CN215900948U - Double-system evaporative crystallization device - Google Patents
Double-system evaporative crystallization device Download PDFInfo
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- CN215900948U CN215900948U CN202121844611.6U CN202121844611U CN215900948U CN 215900948 U CN215900948 U CN 215900948U CN 202121844611 U CN202121844611 U CN 202121844611U CN 215900948 U CN215900948 U CN 215900948U
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Abstract
The utility model discloses a double-system evaporative crystallization device, and belongs to the technical field of evaporative crystallization equipment. The outlet of the unsaturated concentrated solution of the concentration tower is communicated with the top of the concentration tower through a circulating solution circulating pipeline of the concentration tower, the outlet of the saturated concentrated solution is communicated with the crystallization evaporation kettle, and the gas outlet of the concentration tower is communicated with the condensed gas inlet of the condensing tower group; the condensed fluid outlet of each condensing tower is communicated with the top of another condensing tower through a pipeline and a heat exchange device, the condensed gas outlet of the previous condensing tower is communicated with the condensed gas inlet of the next condensing tower, and the condensed gas outlet of the tail condensing tower is communicated with the gas inlet of the condensing tower through a pipeline to form an air circulation loop. The device concentration tower utilizes the surface evaporation principle to concentrate the waste liquid to the saturation after, reuse crystallization evaporation cauldron negative pressure boiling evaporation heating crystallization principle that again, and the condensate water and the secondary steam that produce can the reutilization wherein heat energy, reach energy-conserving purpose, have solved the problem that exists in the use of traditional evaporimeter simultaneously.
Description
Technical Field
The utility model relates to an evaporative crystallization device, in particular to a binary system evaporative crystallization device, belongs to the technical field of evaporative crystallization equipment, and is particularly suitable for pretreatment and reduction of waste liquid containing high-concentration organic matters and inorganic matters and complex industrial wastewater.
Background
In the process of crystallizing liquid containing high salt and high organic matters, an MVR evaporator or a triple-effect evaporator is usually adopted, the two evaporators are both used for evaporating by utilizing the principle that waste liquid is heated to the boiling point under negative pressure and then water in the waste liquid is generated into water vapor through boiling, and the evaporator is widely applied to the salt chemical industry. However, in the complex process of treating industrial waste liquid, because the liquid has high hardness and a large amount of COD, acid, alkali and other substances exist, crystallization is very difficult, and various conditions such as easy corrosion, easy blockage, coking and the like are very common, so that after equipment is constructed and put into operation, continuous and stable operation cannot be realized, and certain economic loss and great troubles are caused to enterprises.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problems, the utility model provides a binary system evaporative crystallization device, evaporative crystallization carried out by using the device can utilize the surface evaporation principle to concentrate waste liquid to a saturated state, then heat and crystallize in a micro-negative pressure boiling evaporation mode, and secondary steam generated by crystallization returns to a surface evaporation section for secondary utilization, thereby achieving the purpose of energy conservation and simultaneously solving the problems existing in the use process of the traditional evaporator.
The technical scheme of the utility model is as follows:
a double-system evaporative crystallization device comprises a concentration tower, wherein an unsaturated concentrated solution discharge port at the bottom of the concentration tower is communicated with the top of the concentration tower through a circulating solution circulating pipeline of the concentration tower; a saturated concentrated solution outlet at the bottom of the concentration tower is communicated with a crystallization evaporation kettle through a pipeline; a gas outlet of the concentration tower at the top of the concentration tower is communicated with a condensed gas inlet at the bottom of a condensation tower set through a pipeline;
the condensation tower group comprises at least two condensation towers, and a condensate outlet at the bottom of each condensation tower is communicated with the tops of other condensation towers after passing through a pipeline and a heat exchange device; and a condensed gas outlet of the previous condensing tower in the condensing tower group is communicated with a condensed gas inlet of the next condensing tower through a pipeline, and a condensed gas outlet of the condensing tower at the tail end is communicated with a gas inlet of the concentrating tower through a pipeline to form an air circulation loop.
The further technical scheme is as follows:
the circulating liquid circulating pipeline of the concentration tower comprises a high-temperature condensed water preheating heat exchanger and a steam heater which are sequentially communicated along the flowing direction of unsaturated condensed liquid, an unsaturated condensed liquid discharge port is communicated with a cold side inlet of the high-temperature condensed water preheating heat exchanger through a pipeline and an evaporation tower circulating pump, a cold side outlet of the high-temperature condensed water preheating heat exchanger is communicated with a cold side inlet of the steam heater through a pipeline, and a cold side outlet of the steam heater is communicated with the top of the concentration tower through a pipeline.
