CN215403194U - System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater - Google Patents
System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater Download PDFInfo
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- CN215403194U CN215403194U CN202121586178.0U CN202121586178U CN215403194U CN 215403194 U CN215403194 U CN 215403194U CN 202121586178 U CN202121586178 U CN 202121586178U CN 215403194 U CN215403194 U CN 215403194U
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Abstract
The utility model discloses a system for carrying out ammonia distillation treatment on ammonia-containing nitrogen-doped salt wastewater, and particularly relates to the field of wastewater treatment. The system comprises a feed pump, a first preheater, a second preheater, a deamination tower, a gas-liquid separator, a reboiler, a tower kettle discharge pump, a tower kettle liquid cooler, an ammonia water product pump, an ammonia water cooler and an ammonia water product storage tank. The feeding pump is connected with the gas-liquid separator through the first preheater, the gas-liquid separator is connected with the ammonia water product pump through the first preheater, and the ammonia water product pump is connected with the ammonia water product storage tank through the ammonia water cooler. According to the utility model, by reasonably controlling the operating parameters, the heat of the steam extracted from the top of the tower and the heat of the discharge of the tower kettle are fully utilized to preheat the feed, so that the energy consumption of the ammonia distillation section is greatly saved. The tower bottom of the utility model adopts the reboiler to generate the secondary steam, thereby avoiding the risk that the steam condensate water is mixed into the tower bottom wastewater discharged material to increase the downstream wastewater quantity and further increase the subsequent evaporation treatment cost due to the direct use of the steam.
Description
Technical Field
The utility model relates to the field of wastewater treatment, in particular to a system for performing ammonia distillation treatment on ammonia-containing nitrogen-doped saline wastewater.
Background
With the development of socioeconomic, the amount of industrial wastewater is also greatly increased. The ammonia-containing wastewater is one of various kinds of wastewater which is difficult to be recycled. For example, in the synthetic production of hydantoin drugs and the production process of ternary precursors of lithium battery positive electrode materials, a large amount of waste water rich in ammonia nitrogen and miscellaneous salt is generated.
With the increasingly strict national requirements on environmental protection, zero discharge of such wastewater gradually becomes a necessary condition for environmental approval or industry admission. At present, resources recovery is preferentially considered by enterprises for the process of zero discharge of the wastewater, and recovered byproducts can be sold or recycled to offset part of wastewater treatment cost and reduce the overall treatment cost; and secondary pollution can be avoided. Therefore, ammonia nitrogen is recovered into ammonia water for recycling in the production line in the treatment of the waste water containing the ammonia nitrogen salt; other salts are produced into industrial salts which meet the national standard and can be sold outside.
Based on the resource requirements, the treatment process of the waste water containing the ammonia nitrogen salt is generally 'steam stripping + chemical adding precipitation + evaporative crystallization'. Wherein, the 'stripping', namely ammonia steaming operation, is the section with the highest energy consumption in the whole process, and under the operation of directly adopting external steam stripping, steam condensate water is mixed into the discharged wastewater at the bottom of the tower, thereby increasing the downstream wastewater quantity, increasing the energy consumption of the subsequent evaporation crystallization operation and further increasing the treatment cost. Therefore, the development of a 'stripping' process and a 'stripping' system which are simple to operate, low in energy consumption and low in wastewater production is a great subject in the technical field of zero discharge of the waste water containing the ammonia nitrogen salt.
Disclosure of Invention
Therefore, the utility model provides a system for carrying out ammonia distillation treatment on ammonia-containing nitrogen-doped salt wastewater, which aims to solve the problems of complex stripping operation, high cost and the like in the method for extracting ammonia from wastewater in the prior art.
In order to achieve the above purpose, the utility model provides the following technical scheme:
according to one aspect of the utility model, the system for performing ammonia distillation treatment on ammonia-containing nitrogen-containing saltwater comprises a feeding pump, a first preheater, a second preheater, a deamination tower, a gas-liquid separator, a reboiler, a tower kettle discharge pump, a tower kettle liquid cooler, an ammonia water product pump, an ammonia water cooler and an ammonia water product storage tank;
the feeding pump is connected with the top end of the gas-liquid separator through the first preheater, the gas-liquid separator is connected with the ammonia water product pump through the first preheater, and the ammonia water product pump is connected with the ammonia water product storage tank through the ammonia water cooler;
the feed pump is connected with a discharge port at the top end of the deamination tower through a first preheater and a second preheater, and the tower bottom of the deamination tower is connected with a tower bottom liquid cooler through a tower bottom discharge pump and the second preheater; the bottom of the deamination tower is connected with a reboiler.
