CN112520930A - Device and method for improving particle size distribution of chemical strong brine byproduct crystalline salt - Google Patents
Device and method for improving particle size distribution of chemical strong brine byproduct crystalline salt Download PDFInfo
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Abstract
The invention discloses a device and a method for improving the particle size distribution of chemical strong brine by-product crystal salt. By the device and the method, the ratio of large-particle-size salt in the byproduct industrial salt can be improved, the ratio of powder salt can be obviously reduced by 20-30%, and the particle size distribution is more uniform.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a device and a method for improving particle size distribution of chemical strong brine by-product crystal salt.
Background
The high-salinity wastewater refers to wastewater with the total salt content of not less than 1%, and chemical strong brine is inevitably generated in the production process of the current chemical industry, such as sodium hypochlorite wastewater generated in the production process of polyvinyl alcohol, concentrated water generated after membrane treatment of a sewage treatment plant and the like. High-concentration brine in the chemical industry is generally directly discharged as clean sewage, and along with the increasing strictness of environmental protection policies in recent years, the standard discharge of the high-concentration brine in the chemical industry is required to be far from insufficient, and the high-concentration brine is recycled to the maximum extent. The most effective method for treating the brine-containing concentrated water at present is an evaporative crystallization technology, and the method mainly utilizes temperature difference to vaporize and remove water in a solvent, so that favorable conditions are provided for solute precipitation. However, in the existing salt crystallization process, the product quality is difficult to control, the particle size distribution of the salt is uneven, the content of the powdery salt in the byproduct salt is high, and the product quality of the byproduct industrial salt is seriously influenced.
Disclosure of Invention
In order to solve the problems of uneven particle size distribution and more powder salt of the byproduct salt, the invention provides a device and a method for improving the particle size distribution of the byproduct crystalline salt of the chemical strong brine, and aims to improve the proportion of large-particle-size salt in the byproduct crystalline salt and make the particle size distribution more uniform.
In order to solve the technical problem, the invention adopts the following technical scheme:
the invention firstly discloses a device for improving the particle size distribution of chemical strong brine byproduct crystalline salt, which is characterized in that: comprises a charging barrel, a heat exchanger, a circulating heater, a multi-effect evaporation system, a steam system, a balance barrel, a circulating pump, a vacuum device, a discharge pump, a cyclone, a centrifuge, a drying bed, a packaging machine, a mother liquor barrel and an end-effect condenser.
Further: the discharge hole of the feed barrel is connected to the feed hole of the heat exchanger; a discharge hole of the heat exchanger is connected to a material inlet at the bottom of the circulating heater through a circulating pump; a steam inlet at the upper part of the circulating heater is connected with the steam system, and a steam condensate outlet at the lower part of the circulating heater is connected with a steam condensate inlet of the balance barrel; the balance barrel is also provided with a gas phase outlet which is connected to a steam reflux port in the middle of the circulating heater; a material outlet at the top of the circulating heater is connected to a material inlet of the multi-effect evaporation system; an outlet of a circulating pipe at the lower part of the multi-effect evaporation system is connected to a material inlet at the bottom of the circulating heater through a circulating pump; a crystallized salt discharge pipe at the bottom of the multi-effect evaporation system is connected to a material inlet of the cyclone through a discharge pump; a steam pipe outlet at the top of the multi-effect evaporation system is connected to a steam inlet of a final-effect condenser, and a steam outlet of the final-effect condenser is connected with a vacuum device; the material outlet of the cyclone is connected to the material inlet of the centrifuge; the liquid phase outlet of the centrifuge is connected to the feeding barrel, the solid phase outlet is connected to the material inlet of the drying bed, and the material outlet of the drying bed is connected to the packaging machine.
Furthermore, the position of a steam condensate outlet of the circulating heater is higher than the liquid level height in the balance barrel, so that condensate generated by heat exchange can overcome pipeline resistance and be smoothly discharged to the balance barrel.
