CN220056596U - High-salt wastewater normal-temperature crystallization treatment system - Google Patents
High-salt wastewater normal-temperature crystallization treatment system Download PDFInfo
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- CN220056596U CN220056596U CN202321633217.7U CN202321633217U CN220056596U CN 220056596 U CN220056596 U CN 220056596U CN 202321633217 U CN202321633217 U CN 202321633217U CN 220056596 U CN220056596 U CN 220056596U
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- 239000002351 wastewater Substances 0.000 title claims abstract description 27
- 238000002425 crystallisation Methods 0.000 title claims abstract description 25
- 230000008025 crystallization Effects 0.000 title claims abstract description 25
- 239000003814 drug Substances 0.000 claims abstract description 39
- 150000003839 salts Chemical class 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 239000011259 mixed solution Substances 0.000 claims abstract description 24
- 239000012267 brine Substances 0.000 claims abstract description 16
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 239000000498 cooling water Substances 0.000 claims description 13
- 239000007787 solid Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000004806 packaging method and process Methods 0.000 claims description 6
- 239000000243 solution Substances 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 2
- 239000013078 crystal Substances 0.000 abstract description 15
- 238000000034 method Methods 0.000 abstract description 12
- 238000001556 precipitation Methods 0.000 abstract description 8
- 239000003153 chemical reaction reagent Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 10
- 238000002156 mixing Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 4
- 230000003993 interaction Effects 0.000 description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 239000013043 chemical agent Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 101100298222 Caenorhabditis elegans pot-1 gene Proteins 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000008177 pharmaceutical agent Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000005185 salting out Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model relates to a normal-temperature crystallization treatment system for high-salt wastewater, which comprises a reagent tank and a concentrated brine tank which are respectively provided with a normal-temperature salt precipitation reagent and high-salt wastewater, wherein the reagent tank and the concentrated brine are connected with the same mixed reaction kettle, the mixed reaction kettle is connected with a crystal growth tank, the crystal growth tank is connected with a horizontal screw centrifuge, a liquid outlet of the horizontal screw centrifuge is connected with a mixed solution tank, the mixed solution tank is connected with a first passage inlet of a plate heat exchanger, a first passage outlet of the plate heat exchanger is connected with a liquid inlet of a fractionating tower, the preheating of the mixed liquid before the diversion is realized, the energy consumption is saved, the fractionating tower is connected with a heat source through a circulating pipeline, an air outlet of the fractionating tower is connected with a first passage inlet of a condenser through a pipeline, a first passage outlet of the condenser is connected with a reagent recovery intermediate tank through a pipeline, and the reagent recovery intermediate tank is connected with the reagent tank through a pipeline. The method realizes the treatment of high-salt wastewater by using normal-temperature salt precipitation medicament, can recycle the medicament, has low treatment cost, is not easy to scale and block a system pipeline, has small occupied area and can treat various inorganic salts.
Description
Technical Field
The utility model relates to a high-salt wastewater normal-temperature crystallization treatment system, and belongs to the technical field of sewage treatment.
Background
The high-salt concentrated solution is one of common waste water in the chemical industry, and generally refers to concentrated solution with the mass fraction of salt above 20%.
In the prior art, a three-effect evaporator crystallization or MVR evaporation crystallization process is generally adopted to treat the high-salt wastewater. The three-effect evaporator crystallization process is generally suitable for treating the salt-containing wastewater with medium concentration, the MVR evaporation crystallization process is generally suitable for treating the salt-containing wastewater with lower concentration, the problems of complex operation management and easy blockage exist in the two processes, the engineering investment and the operation cost are high, the occupied area is large, the water distribution system is complex and has multiple faults, the system is frequently required to be stopped and maintained, the equipment pipeline is often scaled and blocked, and the normal operation is influenced during cleaning. Both prior art methods are not suitable for the treatment of high-salinity wastewater.
The normal temperature salt precipitation is used for treating high salt wastewater through a normal temperature crystallization separation scheme, and the normal temperature salt precipitation refers to a process of precipitating salt crystals by utilizing the water distribution generating effect of a medicament and mother liquor. The high-salinity wastewater normal-temperature crystallization treatment system which adopts the normal-temperature salting-out technology and has reasonable design structure can effectively simplify the operation and reduce the blockage.
Disclosure of Invention
The utility model provides a high-salt wastewater normal-temperature crystallization treatment system, which aims to overcome the defects in the prior art and realize a treatment system suitable for treating high-salt wastewater by a normal-temperature salt precipitation medicament.
