CN219595902U - Improved oslo continuous crystallizer - Google Patents
Improved oslo continuous crystallizer Download PDFInfo
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- CN219595902U CN219595902U CN202222712610.7U CN202222712610U CN219595902U CN 219595902 U CN219595902 U CN 219595902U CN 202222712610 U CN202222712610 U CN 202222712610U CN 219595902 U CN219595902 U CN 219595902U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
An improved Austrian continuous crystallizer comprises a gas-liquid separator 9, a crystal sedimentation separator 16, a heat exchanger 10, a heat exchange circulating pump 15, an Austrian crystallization circulating pump 17 and a stock solution inlet pipe 29; the gas-liquid separator 9 is provided with a blanking pipe 7, a gas discharge pipe 5 and a circulating liquid inlet pipe 6; the crystal separator 16 is provided with a feed liquid inlet pipe 18, an overflow liquid outlet pipe 42, a central blanking pipe 43 and an underflow outlet pipe 20. The utility model separates the gas-liquid separator at the upper part of the oslo sedimentation separator and the crystal sedimentation separator at the lower part into two parts, the gas-liquid separator at the upper part is changed into a circulation transfer station, the crystal sedimentation separator at the lower part is changed into a crystal sedimentation separation small tank, thereby not only meeting the design requirements of normal production process, greatly reducing the volume and the height of the crystal sedimentation separation tank, but also saving equipment and factory investment.
Description
Technical Field
The utility model relates to the technical field of inorganic salt wastewater treatment, in particular to an improved oslo continuous crystallizer.
Background
The Austrian continuous crystallization system is widely applied to industries such as chemical wet smelting, environmental protection wastewater treatment and the like in China, and the structure of the existing Austrian crystallization system is shown as a figure 1, and consists of a gas-liquid separator 1, a crystal sedimentation separator 2, a heat exchanger 3 and a circulating pump 4. The Oslo crystallization system has the main advantages of continuous and rapid heat exchange, uniform crystal growth, large productivity, small occupied area and the like.
In the crystallization separation process (such as evaporation crystallization separation of sodium chloride or potassium chloride wastewater), the inorganic salt in the wastewater is crystallized and separated in a crystallization system by adopting the means of evaporation crystallization or cooling crystallization (utilizing the characteristic that the inorganic salt has different solubility at temperature) generally.
When the capacity is particularly large, the heat exchange area of the heat exchanger is too large when equipment is designed, the number of the heat exchange tubes is large, the flow rate of liquid in the heat exchange tubes needs to be controlled within a certain range when forced circulation heat exchange is carried out according to the design requirement, so that the requirement of the flow rate in the tubes is met by large circulation quantity, and after the circulation quantity is large, the rising speed of the liquid in the tank needs to be controlled within a certain range, so that the diameter of the Austrian crystal sedimentation separator needs to be increased, on-site manufacturing is needed (the volume of the crystal sedimentation separator is too large and the transportation is inconvenient), the manufacturing cost is high, the factory building is high, and the basic construction investment is increased. Moreover, the oslo sedimentation separator has large volume, the hydrodynamic state is not easy to control, and the phenomena of crystal sinking, pipeline blockage and the like are easy to occur, so that the production cannot be carried out normally.
Disclosure of Invention
The utility model aims to provide an improved oslo continuous crystallizer, which solves the problems of high equipment investment, large equipment occupation area, high production cost, low equipment integration degree and low practicality in the background technology.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
an improved oslo continuous crystallizer comprises a gas-liquid separator, a crystal sedimentation separator, a heat exchanger, a heat exchange circulating pump, an oslo crystallization circulating pump and a stock solution inlet pipe;
the gas-liquid separator is connected with the circulating liquid inlet pipe, the feed liquid circulating pipe, the heat exchanger, the heat exchange circulating pump, the connecting pipe, the blanking pipe and the pipeline to form a heat exchange circulating loop, and part of circulating liquid in the blanking pipe enters the heat exchange circulating loop;
the crystal sedimentation separator is provided with a feed liquid inlet pipe, an overflow liquid outlet pipe, a central blanking pipe and an underflow outlet pipe, the central blanking pipe is arranged in the crystal sedimentation separator and is connected with the feed liquid inlet pipe, the feed liquid inlet pipe is connected with the lower part of the blanking pipe on the gas-liquid separator through an oslo crystallization circulating pump and a connecting pipe, and part of circulating liquid in the blanking pipe enters the crystal sedimentation separator; the crystal sedimentation separator is connected with the overflow liquid return pipe through a feed liquid inlet pipe, an Oldham crystallization circulating pump, a connecting pipe and the overflow liquid return pipe, and the crystal sedimentation separator is used for enabling crystal slurry generated in heat exchange to be pumped into the crystal sedimentation separator through the Oldham crystallization circulating pump to carry out crystal sedimentation and be separated from liquid (solid-liquid separation); the overflow liquid outlet pipe is connected with the heat exchange circulation loop through an overflow liquid return pipe and a valve, so that supernatant liquid flows back into the heat exchange circulation loop;
the heat exchanger is provided with a feed pipe, a discharge pipe, a heat exchange medium inlet pipe and a heat exchange medium outlet pipe;
one end of the stock solution inlet pipe is connected with the heat exchange circulation loop, and the other end is connected with the stock solution pond.