Furthermore, the outlet of the circulating pipe at the lower part of the multi-effect evaporation system is also connected with a mother liquid barrel.
Furthermore, the inside of the circulating heater is of a tubular structure, and the steam provided by the steam system is uniformly distributed on the outer wall of each heating tubular column, so that the steam is promoted to fully exchange heat with the heated material through the heating pipe.
Further, the multi-effect evaporation system comprises a first-effect evaporator, a second-effect evaporator and a last-effect evaporator.
Further, an observation window is arranged on the crystallized salt discharge pipe and used for observing the salt level.
The invention also discloses a method for improving the grain size distribution of the chemical strong brine byproduct crystalline salt, which is implemented by utilizing the device according to the following steps:
Chemical strong brine generated in the production process is cached in a feed barrel and then added into a heat exchanger for preheating treatment;
Uniformly circulating steam provided by the preheated material in a heater, and carrying out partition wall heat exchange on the material and saturated steam provided by a steam system;
the heat supply source of the circulating heater is steam provided by a steam system, condensed water generated after steam heat exchange is directly discharged into the balance barrel, a vapor phase part carried by the condensed water entering the balance barrel returns to the circulating heater 3) through the balance pipe, and the steam pressure balance is kept;
step 3, crystallization separation
Feeding the circularly heated material into a multi-effect evaporation system for boiling evaporation, discharging steam generated by evaporation of the material liquid to a final-effect condenser from an outlet of a steam pipe at the top of the steam pipe, performing non-contact heat exchange with condensed water in a row pipe of the final-effect condenser, and pumping the rest material liquid to a circulating heater for circulation through a circulating pump along an outlet of a circulating loop pipe;
When the Baume degree of the feed liquid in the last effect evaporator of the multi-effect evaporation system meets the requirement, a crystallized salt discharge pipe at the bottom of the multi-effect evaporation system starts to discharge, and slurry containing crystallized salt is conveyed to a cyclone through a discharge pump; in the cyclone, the concentration of the slurry is increased by utilizing the centrifugal sedimentation principle;
After thickening, the solid-liquid mixture enters a centrifuge, solid-liquid separation is carried out under centrifugal action force, the obtained liquid enters a feed barrel for circular treatment, and the obtained solid is wet crystalline salt;
And (4) drying the obtained wet crystalline salt in a drying bed, and conveying the dried solid granular crystalline salt into a packaging machine to finish packaging treatment.
Further, in the step 1, the temperature of the material preheated by the heat exchanger is 70-75 ℃; in the step 2, the temperature of the material heated by the circulating heater is 80-90 ℃.
Further, the multi-effect evaporation system comprises a first-effect evaporator, a second-effect evaporator and a last-effect evaporator;
firstly, feeding the circularly heated material into a first-effect evaporator, and performing wall-dividing type heat exchange with raw steam with the pressure of 0.09-0.12 MPa and the temperature of 118 +/-1 ℃ to ensure that the temperature of the material reaches 80-90 ℃, so that the material is evaporated and concentrated, and the generated steam is used as heating steam of a second-effect evaporator;
then, the liquid evaporated and concentrated by the first-effect evaporator enters a second-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and concentrated again, the salt content is concentrated to 8.7-9%, and the generated steam is used as the heating steam of the last-effect evaporator;
and finally, the liquid evaporated and concentrated by the second-effect evaporator enters a last-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and crystallized again, the generated crystallized salt enters a crystallized salt discharge pipe, the steam in the last-effect evaporator is discharged to a last-effect condenser from a steam pipe outlet at the top, and the temperature of condensed water in the last-effect condenser is not higher than 35 ℃.
Further, in the step 4, the solid phase mass content of the solid-liquid mixture after being thickened by the cyclone is 35-45%.
Further, in the step 4, the Baume degree of the material liquid in the last effect evaporator of the multi-effect evaporation system is required to be 14-16% of the material liquid concentration.
