 is connected to the discharge end of thick ware 3, set up forced circulation pump 7 on the freezing crystallizer 2 and connect the circulation refrigerating system, set up circulation liquid elevator pump 8 and circulation liquid buffer tank 9 between the shell side import and the shell side export of freezing crystallizer 2, circulation refrigerating system's return end is connected the circulation pipe 19 import of freezing crystallizer 2.
In the implementation process of the system, the freezing liquid circulation structure capable of circularly reducing the temperature and the circulation freezing system are arranged, the position in the raw material liquid type is crystallized at the temperature of the intersection, so that the crystallization efficiency is improved, and meanwhile, the labor cost is reduced.
In this embodiment, the circulation freezing system includes circulation freezer 10 and refrigerating unit 11, the exit end of forced circulation pump 7 is connected circulation freezer 10 tube side import, the tube side exit linkage of circulation freezer 10 freezes the circulating pipe 19 import of crystallizer 2, the exit end of refrigerating unit 11 is connected the shell side import of circulation freezer 10, the shell side exit linkage refrigerating unit 11's entrance point, refrigerating unit 11 starts after circulation liquid circulation cooling process, last circulation liquid cooling for the purpose that the circulation liquid was last for the stoste cooling in circulation freezer 10 has been reached, the persistence of stoste crystallization has been ensured, crystallization separation efficiency.
In order to avoid that high-temperature circulating liquid directly enters the low-temperature refrigerating unit 11 after being refluxed, the refrigerating unit 11 is damaged, a refrigerant heat exchanger 12 is further arranged between the circulating refrigerating unit 10 and the refrigerating unit 11, the outlet end of the refrigerating unit 11 is connected with the cold liquid inlet of the refrigerant heat exchanger 12, the circulating outlet of the refrigerant heat exchanger 12 is connected with the inlet end of the refrigerating unit 11, the cold liquid outlet of the refrigerant heat exchanger 12 is connected with the shell side inlet end of the circulating refrigerating unit 10 through an auxiliary circulating pump 13, the shell side outlet end of the circulating refrigerating unit 10 is connected with the circulating inlet of the refrigerant heat exchanger 12 through a circulating liquid pump 14, and after heat exchange of the refrigerant heat exchanger 12, the temperature of circulating liquid is kept within a preset temperature range, so that crystallization is maximized.
Under the condition that the working strength of the circulating refrigerator 10 is not high and the temperature change of the refrigerating fluid in the primary circulating process is not large, the shell side outlet end of the circulating refrigerator 10 is also connected with the inlet end of the auxiliary circulating pump 13, the circulating fluid is forced to circulate, the power consumption of the refrigerating unit 11 is reduced, and the cost is reduced.
As shown in fig. 2, the structure of the freezing crystallizer 2 is schematically shown, the freezing crystallizer 2 is a clean container capable of adapting to a low temperature state, the freezing crystallizer 2 is a crystallization barrel, the crystallization barrel is composed of a solid-liquid separation zone 15, a transition zone 16, a thickening zone 17 and a crystallization zone 18, the pipe diameter from the solid-liquid separation zone 15 to the crystallization zone 18 is gradually reduced, a circulating pipe 19 extending to the outside is arranged in the crystallization barrel, an inlet of the circulating pipe 19 is positioned at the solid-liquid separation zone 15, an inner outlet of the circulating pipe 19 extends to the crystallization zone 18 and has a gap with the bottom surface of the crystallization zone 18, a feed liquid circulation outlet 20 is arranged at the transition zone 16, a discharge hole of the freezing crystallizer 2 is arranged on the crystallization zone 18, and an exhaust port and a plurality of sight glass 21 are arranged on the crystallization barrel.
The freezing crystallization separator adopts an overflow crystallization form from bottom to top, and through changing the volume of the overflow process, feed liquid enters the bottom through the central circulating pipe 19 and returns to the upper end, so that an extrusion crystallization form is formed, and the granularity of crystallized salt is ensured to meet the requirement while the rapid crystallization at the bottom of a container is met.
In a specific structure, in order to further enable the crystallization solution to be rapidly crystallized so that the solution is rapidly discharged, the transition area 16 and the crystallization area 18 are inverted truncated cone-shaped cylinders, the diameter of the upper bottom surface of the transition area 16 is the same as that of the lower bottom surface of the crystallization area 18, the upper bottom surface of the crystallization area 18 is of an arc-shaped structure protruding outwards, and the bottom surface of the arc-shaped structure is used for avoiding circulation blockage of feed liquid in the crystallization area 18.