The technical solution of the utility model is as follows: the utility model provides a high salt waste water normal atmospheric temperature crystallization processing system, its structure includes the medicament jar that is equipped with normal atmospheric temperature salt precipitation medicament and the strong brine jar that is equipped with normal atmospheric temperature high salt waste water, medicament jar and strong brine jar are respectively through the same mixing reaction kettle of pipe connection, mixing reaction kettle passes through the crystallization growth jar, crystallization growth jar passes through the pipe connection horizontal screw centrifuge, horizontal screw centrifuge liquid outlet passes through the pipe connection mixed solution jar, mixed solution jar passes through the first passageway import of pipe connection plate heat exchanger, plate heat exchanger first passageway export passes through the pipe connection fractionating tower inlet, realize preheating to mixed liquid before the reposition of redundant personnel, the energy consumption is practiced thrift, the fractionating tower passes through circulating line and connects the heat source, the fractionating tower gas outlet passes through pipe connection condenser one passageway import, condenser one passageway export passes through pipe connection medicament recovery intermediate tank, medicament recovery intermediate tank passes through pipe connection medicament jar. Realizing the closed loop process recycling of the medicament.
Preferably, the solid outlet of the horizontal screw centrifuge is connected with the low temperature heat pump dryer through a pipeline, the liquid outlet is connected with the mixed solution tank through a pipeline, the solid outlet of the low temperature heat pump dryer is provided with packaging equipment, the liquid outlet is connected with the mixed solution tank through a pipeline, the heat source inlet is connected with the outlet of the other passage of the condenser through a pipeline, the heat source outlet is connected with the cooling water tank through a pipeline, and the cooling water tank is connected with the inlet of the other passage of the condenser through a pipeline with a pump. The full liquid removal and packaging of the crystallized solid salt are realized, and the heat source comes from the condenser, so that the energy can be saved.
Preferably, the inlet of the second passage of the plate heat exchanger is connected with the liquid outlet of the fractionating tower through a pipeline, the outlet of the second passage of the plate heat exchanger is connected with a recycling water tank through a pipeline, and the recycling water tank is connected with a production line through a pipeline. Can be returned to the production line to be used as reclaimed water, thereby saving water resources.
Preferably, the heat source is industrial steam or a conduction oil furnace.
The utility model has the advantages that: the high-salt wastewater treatment device has reasonable structural design, realizes normal-temperature salt precipitation medicament treatment of high-salt wastewater, can recycle the medicament, reduces treatment cost, can effectively reduce energy consumption, investment and maintenance cost, is not easy to scale and block a system pipeline, has small occupied area and can treat various inorganic salts.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of a system for normal temperature crystallization treatment of high salt wastewater according to the present utility model.
In the figure, 1 is a chemical tank, 2 is a concentrated brine tank, 3 is a mixed reaction kettle, 4 is a crystal growth tank, 5 is a horizontal decanter centrifuge, 6 is a mixed solution tank, 7 is a plate heat exchanger, 8 is a fractionating tower, 9 is a low-temperature heat pump dryer, 10 is a cooling water tank, 11 is a recycling water tank, 12 is a packaging device, 1 is a condenser, 14 is a chemical recovery intermediate tank, and 15 is a heat source.
Detailed Description
The present utility model will be described in further detail with reference to examples and embodiments.
As shown in figure 1, the high-salt wastewater normal-temperature crystallization treatment system structurally comprises a medicament tank 1 filled with normal-temperature salt precipitation medicament and a concentrated brine tank 2 filled with normal-temperature high-salt wastewater, wherein the medicament tank 1 and the concentrated brine tank 21 are respectively connected with the same mixing reaction kettle 3 through pipelines with metering pumps, the mixing reaction kettle 3 is connected with a crystal growth tank 4 through pipelines with pumps, the crystal growth tank 4 is connected with a decanter centrifuge 5 through pipelines with pumps, a solid outlet of the decanter centrifuge 5 is connected with a low-temperature heat pump dryer 9 through pipelines, a liquid outlet of the decanter centrifuge 5 is connected with a mixed solution tank 6 through pipelines, a solid outlet of the low-temperature heat pump dryer 9 is provided with a packaging device 12, a liquid outlet of the decanter dryer is connected with the mixed solution tank 6 through pipelines, a heat source inlet of the crusher is connected with a first passage outlet of a condenser 13 through pipelines, a heat source outlet of the crusher is connected with a cooling water tank 10 through pipelines, the cooling water tank 10 is connected with a first passage inlet of the condenser 13 through a pipeline with a pump, the mixed solution tank 6 is connected with a first passage inlet of the plate heat exchanger 7 through a pipeline with a pump, a first passage outlet of the plate heat exchanger 7 is connected with a liquid inlet of the fractionating tower 8 through a pipeline, a second passage inlet of the plate heat exchanger 7 is connected with a liquid outlet of the fractionating tower 8 through a pipeline with a pump, an outlet of the plate heat exchanger is connected with the recycling water tank 11 through a pipeline, the recycling water tank 11 is connected with a production line through a pipeline with a pump, the fractionating tower 8 is connected with a heat source 15 through a circulating pipeline, the heat source 15 is industrial steam or a heat conducting oil furnace, an air outlet of the fractionating tower 8 is connected with a second passage inlet of the condenser 13 through a pipeline, a second passage outlet of the condenser 13 is connected with the chemical recovery intermediate tank 14 through a pipeline, and the chemical recovery intermediate tank 14 is connected with the chemical tank 1 through a pipeline with a pump.