Compared with the prior art, the invention has the beneficial effects that:
the device and the method can realize the stable treatment of chemical strong brine with different concentrations, the multistage evaporator is arranged, the material level and the temperature in the evaporator are strictly controlled by controlling the material inlet and outlet quantity and the evaporation quantity, the material in the evaporator is ensured to be in a stable range, the solution is effectively controlled in the supersaturation degree, the formation of particles of crystallized salt is ensured, the problems of uneven particle size distribution and more powder salt of the existing byproduct salt are solved, the proportion of large-particle-size salt in the byproduct industrial salt is improved, the proportion of powder salt is obviously reduced by 20-30%, and the particle size distribution is more uniform.
Drawings
FIG. 1 is a device for improving the particle size distribution of chemical strong brine by-product crystal salt, wherein the reference numbers in the figure are as follows: 1-a charging barrel; 2-a heat exchanger; 3-a circulating heater; 4-a multi-effect evaporation system; 41-crystallized salt discharge pipe; 5-a steam system; 6-a balance barrel; 7-a circulating pump; 8-vacuum device; 9-a discharge pump; 10-a cyclone; 11-a centrifuge; 12-drying the bed; 13-packaging machine; 14-mother liquor barrel; 15-final effect condenser.
Detailed Description
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in detail below. The following disclosure is merely exemplary and illustrative of the inventive concept, and those skilled in the art will appreciate that various modifications, additions and substitutions are possible, without departing from the scope and spirit of the invention as disclosed in the accompanying claims.
As shown in fig. 1, the apparatus for improving the particle size distribution of chemical strong brine by-product crystallized salt in the embodiment includes a feed barrel 1, a heat exchanger 2, a circulation heater 3, a multi-effect evaporation system 4, a steam system 5, a balance barrel 6, a circulation pump 7, a vacuum device 8, a discharge pump 9, a cyclone 10, a centrifuge 11, a drying bed 12, a packing machine 13, a mother liquor barrel 14 and an end-effect condenser 15.
All the parts are connected through pipelines. The discharge hole of the feed barrel 1 is connected to the feed hole of the heat exchanger 2; the discharge port of the heat exchanger 2 is connected to the material inlet at the bottom of the circulation heater 3 through a circulation pump 7. A steam inlet at the upper part of the circulating heater 3 is connected with a steam system 5, and a steam condensate outlet at the lower part is connected with a steam condensate inlet of the balance barrel 6; the balance barrel 6 is also provided with a gas phase outlet which is connected to a steam return port in the middle of the circulation heater 3. A material outlet at the top of the circulating heater 3 is connected to a material inlet of the multi-effect evaporation system 4; the outlet of the circulating pipe at the lower part of the multi-effect evaporation system 4 is connected to the material inlet at the bottom of the circulating heater 3 through a circulating pump 7; a crystallized salt discharge pipe 41 at the bottom of the multi-effect evaporation system 4 is connected to a material inlet of the cyclone 10 through a discharge pump 9; the steam pipe outlet at the top of the multi-effect evaporation system 4 is connected to the steam inlet of the last-effect condenser 15, and the steam outlet of the last-effect condenser 15 is connected with the vacuum device 8, so that the evaporated gas is ensured to enter the condenser. The material outlet of the cyclone 10 is connected to the material inlet of the centrifuge 11; the liquid phase outlet of the centrifuge 11 is connected to the feed barrel 1, the solid phase outlet is connected to the material inlet of the bed dryer 12, and the material outlet of the bed dryer 12 is connected to the packaging machine 13.
Specifically, the steam condensate outlet of the circulating heater 3 is higher than the liquid level in the balance barrel 6, so that the condensate generated by heat exchange can overcome the resistance of the pipeline and be smoothly discharged to the balance barrel.
Specifically, the outlet of the circulating pipe at the lower part of the multi-effect evaporation system 4 is also connected with a mother liquid barrel 14.
Specifically, the inside of the circulating heater 3 is of a tubular structure, and steam provided by the steam system is uniformly distributed on the outer wall of each heating tubular column, so that the steam is promoted to fully exchange heat with the heated material through the heating pipe.