More importantly, the cross-section of the crystallization zone 18 is smaller than the cross-section of the transition zone 16, which can more rapidly promote crystallization of the high concentration feed liquid in the crystallization zone 18 and improve efficiency, and the transition zone 16 can more easily promote discharge of the separated liquid along the feed liquid circulation outlet 20.
In order to further improve the rapid accumulation and crystallization of the mixed feed liquid entering the crystallization zone 18 to the peripheral side of the bottom, the bottom middle position of the crystallization zone 18 is provided with an inward convex round bottom 22, and the round bottom 22 is opposite to the inner outlet of the feed liquid circulation feed pipe.
In this embodiment, the diameter ratio of the solid-liquid separation area 15 to the thickening area 17 is 1.5-2, and generally the higher the concentration is, the larger the diameter ratio is, so that smooth operation is ensured.
In order to be able to easily check the working state of each zone of the freeze crystallizer 2, the sight glass 21 is respectively arranged on the walls of the solid-liquid separation zone 15, the transition zone 16, the thickening zone 17 and the crystallization zone 18, and the feed liquid circulation outlet 20 is at right angles to the outer wall of the transition zone 16.
In this embodiment, referring again to fig. 1, the solid phase outlet of the centrifuge 4 is connected with the aggregate unit, the liquid phase outlet of the centrifuge 4 is connected with the mother liquor tank 23, the upper outlet of the mother liquor tank 23 is connected with the supernatant tank 24, the lower outlet of the mother liquor tank 23 is connected with the feed inlet of the freezing crystallizer 2 through the mother liquor pump 25, and the mother liquor tank 23 is arranged to crystallize potassium chloride in the solution more thoroughly.
Wherein, the overflow port of the thickener 3 is connected with the liquid inlet of the mother liquid tank 23, and the height of one end of the inner lower outlet of the mother liquid tank 23 is lower than that of the opposite side, thereby avoiding the blockage in the thickener 3.
In this embodiment, exhaust ports are provided on the raw material tank 1, the freezing crystallizer 2, the thickener 3, the circulating liquid buffer tank 9, the mother liquid tank 23 and the supernatant liquid tank 24, and the supernatant liquid tank 24 is a terminal separation liquid tank for crystallization separation.
The system mainly treats brine containing potassium chloride and sodium chloride, adopts a process of producing potassium chloride by freezing crystallization, and discharges frozen mother liquor. The working process is as follows:
feeding: the raw material liquid is pumped into the freezing crystallizer 2 through the feed pump 5, the feed is stopped after the liquid level reaches a certain height, and then the forced circulation pump 7 is started and gradually increased in frequency to be close to full frequency. The circulating liquid lifting pump 8 is started at the same time of feeding the raw material liquid, and the circulating liquid is sent into the shell side of the circulating refrigerator 10 until the circulating liquid overflows the circulating refrigerator 10.
System pre-cooling: after the forced circulation pump 7 is started and stably operates, the auxiliary circulation pump 13 is started; after the auxiliary circulation pump 13 is stably operated, the circulating liquid is stably circulated in the shell side of the circulation freezer 10; at this time, the refrigerating unit 11 and the circulating liquid pump 14 are started to gradually cool the system, and the system gradually reaches a stable state. Crystals are separated out in the cooling process, at the moment, sampling can be carried out through a sampling port of the freezing crystallizer 2, and if the solid content reaches a certain amount, a discharging pump 6 is started for discharging.
Continuous operation: when the temperature of the freezing crystallizer 2 reaches 15 ℃ and the temperature of the circulating liquid reaches 5 ℃, the system reaches a stable state. At the moment, continuous feeding and discharging can be kept, the feeding amount is slowly increased to a design value, meanwhile, the refrigerating capacity of the refrigerating unit 11 is increased, and the temperature difference of the circulating refrigerator 10 is ensured to be about 10 ℃.
Continuous discharging: when the solid content in the freezing crystallizer 2 reaches a certain proportion, a discharging pump 6 is started to continuously discharge, the feed liquid containing crystals is concentrated in the thickener 3 and then enters a centrifugal machine 4 for centrifugal separation, and the separated crystals are sent to be packaged.
The separated mother liquor enters a mother liquor tank 23, the mother liquor containing part of crystals at the bottom of the mother liquor tank 23 returns to the freezing crystallizer 2, the supernatant mother liquor enters a supernatant tank 24, and the clear mother liquor is sent out through a supernatant pump.
While the utility model has been described in detail in the foregoing general description and specific examples, it will be apparent to those skilled in the art that modifications and improvements can be made thereto. Accordingly, such modifications or improvements may be made without departing from the spirit of the utility model and are intended to be within the scope of the utility model as claimed.