The further technical scheme is as follows:
and a cold side inlet of the high-temperature condensed water preheating heat exchanger is communicated with a waste treatment waste liquid source through a pipeline and a water inlet pump.
The further technical scheme is as follows:
the condensation tower group comprises a first condensation tower and a second condensation tower, wherein a condensate outlet at the bottom of the first condensation tower is communicated with a heat source pipeline inlet of the high-temperature condensate preheating heat exchanger after passing through a pipeline and a high-temperature condensate circulating pump, and an outlet of a hot side pipeline is communicated with the top of the second condensation tower through a pipeline; and a condensate outlet at the bottom of the second condensing tower is communicated with a hot side pipeline inlet of a cooling plate type heat exchanger after passing through a pipeline and a low-temperature condensate circulating pump, and an outlet of the hot side pipeline is communicated with the top of the first condensing tower.
The further technical scheme is as follows:
and a cold side inlet and a cold side outlet of the cooling plate type heat exchanger are respectively communicated with an external cooling circulating water supply pipeline and a water return pipeline.
The further technical scheme is as follows:
and water distributors for spraying liquid are positioned at the tops of the concentration tower, the first condensation tower and the second condensation tower.
The further technical scheme is as follows:
and a secondary steam outlet of the crystallization evaporation kettle is communicated with an injection interface of a steam jet pump through a pipeline, and an outlet of the steam jet pump is communicated with a hot side inlet of the steam heater.
The further technical scheme is as follows:
and the middle sections of the condensing towers in the condensing tower and the condensing tower group are provided with folded plate type structured packing in a positioning manner.
The further technical scheme is as follows:
a liquid level sensor and a density sensor are positioned at the bottom in the concentration tower, and a row of concentration pumps are positioned on a pipeline outside a saturated liquid outlet of the concentration tower.
The further technical scheme is as follows:
the crystallization evaporation kettle is a jacket type evaporation kettle or a semi-coil heating evaporation kettle, and a steam inlet for an external steam source to enter and a condensate outlet for discharging condensate in the jacket or the coil are arranged at the upper part of the jacket or the outer coil of the evaporation kettle.
The beneficial technical effects of the utility model are as follows:
the device is provided with a circulating liquid circulating pipeline of the concentration tower on the concentration tower, and the water in the raw materials is extracted by utilizing the surface evaporation principle, namely, the moisture carrying capacity of air, so as to achieve the concentration purpose; at the stage after concentration, at least two condensing towers are used in a combined manner, and micro-positive pressure is adopted in combination with the condensing towers, so that heat exchangers in various forms such as plate heat exchangers can be adopted, the frequency of blockage and scaling in the heat exchangers is reduced through high flow rate, and the stable operation of the equipment can be ensured;
the device adopts a jacketed or semi-coiled evaporative crystallization kettle to carry out evaporative crystallization on the concentrated waste liquid in an evaporative crystallization section, heats and pressurizes the generated high-temperature secondary steam through arranging a pipeline and a steam jet pump, and then conveys the high-temperature secondary steam to a heat exchanger in front of a concentration tower to realize heating of the waste liquid and the circulating liquid; in addition, due to the design of pipelines at the condensate outlet and the condensate inlet of each condensing tower in the condensing tower set, condensate generated by the condensing tower set can be cooled and then used as spray water at the tops of other condensing towers in the condensing tower set, so that materials and energy can be recycled, and the purpose of saving energy is achieved.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention; wherein the dotted line represents the circulating air flow path;
1. a water inlet pump;
2. an evaporation tower circulating pump;
3. preheating a heat exchanger by high-temperature condensed water;
4. a concentration tower; 41. an unsaturated concentrated solution outlet; 42. a saturated concentrated solution outlet; 43. a gas outlet of the concentration tower;
5. folded plate type packing;
6. a water distributor;
7. a condensing tower set; 71. a first condensing tower; 72. a second condensing tower;
8. a circulating liquid circulating pipeline of the concentration tower;
9. a concentration discharge pump;
10. a steam heater;
11. a high-temperature condensed water circulating pump;
12. a low-temperature condensed water circulating pump;
13. cooling the plate heat exchanger;
14. a crystallization evaporation kettle;
15. a steam jet pump;
16. and a circulating fan.