The utility model further adopts the technical scheme that: the gas discharge pipe on the gas-liquid separator enters other equipment through a pipeline for reuse.
The utility model further adopts the technical scheme that: the underflow outlet pipe on the crystal sedimentation separator goes to the centrifuge.
The utility model further adopts the technical scheme that: the stock solution inlet pipe is arranged on the gas-liquid separator.
The utility model further adopts the technical scheme that: the flow rate of the oslo crystallization circulation pump is smaller than the flow rate of the evaporation circulation pump.
Compared with the prior art, the utility model reduces the occupied area of equipment, reduces the height of a factory building, greatly reduces the equipment investment, thereby reducing the production cost, and has high integration degree and strong practicability.
Drawings
FIG. 1 is a schematic diagram of a conventional Oslo crystallization system;
fig. 2 is a schematic structural view of the present utility model.
In the figure: the gas-liquid separator 1, the crystal sedimentation separator 2, the heat exchanger 3, the circulating pump 4, the gas discharge pipe 5, the circulating liquid inlet pipe 6, the blanking pipe 7, the gas-liquid separator 9, the heat exchanger 10, the feed pipe 11, the discharge pipe 12, the heat exchange medium inlet pipe 13, the heat exchange medium outlet pipe 14, the heat exchange circulating pump 15, the crystal sedimentation separator 16, the oslo crystallization circulating pump 17, the feed liquid inlet pipe 18, the underflow outlet pipe 20, the connecting pipe 26, the raw liquid inlet pipe 29, the feed liquid circulating pipe 36, the overflow liquid outlet pipe 42, the central blanking pipe 43 and the overflow liquid return pipe 50.
Detailed Description
The technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments of the present utility model, and all other embodiments obtained by those skilled in the art without making any inventive effort based on the embodiments of the present utility model are within the scope of protection of the present utility model.
Examples
As shown in fig. 2, an improved oslo continuous crystallizer comprises a gas-liquid separator 9, a crystal sedimentation separator 16, a heat exchanger 10, a heat exchange circulating pump 15, an oslo crystallization circulating pump 17 and a raw liquid inlet pipe 29.
The gas-liquid separator 9 is provided with a blanking pipe 7, a gas discharge pipe 5 and a circulating liquid inlet pipe 6, and the gas-liquid separator 9 is connected with the circulating liquid inlet pipe 6, a material liquid circulating pipe 36, a heat exchanger 10, a heat exchange circulating pump 15, a connecting pipe 26, the blanking pipe 7 and a pipeline to form a heat exchange circulating loop, wherein part of circulating liquid in the blanking pipe 7 enters the heat exchange circulating loop; the gas discharge pipe 5 on the gas-liquid separator 9 enters other equipment through a pipeline for reuse.
The crystal sedimentation separator 16 is provided with a feed liquid inlet pipe 18, an overflow liquid outlet pipe 42, a central blanking pipe 43 and an underflow outlet pipe 20, the central blanking pipe 43 is arranged in the crystal sedimentation separator 16 and is connected with the feed liquid inlet pipe 18, the feed liquid inlet pipe 18 is connected with the lower part of the blanking pipe 7 on the gas-liquid separator 9 through an oslo crystallization circulating pump 17 and a connecting pipe 26, and part of circulating liquid in the blanking pipe 7 enters the crystal sedimentation separator 16; the crystal sedimentation separator 16 is connected with the overflow liquid return pipe 50 through the feed liquid inlet pipe 18, the oslo crystallization circulating pump 17, the connecting pipe 26 and the overflow liquid return pipe, and the function of the crystal sedimentation separator is that crystal slurry generated in heat exchange is pumped into the crystal sedimentation separator 16 through the oslo crystallization circulating pump 17 to carry out crystal sedimentation and liquid separation (solid-liquid separation); the overflow liquid outlet pipe 42 is connected with the heat exchange circulation loop through an overflow liquid return pipe 50 and a valve, so that supernatant liquid flows back into the heat exchange circulation loop; the underflow outlet pipe 20 from the crystal sedimentation separator 16 is centrifuge removed; the flow rate of the oslo crystallization circulation pump 17 is smaller than the flow rate of the heat exchange circulation pump 15, and the ratio of the flow rate of the oslo crystallization circulation pump 17 to the flow rate of the heat exchange circulation pump 15 is preferably 1:1.1 to 200, preferably 1:2 to 100, more preferably 3 to 50, still more preferably 4 to 30, still more preferably 5 to 10.
The heat exchanger 10 is provided with a feed pipe 11, a discharge pipe 12, a heat exchange medium inlet pipe 13 and a heat exchange medium outlet pipe 14;
the stock solution inlet pipe 29 has one end provided on the gas-liquid separator 9 and the other end connected to a stock solution tank (not shown).