According to the structure, when the device works, chemical high-salt wastewater stored in the strong brine tank 2 at normal temperature and the medicament in the medicament tank 1 are sent to the mixing reaction kettle 3 for reaction, then sent to the crystal growth tank 4 for crystallization, and then sent to the horizontal decanter centrifuge 5 for respectively obtaining mixed liquid of crystal solid salt and medicament+water;
the crystallized solid salt enters a low-temperature heat pump dryer 9, the obtained crystallized solid salt is packaged and stored or recycled by a packaging device 12, the obtained liquid enters a mixed solution tank 6,
the mixed liquid obtained by the horizontal screw centrifuge 5 enters a mixed solution tank 6, then enters a plate heat exchanger 7 for preheating, and is sent into a fractionating tower 8 for evaporation fractionation after being preheated, and a heat source 15 of the fractionating tower 8 is an industrial steam or heat conducting oil furnace;
the liquid obtained by the fractionating tower 8 enters a plate heat exchanger 7 to preheat the mixed liquid from the mixed solution tank 6, and enters a recycling water tank 11 after heat exchange, and can be returned to a production line to be used as reclaimed water, and the gas obtained by the fractionating tower 8 is sent to a condenser 13 to be condensed;
the medicament obtained by condensation of the condenser 13 enters a medicament recovery intermediate tank 14 for storage, the stored medicament can be sent back to the medicament tank 1 to form closed loop process for recycling, a cold source of the condenser 13 is from water discharged from the cooling water tank 10, the cold source water after heat exchange is changed into a gas state for the low-temperature heat pump dryer 9, and the gas returns to the cooling water tank 10 after use.
Examples
The basic principle of the process is as follows: in an organic solvent-electrolyte-water system, there are interactions between organic solvent molecules and water molecules and interactions between ions and water molecules, the two interactions competing with each other. When the interaction between the organic solvent molecules and water molecules is dominant, the number of water molecules interacting with ions is reduced, resulting in a decrease in the solubility of the electrolyte, and crystallization occurs. Hereinafter, the organic solvent is simply referred to as a pharmaceutical agent.
The medicine pot 1 is prepared: the total amount of the medicament to be used is concentrated saline water6 times the hourly throughput (i.e. 1m of treatment 3 In the case of concentrated saline, the total amount of the medicines to be used is 6m 3 ) To meet the amount of agent occupied by the stay in the system.
Delivering a medicament and a concentrated saline: the medicament and the strong brine are respectively delivered to the mixing reaction kettle 3 through metering pumps arranged at the bottom of the tank according to the proportion of medicament to strong brine=1.5:1. The mixing reaction time should be not less than 5 minutes to ensure uniform mixing and to allow fine salt grains to form in the mixed solution.
The crystal growth process comprises the following steps: the mixed solution containing fine crystal grains is fed to the crystal growth tank 4 by a metering pump provided at the bottom of the tank, and allowed to stand still. The residence time should be not less than 30 minutes to enable the grain size to grow to 0.5-1 mm. Subsequently, the mixed liquid containing crystals was sent to the decanter centrifuge 5 by a diaphragm pump for solid-liquid separation.
Solid-liquid separation: the decanter centrifuge 5 is used for separating solid crystals, and the separated solid crystals are sent to a low-temperature heat pump dryer through a screw conveyor. The mixed solution without solid crystals enters the mixed solution tank 6.
And (3) mixed solution treatment: the metering pump arranged at the bottom of the mixed solution tank 6 preheats the mixed solution through the plate heat exchanger 7 and then conveys the mixed solution to the top of the fractionating tower 8.
The fractionation process comprises the following steps: the temperature of the top of the fractionating tower 8 is controlled between 65 ℃ and 67 ℃ to enable the medicament to reach the boiling point temperature to be converted into gas phase, and the gas phase is guided to a condenser 13 for condensation through a top conduit. The dilute brine with the reagent removed automatically flows into the bottom heating kettle along the fractionating tower body. According to the amount of the dilute brine which is desolventized after entering the fractionating tower 8, a metering pump is arranged at the bottom of the tower to convey the hot dilute brine to the plate heat exchanger 7 for preheating the mixed liquor. The cooled dilute brine enters a reuse water tank 11 and is pumped back to the production line for use according to production requirements.
