CN213221025U - Control system for improving potassium chloride particle size in potassium-sodium separation - Google Patents
Control system for improving potassium chloride particle size in potassium-sodium separation Download PDFInfo
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- CN213221025U CN213221025U CN202021367551.9U CN202021367551U CN213221025U CN 213221025 U CN213221025 U CN 213221025U CN 202021367551 U CN202021367551 U CN 202021367551U CN 213221025 U CN213221025 U CN 213221025U
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Abstract
The utility model discloses a control system for improving the grain diameter of potassium chloride in the separation of potassium and sodium, relating to the technical field of chemical process; comprises a front-end MVR evaporation system for evaporating and separating out sodium chloride and a rear-end vacuum flash evaporation Oslo system for cooling and separating out potassium chloride crystals; the method is characterized in that: the MVR evaporation system is communicated with the vacuum flash Oslo system. The utility model solves the problems of uneven particle size distribution, uneven crystal form, serious entrainment, poor product quality and the like of the chlorinating agent product, so that the particle size is controllable; the control system comprises an evaporation system and a cooling system, so that the efficiency of the whole reaction is improved, and the production energy consumption is reduced.
Description
Technical Field
The utility model relates to a chemical industry technology technical field, especially a control system who improves potassium chloride particle diameter in potassium-sodium separation.
Background
The potassium-sodium salt separation technology mainly aims at a mixed solution of potassium chloride and sodium chloride, and a lot of wastewater mainly contains sodium chloride and potassium chloride in an industrial process. The concentration fluctuation of the two materials is large, and in order to obtain potassium chloride and sodium chloride products with high purity, a process route for thermally crystallizing sodium chloride salt and cold crystallizing potassium chloride salt is designed according to the physical and chemical properties of the sodium chloride and the potassium chloride. There are three distinct regions of solution concentration and temperature: unstable area, metastable area and stable area, the designed evaporative crystallizer and Oslo crystallizer need to effectively control the supersaturation degree of the solution in the metastable area to ensure the formation of crystallized particles.
The existing process for producing potassium chloride by cold crystallization has the defects of discontinuous and uncontrollable operation, large labor intensity, large occupied area of equipment, difficult control of product quality, difficult qualification of granularity and span indexes and the like.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problems in the prior art and provide a control system for improving the particle size of potassium chloride in the separation of potassium and sodium; a more reasonable process method is provided, and the reaction efficiency is improved; solves the problems of uneven particle size distribution, inhomogeneous crystal form, serious entrainment, poor product quality and the like of the chlorinating agent product, and ensures that the particle size is controllable.
In order to solve the technical problem, the utility model discloses a following technical scheme:
a control system for improving the grain size of potassium chloride in potassium-sodium separation comprises a front-end MVR evaporation system for evaporating and separating out sodium chloride and a rear-end vacuum flash evaporation Oslo system for cooling and separating out potassium chloride crystals; the MVR evaporation system is communicated with the vacuum flash Oslo system.
Preferably, the MVR evaporation system comprises a raw liquid tank, a distilled water preheater, a steam preheater, a forced circulation pump, a forced circulation heat exchanger, a sodium separation mother liquid tank, a crystallization separator, a sodium chloride thickener and a sodium chloride centrifuge; the raw liquid tank is connected with the distilled water preheater through a raw material pump, the distilled water preheater is communicated with the steam preheater, and the steam preheater is connected with a forced circulation heat exchanger through a forced circulation pump; the top of the forced circulation heat exchanger is communicated with a crystallization separator, the bottom of the crystallization separator is communicated with the top of a sodium chloride thickener through a sodium chloride discharge pump, the bottom of the sodium chloride thickener is communicated with a sodium chloride centrifuge, and the sodium chloride centrifuge is communicated with a sodium separation mother liquor tank; the bottom of the sodium separation mother liquor tank is communicated with a vacuum flash evaporation Oslo system through a sodium separation mother liquor pump, and the bottom of the sodium separation mother liquor tank is also communicated with a forced circulation heat exchanger through the sodium separation mother liquor pump and a forced circulation pump.
Preferably, the crystallization separator is communicated with a forced circulation pump; wherein the forced circulation pump, the forced circulation heat exchanger and the crystallization separator form a circulation path.
Preferably, the top of the crystallization separator is communicated with a secondary separator, the secondary separator is respectively communicated with the liquid accumulation tank and a compressor, and the compressor is communicated with the liquid accumulation tank; the liquid accumulation tank is communicated with the distilled water tank through a liquid accumulation pump, the bottom of the distilled water tank is communicated with the distilled water preheater through a distilled water pump, the top of the distilled water tank is also communicated with the steam preheater and the forced circulation heat exchanger respectively, and the forced circulation heat exchanger is communicated with the vacuum pump through a vacuum pump cooler.