The utility model divides the gas-liquid separator at the upper part of the oslo sedimentation separator and the crystal sedimentation separator at the lower part into two parts, the gas-liquid separator at the upper part is changed into a circulation transfer station, the crystal sedimentation separator at the lower part is changed into a crystal sedimentation separation small tank, a circulation system is changed into two circulation from one large-flow circulation, the heat exchange system is a large-flow circulation system, the crystallization system is a small-flow circulation system, the large-flow circulation system meets the requirement of the flow velocity in the heat exchanger, the small-flow circulation system meets the requirement of the liquid rising speed in the sedimentation separation small tank, not only meets the design requirement of the normal production process, but also greatly reduces the volume and the height of the crystal sedimentation separation tank, and saves equipment and factory investment.
Claims (10)
1. An improved Austrian continuous crystallizer is characterized by comprising a gas-liquid separator, a crystal sedimentation separator, a heat exchanger, a heat exchange circulating pump, an Austrian crystallization circulating pump and a stock solution inlet pipe; the heat exchanger is provided with a feed pipe, a discharge pipe, a heat exchange medium inlet pipe and a heat exchange medium outlet pipe; one end of the stock solution inlet pipe is connected with the heat exchange circulation loop, and the other end is connected with the stock solution pond.
2. The improved oslo continuous crystallizer as claimed in claim 1, wherein: the gas-liquid separator is provided with a blanking pipe, a gas discharge pipe and a circulating liquid inlet pipe, and is connected with the circulating liquid inlet pipe, a feed liquid circulating pipe, a heat exchanger, a heat exchange circulating pump, a connecting pipe, the blanking pipe and a pipeline to form a heat exchange circulating loop, and part of circulating liquid in the blanking pipe enters the heat exchange circulating loop.
3. An improved oslo continuous crystallizer as claimed in claim 1 or 2, characterized in that: the crystal sedimentation separator is provided with a feed liquid inlet pipe, an overflow liquid outlet pipe, a central blanking pipe and an underflow outlet pipe, the central blanking pipe is arranged in the crystal sedimentation separator and is connected with the feed liquid inlet pipe, the feed liquid inlet pipe is connected with the lower part of the blanking pipe on the gas-liquid separator through an oslo crystallization circulating pump and a connecting pipe, and part of circulating liquid in the blanking pipe enters the crystal sedimentation separator; the crystal sedimentation separator is connected with the overflow liquid return pipe through a feed liquid inlet pipe, an oslo crystallization circulating pump, a connecting pipe and a liquid overflow pipe; the overflow liquid outlet pipe is connected with the heat exchange circulation loop through an overflow liquid return pipe and a valve.
4. An improved oslo continuous crystallizer as claimed in claim 1 or 2, characterized in that: the stock solution inlet pipe is arranged on the gas-liquid separator, one end of the stock solution inlet pipe is connected with the gas-liquid separator, and the other end of the stock solution inlet pipe is connected with the stock solution pool; the underflow outlet pipe on the crystal sedimentation separator goes to the centrifuge.
5. A modified oslo continuous crystallizer as claimed in claim 3, characterized in that: the stock solution inlet pipe is arranged on the gas-liquid separator, one end of the stock solution inlet pipe is connected with the gas-liquid separator, and the other end of the stock solution inlet pipe is connected with the stock solution pool; the underflow outlet pipe on the crystal sedimentation separator goes to the centrifuge.
6. An improved oslo continuous crystallizer as claimed in claim 1 or 2, characterized in that: the flow rate of the oslo crystallization circulation pump is smaller than the flow rate of the evaporation circulation pump.
7. A modified oslo continuous crystallizer as claimed in claim 3, characterized in that: the flow rate of the oslo crystallization circulation pump is smaller than the flow rate of the evaporation circulation pump.
8. The improved oslo continuous crystallizer as in claim 4, wherein: the flow rate of the oslo crystallization circulation pump is smaller than the flow rate of the evaporation circulation pump.
9. The improved oslo continuous crystallizer as in claim 5, wherein: the flow rate of the oslo crystallization circulation pump is smaller than the flow rate of the evaporation circulation pump.
10. The improved oslo continuous crystallizer as claimed in any one of claims 7 to 9, characterized in that: the ratio of the flow rate of the oslo crystallization circulating pump to the flow rate of the heat exchange circulating pump is 1:1.1 to 200.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222712610.7U CN219595902U (en) | 2022-10-14 | 2022-10-14 | Improved oslo continuous crystallizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222712610.7U CN219595902U (en) | 2022-10-14 | 2022-10-14 | Improved oslo continuous crystallizer |
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| Publication Number | Publication Date |
|---|---|
| CN219595902U true CN219595902U (en) | 2023-08-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222712610.7U Active CN219595902U (en) | 2022-10-14 | 2022-10-14 | Improved oslo continuous crystallizer |
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| CN (1) | CN219595902U (en) |
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2022
- 2022-10-14 CN CN202222712610.7U patent/CN219595902U/en active Active
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