Specifically, the multi-effect evaporation system 4 includes a one-effect evaporator, a two-effect evaporator, and a last-effect evaporator.
Specifically, an observation window is provided on the crystallized salt discharge pipe 41 for observing the salt level.
The method for improving the particle size distribution of the chemical strong brine byproduct crystalline salt by using the device is carried out according to the following steps:
Chemical strong brine generated in the production process is cached in the feed barrel 1 and then added into the heat exchanger 2 for preheating treatment, the temperature of the material preheated by the heat exchanger is 70-75 ℃, the material temperature is prevented from being too low, and the preheating mode is that the preheating treatment is carried out in a dividing wall type heat exchange mode with steam.
Adding the preheated material into a circulating heater 3 from bottom to top, carrying out partition wall heat exchange on the material and saturated steam provided by a steam system 5, and controlling the temperature of the material heated by the circulating heater 3 to be 80-90 ℃;
the heat supply source of the circulating heater 3 is steam provided by a steam system 5, condensed water generated after steam heat exchange is directly discharged into the balance barrel 6, a vapor phase part carried by the condensed water entering the balance barrel 6 returns into the circulating heater 3 through a balance pipe, and the steam pressure balance is kept.
Step 3, crystallization separation
The material after the cyclic heating is sent into a multi-effect evaporation system 4 for boiling evaporation, steam generated by the evaporation of the material liquid is discharged to a final-effect condenser 15 from a steam pipe outlet at the top, non-contact heat exchange is carried out between the steam and condensed water in a row pipe of the final-effect condenser, and the rest material liquid is sent to a cyclic heater 3 for circulation through a circulating pump 7 along a circulating pipe outlet.
When the baume degree of the material liquid in the last effect evaporator of the multi-effect evaporation system 4 meets the requirement (the baume degree of the material liquid in the last effect evaporator is required to be 14-16% of the concentration of the material liquid), a crystallized salt discharging pipe 41 at the bottom of the multi-effect evaporation system 4 starts to discharge, and slurry containing crystallized salt is sent to a swirler 10 through a discharging pump 9; in the cyclone, the centrifugal sedimentation principle is utilized to increase the concentration of the slurry, and the solid phase mass content of the solid-liquid mixture thickened by the cyclone 10 is 35-45%.
And (3) feeding the solid-liquid mixture after thickening into a centrifugal machine 11, carrying out solid-liquid separation under the centrifugal action force, feeding the obtained liquid into a feed and circulating the liquid by 1, wherein the obtained solid is wet crystalline salt.
The obtained wet crystalline salt enters a drying bed 12 for drying treatment, and the dried solid granular crystalline salt is sent to a packaging machine 13 to complete the packaging treatment.
Specifically, the multi-effect evaporation system 4 comprises a first-effect evaporator, a second-effect evaporator and a last-effect evaporator;
firstly, feeding the circularly heated material into a first-effect evaporator, and performing wall-dividing type heat exchange with raw steam with the pressure of 0.09-0.12 MPa and the temperature of 118 +/-1 ℃ to ensure that the temperature of the material reaches 80-90 ℃, so that the material is evaporated and concentrated, and the generated steam is used as heating steam of a second-effect evaporator;
then, the liquid evaporated and concentrated by the first-effect evaporator enters a second-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and concentrated again, the salt content is concentrated to 8.7-9%, and the generated steam is used as the heating steam of the last-effect evaporator;
and finally, the liquid evaporated and concentrated by the second-effect evaporator enters a last-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and crystallized again, the generated crystallized salt enters a crystallized salt discharge pipe 41, the steam in the last-effect evaporator is discharged to a last-effect condenser 15 from a steam pipe outlet at the top, and the temperature of condensed water in the last-effect condenser is not higher than 35 ℃.
When impurities exist on the upper layer of the material in the last-effect evaporator, the upper layer liquid is discharged into the mother liquid barrel 14 for recycling.