Detailed Description
In order to make the technical means of the present invention clearer and to make the technical means of the present invention capable of being implemented according to the content of the specification, the following detailed description of the embodiments of the present invention is made with reference to the accompanying drawings and examples, which are provided for illustrating the present invention and are not intended to limit the scope of the present invention.
The utility model discloses a double-system evaporative crystallization device, which mainly comprises a concentration tower 4, a crystallization evaporation kettle 14, a condensation tower group 7, a concentration tower circulating liquid circulating pipeline 8 and a heat exchange device.
The lowest point of the bottom of the concentration tower 4 is provided with an unsaturated concentrated solution outlet 41, the unsaturated concentrated solution outlet 41 is communicated with the top of the concentration tower through a circulating liquid circulating pipeline 8 of the concentration tower, wherein the circulating liquid circulating pipeline 8 of the concentration tower comprises a high-temperature condensed water preheating heat exchanger 3 and a steam heater 10 which are sequentially communicated and arranged along the flowing direction of the unsaturated concentrated solution. The specific connection mode is that the unsaturated concentrated solution outlet 41 is communicated with the cold side inlet of the high-temperature condensed water preheating heat exchanger 3 through a pipeline and an evaporation tower circulating pump 2 positioned at the outlet, the cold side outlet of the high-temperature condensed water preheating heat exchanger 3 is communicated with the cold side inlet of the steam heater 10 through a pipeline, and the cold side outlet of the steam heater 10 is communicated with the top of the concentration tower 4 through a pipeline; in addition, a cold side inlet of the high-temperature condensed water preheating heat exchanger 3 is communicated with a waste liquid source to be treated through a pipeline and a water inlet pump 1. Thus, the unsaturated condensate and the waste liquid to be treated pass through the high-temperature condensate preheating heat exchanger 3 and the steam heater 10 in this order as the cold side, are heated to a predetermined temperature, and are sprayed from the top of the concentrating tower 4.
A saturated concentrated solution outlet 42 is arranged at the upper position of the bottom of the concentration tower 4, and the saturated concentrated solution outlet 42 is communicated with the crystallization evaporation kettle 14 through a pipeline. The bottom department location in the concentrated tower 4 is equipped with a level sensor and a density sensor, and the location is equipped with one row of concentrate pump 9 on the outside pipeline of saturated liquid discharge port of concentrated tower, after detecting that concentrate density reaches the default, row's concentrate pump starts, arranges the saturated concentrate to crystallization evaporation cauldron, and the liquid level height bottom this concentrated tower of control through level sensor.
The crystallization evaporation kettle 14 is a jacketed evaporation kettle or a semi-coil heating evaporation kettle, a steam inlet for an external steam source to enter and a condensate outlet for condensate water in the jacket or the coil to discharge are arranged at the upper part of the jacket or the outer coil of the evaporation kettle, raw steam enters the jacket or the coil from the steam inlet, exchanges heat with the evaporation kettle to form steam condensate water, and then is discharged from the condensate outlet. A secondary steam outlet is formed in the top cover of the evaporation kettle 14 and is communicated with an injection inlet of a steam jet pump 15 through a pipeline, a driving steam inlet of the steam jet pump is communicated with an external steam source through a pipeline, and an outlet of the steam jet pump 15 is communicated with a hot side inlet of the steam heater 10. The secondary steam generated by mixing is used as the hot side of the steam heater 10, the preheated circulating unsaturated concentrated solution and the waste liquid to be treated are used as cold sources of the steam heater 10, and the two are subjected to heat exchange in the steam heater 10. In addition, a stirring device is positioned in the crystallization evaporation kettle 14, and a crystallization salt outlet is arranged at the bottom of the kettle body.
The highest point of the top of the concentration tower 4 is provided with a concentration tower gas outlet 43, and the concentration tower gas outlet 43 is communicated with a condensed gas inlet at the bottom of the condensation tower group 7 through a pipeline. The condensing tower group 7 comprises at least two condensing towers, and a condensate outlet at the bottom of each condensing tower is communicated with the tops of other condensing towers after passing through a pipeline and a heat exchange device; and the condensed gas outlet of the previous condensing tower in the condensing tower group 7 is communicated with the condensed gas inlet of the next condensing tower through a pipeline, and the condensed gas outlet of the condensing tower at the tail end is communicated with the gas inlet of the condensing tower through a pipeline and a circulating fan 16 to form an air circulation loop.