The heating mode of the bottom of the fractionating tower is as follows: in the presence of industrial steam, heating is performed using steam coils. If no industrial steam is available, a conduction oil furnace may be selected for heating.
And (3) medicament recovery: the gaseous chemical agent led out from the top of the fractionating tower 8 is condensed by a condenser 13 and then is converted into a liquid phase, and enters a chemical agent recovery intermediate tank 14. Subsequently, the medicament is recovered to the medicament tank 1 by pumping.
Heat source of low temperature heat pump dryer 9: part of the heat source of the low-temperature heat pump dryer 9 comes from the condensate water after use of the condenser 13. The condensed water carrying heat is cooled by the heat exchange end of the low-temperature heat pump dryer 9 and then flows back to the cooling water tank 10 for recycling. The hot end of the low temperature heat pump dryer 9 dries the surface moisture of crystallization by fan hot air. The hot air containing water is dehydrated by a condenser arranged in the low temperature heat pump dryer 9 to form dry air, and circulates in the low temperature heat pump dryer 9. The removed water is led into the mixed solution tank 6 through a water guide pipe.
Cooling water pool 10: the cooling water tank 10 is used for storing condensed circulating water, and an ozone aeration algae removal device can be arranged in the cooling water tank to prevent microorganism growth.
The above components are all of the prior art, and any model and existing design that can achieve their corresponding functions can be used by those skilled in the art.
The foregoing is merely a preferred embodiment of the present utility model, and it should be noted that modifications and improvements could be made by those skilled in the art without departing from the inventive concept, which falls within the scope of the present utility model.
Claims (4)
1. The utility model provides a high salt waste water normal atmospheric temperature crystallization processing system, a serial communication port, including medicament jar (1) and the strong brine jar (2) of normal atmospheric temperature high salt waste water that are equipped with the normal atmospheric temperature salt separation medicament, medicament jar (1) and strong brine jar (2) are respectively through the same hybrid reaction cauldron (3) of pipe connection, hybrid reaction cauldron (3) are through pipe connection crystallization growth jar (4), crystallization growth jar (4) are through pipe connection horizontal centrifuge (5), horizontal centrifuge (5) liquid outlet is through pipe connection hybrid solution jar (6), hybrid solution jar (6) are through pipe connection plate heat exchanger (7) first passageway import, plate heat exchanger (7) first passageway export is through pipe connection fractionating tower (8) inlet, fractionating tower (8) are through circulating pipe connection heat source (15), fractionating tower (8) gas outlet is through pipe connection condenser (13) one passageway import, condenser (13) one passageway export is through pipe connection medicament recovery intermediate tank (14), medicament recovery intermediate tank (14) is through pipe connection medicament jar (1).
2. The normal-temperature crystallization treatment system for high-salt wastewater according to claim 1, wherein a solid outlet of the horizontal screw centrifuge (5) is connected with a low-temperature heat pump dryer (9) through a pipeline, a liquid outlet is connected with a mixed solution tank (6) through a pipeline, a packaging device (12) is arranged at the solid outlet of the low-temperature heat pump dryer (9), a liquid outlet is connected with the mixed solution tank (6) through a pipeline, a heat source inlet is connected with another passage outlet of a condenser (13) through a pipeline, a heat source outlet is connected with a cooling water tank (10) through a pipeline, and the cooling water tank (10) is connected with another passage inlet of the condenser (13) through a pipeline with a pump.
3. The normal-temperature crystallization treatment system for high-salt wastewater according to claim 1, wherein the inlet of the second passage of the plate heat exchanger (7) is connected with the liquid outlet of the fractionating tower (8) through a pipeline, the outlet of the second passage of the plate heat exchanger is connected with the recycling water tank (11) through a pipeline, and the recycling water tank (11) is externally connected with a production line through a pipeline.
4. The high-salt wastewater normal-temperature crystallization treatment system according to claim 1, wherein the heat source (15) is an industrial steam or heat conduction oil furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321633217.7U CN220056596U (en) | 2023-06-26 | 2023-06-26 | High-salt wastewater normal-temperature crystallization treatment system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321633217.7U CN220056596U (en) | 2023-06-26 | 2023-06-26 | High-salt wastewater normal-temperature crystallization treatment system |
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| CN220056596U true CN220056596U (en) | 2023-11-21 |
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|---|---|---|---|
| CN202321633217.7U Active CN220056596U (en) | 2023-06-26 | 2023-06-26 | High-salt wastewater normal-temperature crystallization treatment system |
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| Country | Link |
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| CN (1) | CN220056596U (en) |
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2023
- 2023-06-26 CN CN202321633217.7U patent/CN220056596U/en active Active
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