Tests show that after the crystal salt is treated by the device and the method, the obtained crystal salt has the purity of sodium chloride of more than 98.99 percent, the whiteness of not less than 81.4 degrees, the calcium and magnesium ions of less than 0.0095 percent and the sulfate radical of not more than 0.007 percent, and has uniform particle size and the powder salt content of 20-30 percent.
The present invention is not limited to the above exemplary embodiments, and any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (11)
1. The utility model provides an improve device of chemical industry strong brine by-product crystal salt particle size distribution which characterized in that: the device comprises a feed barrel (1), a heat exchanger (2), a circulating heater (3), a multi-effect evaporation system (4), a steam system (5), a balance barrel (6), a circulating pump (7), a vacuum device (8), a discharge pump (9), a cyclone (10), a centrifugal machine (11), a drying bed (12), a packing machine (13), a mother liquor barrel (14) and an end-effect condenser (15).
2. The apparatus of claim 1, wherein:
the discharge hole of the feed barrel (1) is connected to the feed hole of the heat exchanger (2); a discharge hole of the heat exchanger (2) is connected to a material inlet at the bottom of the circulating heater (3) through a circulating pump (7);
a steam inlet at the upper part of the circulating heater (3) is connected with the steam system (5), and a steam condensate outlet at the lower part of the circulating heater is connected with a steam condensate inlet of the balance barrel (6); the balance barrel (6) is also provided with a gas phase outlet which is connected to a steam return port in the middle of the circulating heater (3);
a material outlet at the top of the circulating heater (3) is connected to a material inlet of the multi-effect evaporation system (4); an outlet of a circulating pipe at the lower part of the multi-effect evaporation system (4) is connected to a material inlet at the bottom of the circulating heater (3) through a circulating pump (7); a crystallized salt discharge pipe (41) at the bottom of the multi-effect evaporation system (4) is connected to a material inlet of the cyclone (10) through a discharge pump (9); a steam pipe outlet at the top of the multi-effect evaporation system (4) is connected to a steam inlet of a final-effect condenser (15), and a steam outlet of the final-effect condenser (15) is connected with a vacuum device (8);
the material outlet of the cyclone (10) is connected to the material inlet of the centrifuge (11); the liquid phase outlet of the centrifuge (11) is connected to the feed drum (1), the solid phase outlet is connected to the material inlet of the drying bed (12), and the material outlet of the drying bed (12) is connected to the packaging machine (13).
3. The apparatus of claim 2, wherein: the position of a steam condensate outlet of the circulating heater (3) is higher than the liquid level height in the balance barrel (6).
4. The apparatus of claim 2, wherein: the outlet of the circulating pipe at the lower part of the multi-effect evaporation system (4) is also connected with a mother liquid barrel (14).
5. The apparatus of claim 2, wherein: the interior of the circulating heater (3) is of a tubular structure.
6. The apparatus of claim 2, wherein: the multi-effect evaporation system (4) comprises a first-effect evaporator, a second-effect evaporator and a last-effect evaporator.