In the present embodiment, the condensation tower group 7 includes two condensation towers, i.e., a first condensation tower 71 and a second condensation tower 72. The condensate outlet at the bottom of the first condensation tower 71 is communicated with the hot side pipeline inlet of the high-temperature condensate preheating heat exchanger 3 through a pipeline and a high-temperature condensate circulating pump 11, and the hot side pipeline outlet is communicated with the top of the second condensation tower through a pipeline, namely, the high-temperature condensate formed by condensation in the first condensation tower enters the high-temperature condensate preheating heat exchanger as the hot side. The condensate outlet of the bottom 72 of the second condensing tower is communicated with the hot side pipeline inlet of a cooling plate heat exchanger 13 through a pipeline and a low-temperature condensate circulating pump 12, and the outlet of the hot side pipeline is communicated with the top of the first condensing tower, wherein the cold side inlet and the cold side outlet of the cooling plate heat exchanger 13 are respectively communicated with an external cooling circulating water source, namely, the low-temperature condensate formed by condensation in the second condensing tower enters the cooling plate heat exchanger as the hot side. The condensed gas outlet at the top of the first condensing tower 71 is communicated with the condensed gas inlet at the bottom of the second condensing tower 72 through a pipeline, and the condensed gas outlet at the top of the second condensing tower 72 is communicated with the gas inlet at the bottom of the concentration tower through a pipeline and the circulating fan 16.
In this embodiment, a water distributor 6 for spraying liquid is positioned at the top of each of the concentration tower 4, the first condensation tower 71 and the second condensation tower 72, and the liquid entering the top of the tower through the pipeline is uniformly distributed from the top to the bottom of the tower through the water distributor.
In this embodiment, the folding plate type structured packing 5 is positioned at the middle position of each of the condensing towers 4 and 7, such as the first condensing tower 71 and the second condensing tower 72, and can increase the water-gas contact area and promote the conversion of gas phase and liquid phase.
In the embodiment, the corrosion-resistant polymer composite material is mainly used as the contact medium part and the equipment main body material of the concentration tower, the condensation tower and other main equipment, so that the corrosion resistance of the system can be obviously improved, the application of metal materials is reduced, and the equipment cost can be effectively reduced.
The method for carrying out the dual-system evaporative crystallization by using the device mainly comprises the following steps:
the waste liquid is pressurized by a water inlet pump 1 and sent to a circulating liquid circulating pipeline 8 of the concentration tower. The circulating liquid circulating pipeline 8 of the concentration tower mainly comprises an evaporation tower circulating pump 2, a high-temperature condensate preheating heat exchanger 3 and a steam heater 10 which are sequentially communicated along the flowing direction of unsaturated concentrated liquid and are used for circulating the unsaturated concentrated circulating liquid in the concentration tower.
The unsaturated concentrated circulating liquid flows out from an unsaturated concentrated liquid outlet at the bottom of the concentrating tower 4 and then enters a circulating liquid circulating pipeline 8 of the concentrating tower. The unsaturated concentrated circulating liquid is pressurized by a circulating pump 2 of the evaporation tower, is sent into a high-temperature condensed water preheating heat exchanger 3, is merged with the waste liquid and then is preheated by the high-temperature condensed water preheating heat exchanger 3 as a cold side, then enters a steam heater 10 through a pipeline to be heated by the steam heater 10 as the cold side, heats the temperature of the waste liquid and the unsaturated concentrated circulating liquid to 80-85 ℃ through the two heat exchange devices, and then is distributed to a concentration tower 4 through a water distributor 6 at the top in the concentration tower 4. The middle section position in the concentration tower 4 is provided with a folded plate type structured packing for increasing the contact area of air and water and promoting the transfer of water in the waste liquid to the gas phase. When the density of the liquid at the bottom of the concentration tower reaches a preset value, controlling a concentration discharge pump 9 to discharge saturated concentrated liquid into the evaporation crystallization kettle; and when the density of the liquid at the bottom of the concentrated solution does not reach a preset value but reaches a preset minimum working liquid level, controlling the concentration tower to discharge unsaturated concentrated solution into the circulating liquid circulating pipeline of the concentration tower.
The circulating fan 16 continuously blows circulating air into the concentration tower 4 from the bottom of the concentration tower. In the tower, circulating air is in continuous countercurrent contact with high-temperature waste liquid, the waste liquid forms a liquid film on the surface of the folded plate, and after the liquid film is in contact with the air, moisture in the waste liquid is transferred to the air to form a concentration process. Saturated high-temperature wet air is formed when the air reaches the top of the concentration tower, and the saturated high-temperature wet air sequentially enters each condensation tower in the condensation tower group from the bottom of the condensation tower group 7 for condensation; the formed condensed water is subjected to heat exchange and refrigeration and then is used as spray water of other condensing towers to be sprayed into the condensing towers; the air after condensation treatment is used as circulating air and introduced into the bottom of the concentration tower.