Preferably, the vacuum flash oslo system comprises a cold crystallization forced circulation pump, a potassium precipitation mother liquor tank, a potassium chloride centrifuge, an oslo crystallizer and a coagulator; a circulation loop is formed between the cold crystallization forced circulation pump and the Oslo crystallizer, the top of the Oslo crystallizer is communicated with the bottom of the condenser, and a steam ejector is arranged between the Oslo crystallizer and the condenser; the bottom of the Oslo crystallizer is communicated with a potassium chloride thickener through a potassium chloride discharge pump, the potassium chloride thickener is connected with a potassium chloride centrifugal machine, and the potassium chloride centrifugal machine is communicated with a potassium separation mother liquor tank; the bottom of the potassium analysis mother liquor tank is communicated with an MVR evaporation system.
Preferably, the upper part of the potassium chloride thickener is also directly communicated with a potassium analysis mother liquor tank, and the bottom of the potassium analysis mother liquor tank is communicated with the bottom of the forced circulation heat exchanger of the MVR evaporation system through a potassium analysis mother liquor pump; and a circulation loop is also formed between the potassium separation mother liquor pump and the potassium separation mother liquor tank.
Preferably, the upper part of the coagulation device is also connected with a potassium chloride vacuum pump.
Based on the system, the utility model also provides a control method for improving the grain diameter of potassium chloride in the separation of potassium and sodium, which comprises the following steps,
1) the compressor supplies heat to the forced circulation heat exchanger, the raw material pump inputs the raw material into the MVR evaporation system, and the forced circulation pump, the forced circulation heat exchanger and the crystallization separator are sequentially connected to form evaporation concentration circulation of the material;
2) a flow detector and a density detector at the bottom of the crystallization separator detect the flow and the density of the material concentrated solution;
3) when the concentrated solution of the material reaches the required concentration ratio, discharging, conveying the concentrated solution containing crystals to a sodium chloride thickener through a sodium chloride discharging pump, and separating and crystallizing through a sodium chloride centrifugal machine to separate out sodium chloride salt; transferring the potassium chloride mother liquor rich in saturated concentration into a vacuum flash evaporation Oslo system;
4) through the vacuum combination of a steam ejector and a potassium chloride vacuum pump, the potassium chloride solution is flashed and cooled in an Oslo crystallizer, and the potassium chloride is cooled and crystals grow in the Oslo crystallizer;
5) then detecting the flow and density of the material concentrated solution by a flow detector and a density detector at the bottom of the Oslo crystallizer, and starting discharging when the concentrated solution of the material reaches the required concentration ratio;
6) and (3) pumping the concentrated solution containing the crystals to a potassium chloride thickener through a potassium chloride discharge pump, separating and crystallizing through a potassium chloride centrifugal machine, and separating potassium chloride salt out of the system.
The utility model has the advantages that: the problems of uneven particle size distribution, non-uniform crystal form, serious entrainment, poor product quality and the like of the chlorinating agent product particles are solved, so that the particle size is controllable, and more ideal crystal particle size is obtained; the control system comprises an evaporation system and a cooling system, so that the efficiency of the whole reaction is improved, and the production energy consumption is reduced.
Drawings
The accompanying drawings are included to provide a preferred understanding of the present invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
fig. 1 is a schematic diagram of the system distribution of the present invention.
Reference numbers in the figures: a raw material tank 101, a raw material pump 102, a distilled water preheater 103, a distilled water pump 104, a steam preheater 105, a distilled water tank 106, a liquid loading pump 107, a liquid loading tank 108, a forced circulation pump 109, a forced circulation heat exchanger 110, a sodium precipitation mother liquor pump 111, a sodium precipitation mother liquor tank 112, a vacuum pump 113, a vacuum pump cooler 114, a compressor 115, a secondary separator 116, a crystallization separator 117, a sodium chloride discharge pump 118, a sodium chloride thickener 119, a sodium chloride centrifuge 120, a cold crystallization forced circulation pump 201, a potassium precipitation mother liquor pump 202, a potassium precipitation mother liquor tank 203, a potassium chloride centrifuge 204, an Oslo crystallizer 205, a potassium chloride discharge pump 206, a steam ejector 207, a coagulation device 208, a potassium chloride thickener 209, and a potassium chloride vacuum pump 210.
Detailed Description
The following describes preferred embodiments of the present invention in detail with reference to the accompanying drawings.