7. A method for improving the particle size distribution of chemical strong brine by-product crystal salt is characterized in that the device of any one of claims 1 to 6 is used, and the method comprises the following steps:
step 1, preheating materials
Chemical strong brine generated in the production process is cached in a feed barrel (1) and then is added into a heat exchanger (2) for preheating treatment;
step 2, cyclic heating
Adding the preheated materials into a circulating heater (3) from bottom to top, and carrying out partition wall heat exchange on the materials and saturated steam provided by a steam system (5);
the heat supply source of the circulating heater (3) is steam provided by a steam system (5), condensed water generated after steam heat exchange is directly discharged into a balance barrel (6), a vapor phase part carried by the condensed water entering the balance barrel (6) returns into the circulating heater (3) through a balance pipe, and the vapor pressure balance is kept;
step 3, crystallization separation
The material after cyclic heating is sent into a multi-effect evaporation system (4) for boiling evaporation, steam generated by the evaporation of the material liquid is discharged to a final-effect condenser (15) from a steam pipe outlet at the top, non-contact heat exchange is carried out between the steam and condensed water in a row pipe of the final-effect condenser, and the rest material liquid is sent to a cyclic heater (3) for circulation through a circulating pump (7) along a circulating pipe outlet;
step 4, thickening the feed liquid
When the Baume degree of the feed liquid in the last effect evaporator of the multi-effect evaporation system (4) meets the requirement, a crystallized salt discharge pipe (41) at the bottom of the multi-effect evaporation system (4) starts to discharge, and slurry containing crystallized salt is conveyed to a cyclone (10) through a discharge pump (9); in the cyclone, the concentration of the slurry is increased by utilizing the centrifugal sedimentation principle;
step 5, separating mother liquor
After thickening, the solid-liquid mixture enters a centrifugal machine (11), solid-liquid separation is carried out under the centrifugal action force, the obtained liquid enters a feed barrel (1) for circular treatment, and the obtained solid is wet crystalline salt;
step 6, drying and packaging
The obtained wet crystalline salt enters a drying bed (12) for drying treatment, and the dried solid granular crystalline salt is sent to a packaging machine (13) to complete the packaging treatment.
8. The method of claim 7, wherein: in the step 1, the temperature of the material preheated by the heat exchanger is 70-75 ℃; in the step 2, the temperature of the material heated by the circulating heater (3) is 80-90 ℃.
9. The method of claim 7, wherein: the multi-effect evaporation system (4) comprises a first-effect evaporator, a second-effect evaporator and a last-effect evaporator;
firstly, feeding the circularly heated material into a first-effect evaporator, and performing wall-dividing type heat exchange with raw steam with the pressure of 0.09-0.12 MPa and the temperature of 118 +/-1 ℃ to ensure that the temperature of the material reaches 80-90 ℃, so that the material is evaporated and concentrated, and the generated steam is used as heating steam of a second-effect evaporator;
then, the liquid evaporated and concentrated by the first-effect evaporator enters a second-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and concentrated again, the salt content is concentrated to 8.7-9%, and the generated steam is used as the heating steam of the last-effect evaporator;
and finally, the liquid evaporated and concentrated by the second-effect evaporator enters a last-effect evaporator to perform wall-dividing heat exchange with heating steam, so that the material is evaporated and crystallized again, the generated crystallized salt enters a crystallized salt discharge pipe (41), the steam in the last-effect evaporator is discharged to a last-effect condenser (15) from a steam pipe outlet at the top, and the temperature of condensed water in the last-effect condenser is not higher than 35 ℃.
10. The method of claim 7, wherein: in the step 4, the solid phase mass content of the solid-liquid mixture after being thickened by the cyclone (10) is 35-45%.
11. The method of claim 7, wherein: in the step 4, the Baume degree of the material liquid in the last effect evaporator of the multi-effect evaporation system (4) is required to be 14-16% of the material liquid concentration.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011510692.6A CN112520930A (en) | 2020-12-18 | 2020-12-18 | Device and method for improving particle size distribution of chemical strong brine byproduct crystalline salt |
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| CN202011510692.6A CN112520930A (en) | 2020-12-18 | 2020-12-18 | Device and method for improving particle size distribution of chemical strong brine byproduct crystalline salt |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113307435A (en) * | 2021-05-25 | 2021-08-27 | 中煤能源研究院有限责任公司 | Dynamic PCA (principal component analysis) -based evaporative crystallization solid-liquid separation system and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113307435A (en) * | 2021-05-25 | 2021-08-27 | 中煤能源研究院有限责任公司 | Dynamic PCA (principal component analysis) -based evaporative crystallization solid-liquid separation system and method |
| CN113307435B (en) * | 2021-05-25 | 2022-12-13 | 中煤能源研究院有限责任公司 | Dynamic PCA (principal component analysis) -based evaporative crystallization solid-liquid separation system and method |
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