The condensing tower group 7 comprises at least two condensing towers, in this embodiment, a first condensing tower 71 and a second condensing tower 72, and each condensing tower is provided with a water distributor 6 and a folded plate type packing 5. Saturated high-temperature humid air enters from the lower part of the first condensing tower and is fully contacted with condensed water at the folded plate type packing, the temperature of the moisture in the air is reduced when encountering the condensed water, the moisture in the air is converted from a gaseous state into a liquid state, and meanwhile, latent heat is released, so that the temperature of the condensed water is increased. The bottom of the first condensing tower is provided with a condensate outlet for being connected with a high-temperature condensate circulating pump 11, the high-temperature condensate passes through the high-temperature condensate circulating pump 11 and is conveyed to the high-temperature condensate preheating heat exchanger 3 to provide heat, and after the high-temperature condensate is subjected to heat exchange with the condensate circulating liquid of the condensing tower, the temperature of the condensate is reduced, the condensate is returned to the top of the second condensing tower 72, and the condensate is sprayed into the tower through a water distributor and then is contacted with the air.
Namely, the discharged unsaturated concentrated solution enters the high-temperature condensate preheating heat exchanger 3 as the cold side, and the high-temperature condensate formed by the first condensing tower enters the high-temperature condensate preheating heat exchanger 3 as the hot side, so that the preheating of the unsaturated concentrated solution and the refrigeration of the high-temperature condensate are realized; the preheated unsaturated concentrated solution enters a steam heater 10 as a cold side, secondary steam obtained by boiling and evaporating at a slight negative pressure of an evaporation crystallization kettle is pressurized and heated up and then enters the steam heater as a hot side, and the unsaturated concentrated solution can be heated up to 80-85 ℃.
The air cooled by the first condensing tower 71 has a higher temperature, generally reaching about 60 ℃, and in order to further recover moisture in the air, the air is continuously sent to the second condensing tower 72 through a pipeline, and the spray liquid at the top of the second condensing tower 72 is used for further cooling and dehumidifying. The structure of the second condensing tower is the same as that of the first-stage condensing tower, a bottom condensed water outlet, a low-temperature condensed water circulating pump 12 and a cooling plate type heat exchanger 13 form a circulating pipeline, outside cooling circulating water is used for cooling condensed water, the cooled condensed water is conveyed to the top of the first condensing tower and sprayed into the tower through a water distributor, latent heat of water condensation in the recovered air forms high-temperature condensed water and is conveyed to a high-temperature condensed water preheating heat exchanger 3.
The saturated concentrated solution discharged from the bottom of the concentration tower 4 is sent to an evaporation crystallization kettle 14 for boiling evaporation under a slight negative pressure. The evaporative crystallization kettle adopts a jacket type or an outer semi-coil type, external steam is introduced into the jacket or the coil, the external steam is used for heating up the concentrated solution in the kettle until boiling, water in the micro negative pressure boiling evaporation is converted into secondary steam, and then the secondary steam is sent to a steam jet pump 15 for repressurization and provides heat for a steam heater 10 for heating up the unsaturated concentrated solution. And (3) with the continuous reduction of the water in the evaporation crystallization kettle 14, finally reaching supersaturation, precipitating the crystallization salt, when the water is evaporated to 30-40% of solid content, sending the solution to an external centrifugal device for solid-liquid separation, and taking out the salt crystal from the system to obtain the salt crystal.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, it should be noted that, for those skilled in the art, many modifications and variations can be made without departing from the technical principle of the present invention, and these modifications and variations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A dual system evaporation crystallization device is characterized in that: comprises a concentration tower (4), wherein an unsaturated concentrated solution discharge port (41) at the bottom of the concentration tower is communicated with the top of the concentration tower through a circulating liquid circulating pipeline (8) of the concentration tower; a saturated concentrated solution outlet (42) at the bottom of the concentration tower is communicated with a crystallization evaporation kettle (14) through a pipeline; a gas outlet (43) of the concentration tower at the top of the concentration tower is communicated with a condensed gas inlet at the bottom of a condensation tower group (7) through a pipeline;
the condensation tower group (7) comprises at least two condensation towers, and a condensate outlet at the bottom of each condensation tower is communicated with the tops of other condensation towers after passing through a pipeline and a heat exchange device; and a condensed gas outlet of a previous condensing tower in the condensing tower group (7) is communicated with a condensed gas inlet of a next condensing tower through a pipeline, and a condensed gas outlet of a condensing tower at the tail end is communicated with a gas inlet of a concentrating tower through a pipeline to form an air circulation loop.