Claims (10)
1. The utility model provides a continuous freezing crystallization potassium chloride piece-rate system, its characterized in that includes head tank, freezing crystallizer, thick ware, centrifuge and circulation refrigerating system, the feed inlet of freezing crystallizer is connected through the charge pump to the head tank, the discharge gate of freezing crystallizer passes through the feed end that the discharge pump connects thick ware, the discharge end of thick ware is connected centrifuge, set up forced circulation pump connection circulation refrigerating system on the freezing crystallizer, set up circulation liquid elevator pump and circulation liquid buffer tank between the shell side import and the shell side export of freezing crystallizer, circulation refrigerating system's return end is connected the circulation pipe import of freezing crystallizer.
2. The continuous freezing and crystallizing potassium chloride separation system as recited in claim 1, wherein the circulating freezing system comprises a circulating freezer and a freezing unit, an outlet end of the forced circulation pump is connected to a tube side inlet of the circulating freezer, a tube side outlet of the circulating freezer is connected to a circulating tube inlet of the freezing crystallizer, an outlet end of the freezing unit is connected to a shell side inlet of the circulating freezer, and a shell side outlet of the circulating freezer is connected to an inlet end of the freezing unit.
3. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 2, wherein a refrigerant heat exchanger is further arranged between the circulating refrigerator and the refrigerating unit, an outlet end of the refrigerating unit is connected with a cold liquid inlet of the refrigerant heat exchanger, a circulating outlet of the refrigerant heat exchanger is connected with an inlet end of the refrigerating unit, the cold liquid outlet of the refrigerant heat exchanger is connected with a shell side inlet end of the circulating refrigerator through an auxiliary circulating pump, and a shell side outlet end of the circulating refrigerator is connected with a circulating inlet of the refrigerant heat exchanger through a circulating liquid pump.
4. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 3, wherein the shell side outlet end of the circulation chiller is further connected to the inlet end of an auxiliary circulation pump.
5. The continuous freezing and crystallizing potassium chloride separating system as claimed in claim 1, wherein the crystallizing cylinder of the freezing crystallizer consists of a solid-liquid separating area, a transition area, a thickening area and a crystallizing area, wherein the pipe diameter from the solid-liquid separating area to the crystallizing area is gradually reduced, a circulating pipe extending to the outside of the crystallizing cylinder is arranged in the crystallizing cylinder, an inlet of the circulating pipe is positioned at the solid-liquid separating area, an inner outlet of the circulating pipe extends to the crystallizing area and has a gap with the bottom surface of the crystallizing area, a feed liquid circulating outlet is arranged at the transition area, a discharge hole of the freezing crystallizer is arranged on the crystallizing area, and an exhaust port and a plurality of viewing mirrors are arranged on the crystallizing cylinder.
6. The continuous freezing and crystallizing potassium chloride separating system as claimed in claim 5, wherein the transition zone and the crystallization zone are in an inverted truncated cone type cylinder, the diameter of the upper bottom surface of the transition zone is the same as the diameter of the lower bottom surface of the crystallization zone, and the upper bottom surface of the crystallization zone is in an arc-shaped structure protruding outwards.
7. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 6, wherein a bottom surface intermediate the crystallization zone is provided with an inwardly convex rounded bottom, said rounded bottom being opposite to the inner outlet of said circulation tube.
8. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 7, wherein said sight glass is respectively disposed on the walls of the solid-liquid separation zone, the transition zone, the thickening zone and the crystallization zone, and said feed liquid circulation outlet is at right angles to the outer wall of the transition zone.
9. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 1, wherein a solid phase outlet of the centrifuge is connected with a collecting unit, a liquid phase outlet of the centrifuge is connected with a mother liquor tank, an upper outlet of the mother liquor tank is connected with a supernatant tank, and a lower outlet of the mother liquor tank is connected with a feed inlet of the freezing crystallizer through a mother liquor pump.
10. The continuous freezing and crystallizing potassium chloride separation system as claimed in claim 9, wherein an overflow port of said thickener is connected to a liquid inlet of said mother liquor tank, and a lower outlet of an interior of said mother liquor tank is lower in height at one end than at the opposite side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321463319.9U CN220345128U (en) | 2023-06-09 | 2023-06-09 | Continuous freezing crystallization potassium chloride separation system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321463319.9U CN220345128U (en) | 2023-06-09 | 2023-06-09 | Continuous freezing crystallization potassium chloride separation system |
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| CN220345128U true CN220345128U (en) | 2024-01-16 |
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| CN202321463319.9U Active CN220345128U (en) | 2023-06-09 | 2023-06-09 | Continuous freezing crystallization potassium chloride separation system |
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- 2023-06-09 CN CN202321463319.9U patent/CN220345128U/en active Active
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