As shown in the figure, a control system for improving the particle size of potassium chloride in potassium-sodium separation comprises a front-end MVR evaporation system 100 for evaporating and separating out sodium chloride and a rear-end vacuum flash evaporation Oslo system 200 for cooling and separating out potassium chloride crystals; the MVR vaporization system 100 is in communication with a vacuum flash oslo system 200.
The front-end MVR evaporation system 100 includes a raw liquid tank 101, a distilled water preheater 103, a steam preheater 105, a forced circulation pump 109, a forced circulation heat exchanger 110, a sodium-separating mother liquid tank 112, a crystallization separator 117, a sodium chloride thickener 119, and a sodium chloride centrifuge 120.
The raw material tank 101 is connected with the distilled water preheater 103 through a raw material pump 102, the distilled water preheater 103 is communicated with the steam preheater 105, and the steam preheater 105 is connected with a forced circulation heat exchanger 110 through a forced circulation pump 109; the materials are stored in a raw material tank 101 and are pumped into a distilled water preheater 103 through a raw material pump 102; then the secondary steam and the material heated by the compressor 115 are heated in the forced circulation heat exchanger 110 to raise the temperature after passing through the steam preheater 105 and reaching the evaporation temperature.
The crystallization separator 117 is communicated with the forced circulation pump 109; wherein the forced circulation pump 109, the forced circulation heat exchanger 110 and the crystal separator 117 form a circulation path; the material is circulated by the forced circulation pump 109 by axial pushing, and then the material is subjected to gas-liquid separation in the crystal separator 117.
The top of the crystallization separator 117 is communicated with a secondary separator 116, the secondary separator 116 is respectively communicated with the liquid loading tank 108 and the compressor 115, and the compressor 115 is communicated with the liquid loading tank 108; the liquid accumulation tank 108 is communicated with the distilled water tank 106 through the liquid accumulation pump 107, secondary steam generated in the crystallization separator 117 passes through the secondary separator 116 and then enters the compressor 115 to be compressed and do work, the enthalpy value of the steam is increased, the steam is rewashed and enters the forced circulation heat exchanger 110 to be heated, condensed water enters the distilled water tank 106, the bottom of the distilled water tank 106 is communicated with the distilled water preheater 103 through the distilled water pump 104, and the condensed water enters the distilled water preheater 103 to exchange heat with materials after passing through the distilled water pump 104.
The bottom of the crystallization separator 117 is communicated with the top of a sodium chloride thickener 119 through a sodium chloride discharge pump 118, the bottom of the sodium chloride thickener 119 is communicated with a sodium chloride centrifuge 120, and the sodium chloride centrifuge 120 is communicated with a sodium-separating mother liquor tank 112; the bottom of the sodium separation mother liquor tank 112 is communicated with the vacuum flash Oslo system 200 through a sodium separation mother liquor pump 111; the bottom of the sodium separation mother liquor tank 112 is also communicated with the forced circulation heat exchanger 110 through a sodium separation mother liquor pump 111 and a forced circulation pump 109; the material which generates certain sodium chloride crystals in the crystallization separator 117 is pumped into a sodium chloride thickener 119 through a sodium chloride discharging pump 118, then is centrifuged to discharge salt through a sodium chloride centrifuge 120, the mother liquor enters a sodium-separating mother liquor tank 112, a part of the mother liquor is pumped into a rear-end vacuum flash evaporation Oslo system 200, and a part of the mother liquor returns to a front-end MVR evaporation system 100 to carry out secondary evaporation.
The back-end vacuum flash oslo system 200 includes a cold crystallization forced circulation pump 201, a potassium eduction mother liquor tank 203, a potassium chloride centrifuge 204, an oslo crystallizer 205, and a coagulation vessel 208. The upper part of the coagulation vessel 208 is also connected with a potassium chloride vacuum pump 210, and the steam ejector 207 condenses in the coagulation vessel 208 by steam ejection.
A circulation loop is formed between the cold crystallization forced circulation pump 201 and the Oslo crystallizer 205, the top of the Oslo crystallizer 205 is communicated with the bottom of the condenser 208, and a steam ejector 207 is arranged between the Oslo crystallizer 205 and the condenser 208; the bottom of the Oslo crystallizer 205 is communicated with a potassium chloride thickener 209 through a potassium chloride discharge pump 206, the potassium chloride thickener 209 is connected with a potassium chloride centrifuge 204, and the potassium chloride centrifuge 204 is communicated with a potassium separation mother liquor tank 203; the bottom of the potassium analysis mother liquor tank 203 is communicated with the MVR evaporation system 100.