2. The dual system evaporative crystallization apparatus of claim 1, wherein: the concentrating tower circulating liquid circulating pipeline (8) comprises a high-temperature condensed water preheating heat exchanger (3) and a steam heater (10) which are sequentially communicated along the flowing direction of unsaturated concentrated liquid, an unsaturated concentrated liquid discharge port (41) is communicated with a cold side inlet of the high-temperature condensed water preheating heat exchanger (3) through a pipeline and an evaporation tower circulating pump (2), a cold side outlet of the high-temperature condensed water preheating heat exchanger (3) is communicated with a cold side inlet of the steam heater (10) through a pipeline, and a cold side outlet of the steam heater is communicated with the top of the concentrating tower (4) through a pipeline.
3. The dual system evaporative crystallization apparatus of claim 2, wherein: and a cold side inlet of the high-temperature condensed water preheating heat exchanger (3) is communicated with a waste treatment waste liquid source through a pipeline and a water inlet pump (1).
4. The dual system evaporative crystallization apparatus of claim 2, wherein: the condensation tower group (7) comprises a first condensation tower (71) and a second condensation tower (72), wherein a condensate discharge port at the bottom of the first condensation tower is communicated with a heat source pipeline inlet of the high-temperature condensate preheating heat exchanger (3) after passing through a pipeline and a high-temperature condensate circulating pump (11), and a hot side pipeline outlet is communicated with the top of the second condensation tower through a pipeline; and a condensate outlet at the bottom of the second condensing tower is communicated with a hot side pipeline inlet of a cooling plate type heat exchanger (13) after passing through a pipeline and a low-temperature condensate circulating pump (12), and an outlet of the hot side pipeline is communicated with the top of the first condensing tower.
5. The dual system evaporative crystallization apparatus of claim 4, wherein: and a cold side inlet and a cold side outlet of the cooling plate type heat exchanger (13) are respectively communicated with an external cooling circulating water supply pipeline and a water return pipeline.
6. The dual system evaporative crystallization apparatus of claim 4, wherein: and a water distributor (6) for spraying liquid is positioned at the top of each of the concentration tower (4), the first condensation tower (71) and the second condensation tower (72).
7. The dual system evaporative crystallization apparatus of claim 4, wherein: and a secondary steam outlet of the crystallization evaporation kettle (14) is communicated with an injection interface of a steam injection pump (15) through a pipeline, and an outlet of the steam injection pump (15) is communicated with a hot side inlet of the steam heater (10).
8. The dual system evaporative crystallization apparatus of claim 1, wherein: and the middle sections of the condensing towers in the condensing tower (4) and the condensing tower set (7) are provided with folded plate type structured packing (5) in a positioning way.
9. The dual system evaporative crystallization apparatus of claim 1, wherein: a liquid level sensor and a density sensor are positioned at the bottom in the concentration tower (4), and a row of concentration pumps (9) are positioned on a pipeline outside a saturated liquid outlet of the concentration tower.
10. The dual system evaporative crystallization apparatus of claim 1, wherein: the crystallization evaporation kettle (14) is a jacketed evaporation kettle or a semi-coil heating evaporation kettle, and the upper part of a jacket or an outer coil of the evaporation kettle is provided with a steam inlet for an external steam source to enter and a condensed water outlet for discharging condensed water in the jacket or the coil.
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| CN202121844611.6U CN215900948U (en) | 2021-08-09 | 2021-08-09 | Double-system evaporative crystallization device |
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| CN202121844611.6U CN215900948U (en) | 2021-08-09 | 2021-08-09 | Double-system evaporative crystallization device |
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Effective date of registration: 20230118 Address after: 233000 A2, 290 Tebu Avenue, Huaishang District, Bengbu City, Anhui Province Patentee after: Anhui juyun environmental protection equipment manufacturing Co.,Ltd. Address before: 210000 room 205, No. 112 Hanzhong Road, Gulou District, Nanjing, Jiangsu Province Patentee before: Jiangsu juyunruichuang Environmental Protection Technology Co.,Ltd. |