The potassium chloride vacuum pump 210 pumps air to enable low negative pressure to be formed inside the oslo crystallizer 205, the saturated potassium chloride solution is circulated through the axial pushing of the cold crystallization forced circulation pump 201, the potassium chloride solution is flashed and cooled in the oslo crystallizer 205 to form a cooling circulation of materials, and potassium chloride crystals are formed and grow. The circulating material is crystallized and grown in the Oslo crystallizer 205, large-particle crystals are settled at the bottom of the Oslo crystallizer 205, and most of small-particle crystals float on the upper side of the Oslo crystallizer 205; the bottom of the oslo crystallizer 205 is respectively used for detecting the flow and density of the material concentrated solution by a flow detector and a density detector, and the discharged material concentration is judged by detecting the densities corresponding to different particle sizes; the bottom of the Oslo crystallizer 205 is provided with a crystal discharge port which is connected with a potassium chloride discharge pump 206, and a potassium chloride thickener 209 and a potassium chloride centrifuge 204 are connected through a cold insulation pipeline in sequence. The bottom of the oslo crystallizer 205 is in a special circular arc shape, which improves the flowing state of the feed liquid in the oslo crystallizer 205 and prevents the formation of dead zones.
The motor of the forced cold crystallization circulating pump 201 is an adjustable motor, and the flow of the circulating pump is adjusted by adjusting the rotating speed of the motor, so that the particle size of salt crystals in the circulating liquid and the crystallization amount of the discharged salt crystals are adjusted. Because the diameter of the oslo crystallizer 205 is larger, an upright guide cylinder is arranged in the center of the oslo crystallizer 205, the diameter of the guide cylinder is about 1/8-1/5 of the diameter of the oslo crystallizer 205, a gap is arranged between the guide cylinder and the bottom wall of the oslo crystallizer 205, and the material flows downwards through the guide cylinder and gradually rises along the outer wall of the guide cylinder.
The upper side of the side wall of the oslo crystallizer 205 is provided with a circulating outlet, the circulating outlet is connected with the inlet of the cold crystallization forced circulation pump 201 through a cold insulation pipeline, and the mother liquor and the small-particle crystals floating on the upper side of the cold crystallization forced circulation pump 201 flow out of the cold crystallization forced circulation pump 201 from the circulating outlet and enter the cold crystallization forced circulation pump 201. Therefore, the circulation outlet can discharge the mother liquor to control the salt crystal content in the crystallization separator, and can also discharge some fine salt crystals to keep the crystal nucleus in the Oslo crystallizer 205 relatively stable, which is beneficial to keeping the crystal grain uniform.
The oslo crystallizer 205 includes an upper section, a middle section, and a lower section, and the diameters of the upper section, the middle section, and the lower section decrease from top to bottom in sequence. The residence time of the feed liquid in the crystallization separator 117 and the cold insulation pipeline affects the particle size of the crystals and the production capacity of the equipment, and the residence time of the feed liquid has a great relationship with the size of the equipment, so that the residence time of the feed liquid is controlled by reasonably controlling the length of the Oslo crystallizer 205 to control the particle size of the discharged salt.
The utility model discloses a working method:
in this embodiment, the specific operation steps are as follows:
1) the compressor 115 supplies heat to the forced circulation heat exchanger 110, the raw material pump 102 inputs the raw material into the MVR evaporation system 100, and the forced circulation pump 109, the forced circulation heat exchanger 110 and the crystallization separator 117 are sequentially connected to form evaporation concentration circulation of the material;
2) a flow detector and a density detector at the bottom of the crystallization separator 117 detect the flow and the density of the material concentrated solution;
3) when the concentrated solution of the materials reaches the required concentration ratio, the materials are discharged, the concentrated solution containing crystals is sent to a sodium chloride thickener 119 through a sodium chloride discharge pump 118, and then separated and crystallized through a sodium chloride centrifuge 120 to separate out sodium chloride salt; transferring the potassium chloride mother liquor rich in saturated concentration into a vacuum flash evaporation Oslo system 200;
4) through the vacuum combination of the steam ejector 207 and the potassium chloride vacuum pump 210, the potassium chloride solution is flashed and cooled in the Oslo crystallizer 205, and the potassium chloride is cooled and crystals grow in the Oslo crystallizer 205;
5) then detecting the flow and density of the material concentrated solution by a flow detector and a density detector at the bottom of the Oslo crystallizer 205, and starting discharging when the concentrated solution of the material reaches the required concentration ratio;
6) the concentrated solution containing the crystals is sent to a potassium chloride thickener 209 by a potassium chloride discharge pump 206, and then separated and crystallized by a potassium chloride centrifuge 204, and the potassium chloride salt is separated out and leaves the system.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. A control system for improving the grain size of potassium chloride in potassium-sodium separation comprises a front-end MVR evaporation system (100) for evaporating and separating out sodium chloride and a rear-end vacuum flash evaporation Oslo system (200) for cooling and separating out potassium chloride crystals; the method is characterized in that: the MVR evaporation system (100) is communicated with the vacuum flash Oslo system (200).
2. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 1, characterized in that: the MVR evaporation system (100) comprises a raw liquid tank (101), a distilled water preheater (103), a steam preheater (105), a forced circulation pump (109), a forced circulation heat exchanger (110), a sodium precipitation mother liquid tank (112), a crystallization separator (117), a sodium chloride thickener (119) and a sodium chloride centrifuge (120); the raw material tank (101) is connected with the distilled water preheater (103) through a raw material pump (102), the distilled water preheater (103) is communicated with the steam preheater (105), and the steam preheater (105) is connected with a forced circulation heat exchanger (110) through a forced circulation pump (109); the top of the forced circulation heat exchanger (110) is communicated with a crystallization separator (117), the bottom of the crystallization separator (117) is communicated with the top of a sodium chloride thickener (119) through a sodium chloride discharge pump (118), the bottom of the sodium chloride thickener (119) is communicated with a sodium chloride centrifuge (120), and the sodium chloride centrifuge (120) is communicated with a sodium precipitation mother liquor tank (112); the bottom of the sodium-separating mother liquor tank (112) is communicated with a vacuum flash Oslo system (200) through a sodium-separating mother liquor pump (111), and the bottom of the sodium-separating mother liquor tank (112) is also communicated with a forced circulation heat exchanger (110) through the sodium-separating mother liquor pump (111) and a forced circulation pump (109).
3. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 2, is characterized in that: the crystallization separator (117) is communicated with the forced circulation pump (109); wherein the forced circulation pump (109), the forced circulation heat exchanger (110) and the crystallization separator (117) form a circulation path.
4. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 2, is characterized in that: the top of the crystallization separator (117) is communicated with a secondary separator (116), the secondary separator (116) is respectively communicated with a liquid accumulation tank (108) and a compressor (115), and the compressor (115) is communicated with the liquid accumulation tank (108); the liquid accumulation tank (108) is communicated with the distilled water tank (106) through a liquid accumulation pump (107), the bottom of the distilled water tank (106) is communicated with the distilled water preheater (103) through a distilled water pump (104), the top of the distilled water tank (106) is also respectively communicated with the steam preheater (105) and the forced circulation heat exchanger (110), and the forced circulation heat exchanger (110) is communicated with the vacuum pump (113) through a vacuum pump cooler (114).
5. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 1, characterized in that: the vacuum flash Oslo system (200) comprises a cold crystallization forced circulation pump (201), a potassium precipitation mother liquor tank (203), a potassium chloride centrifuge (204), an Oslo crystallizer (205) and a coagulation device (208); a circulation loop is formed between the cold crystallization forced circulation pump (201) and the Oslo crystallizer (205), the top of the Oslo crystallizer (205) is communicated with the bottom of the condenser (208), and a steam ejector (207) is arranged between the Oslo crystallizer (205) and the condenser (208); the bottom of the Oslo crystallizer (205) is communicated with a potassium chloride thickener (209) through a potassium chloride discharge pump (206), the potassium chloride thickener (209) is connected with a potassium chloride centrifuge (204), and the potassium chloride centrifuge (204) is communicated with a potassium precipitation mother liquor tank (203); the bottom of the potassium analysis mother liquor tank (203) is communicated with an MVR evaporation system (100).
6. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 5, wherein: the upper part of the potassium chloride thickener (209) is also directly communicated with a potassium analysis mother liquor tank (203), and the bottom of the potassium analysis mother liquor tank (203) is communicated with the bottom of a forced circulation heat exchanger (110) of the MVR evaporation system through a potassium analysis mother liquor pump (202); a circulation loop is also formed between the potassium separation mother liquor pump (202) and the potassium separation mother liquor tank (203).
7. The control system for increasing the particle size of potassium chloride in potassium-sodium separation according to claim 5, wherein: the upper part of the coagulation device (208) is also connected with a potassium chloride vacuum pump (210).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477591A (en) * | 2022-02-08 | 2022-05-13 | 青岛康景辉环境科技集团有限公司 | Sodium chloride and potassium chloride high-concentration wastewater salt separation process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114477591A (en) * | 2022-02-08 | 2022-05-13 | 青岛康景辉环境科技集团有限公司 | Sodium chloride and potassium chloride high-concentration wastewater salt separation process |
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