Further, the deamination tower is a packed tower.
Further, the deamination tower is a plate tower.
Further, the gas-liquid separator in the gas-liquid separator is a wire mesh demister.
Further, the reboiler is a vertical thermosiphon reboiler.
According to another aspect of the present invention, there is provided a method for treating ammonia-containing nitrogen-containing aza-salt wastewater by ammonia distillation using the above system, the method comprising the steps of:
the wastewater containing the ammonia nitrogen miscellaneous salt is pressurized by a feed pump, passes through a first preheater and the wastewater subjected to heat exchange with the overhead steam of the gas-liquid separator, and then passes through a second preheater and a tower kettle discharge pump to exchange heat with the bottom discharge of the tower;
feeding the wastewater preheated in the two steps from the upper part of a first theoretical plate of the deamination tower, wherein the gas-liquid balance is formed between secondary steam generated by the tower bottom of the deamination tower and a reboiler and liquid added above the first theoretical plate of the deamination tower; the steam in the gas-liquid separator exchanges heat with the wastewater entering through the feed pump through the first preheater and is condensed into ammonia water, and then enters an ammonia water product storage tank after exchanging heat with the circulating water in the ammonia water cooler through an ammonia water product pump and cooling;
and the product at the bottom of the deamination tower passes through a tower kettle discharge pump and a second preheater and then is discharged out of the system after being subjected to heat exchange and cooling with circulating water through a tower kettle liquid cooler.
Further, after the wastewater is preheated for two times, the temperature of the wastewater is 90-100 ℃.
Further, after the wastewater is preheated for two times, the temperature of the wastewater is 95-100 ℃.
Further, steam in the gas-liquid separator exchanges heat with wastewater entering through a feed pump through a first preheater and is condensed into ammonia water, and the condensation temperature of the ammonia water is 30-57 ℃.
Further, the operation pressure of the top of the deamination tower is 80-105 kPa, and the pressure drop of the whole deamination tower is 0-20 kPa.
Further, the operation pressure of the top of the deamination tower is 95-105 kPa, and the pressure drop of the whole deamination tower is 0-10 kPa.
Further, the operating pressure of the reboiler is 100-120 kPa.
Further, the operating pressure of the reboiler is 100-110 kPa
The pressure drop of the whole tower is the tower bottom pressure-tower top pressure.
The utility model has the following advantages:
1. according to the utility model, by reasonably controlling the operating parameters, the heat of the steam extracted from the top of the tower and the heat of the material discharged from the bottom of the tower are fully utilized to preheat the material, so that the energy consumption of the ammonia distillation section is greatly saved.
2. The tower bottom of the utility model adopts the reboiler to generate the secondary steam, thereby avoiding the risk that the steam condensate water is mixed into the tower bottom wastewater discharged material to increase the downstream wastewater quantity and further increase the subsequent evaporation treatment cost due to the direct use of the steam.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It should be apparent that the drawings in the following description are merely exemplary, and that other embodiments can be derived from the drawings provided by those of ordinary skill in the art without inventive effort.
The structures, ratios, sizes, and the like shown in the present specification are only used for matching with the contents disclosed in the specification, so as to be understood and read by those skilled in the art, and are not used to limit the conditions that the present invention can be implemented, so that the present invention has no technical significance, and any structural modifications, changes in the ratio relationship, or adjustments of the sizes, without affecting the effects and the achievable by the present invention, should still fall within the range that the technical contents disclosed in the present invention can cover.
FIG. 1 is a diagram of a system for ammonia distillation treatment of waste water containing ammonia nitrogen salt according to example 1 of the present invention;
FIG. 2 is a single tower system for ammonia distillation of ammoniacal miscellaneous salt wastewater provided in prior art comparative example 1;
FIG. 3 is a single-tower ammonia still system for stripping ammoniacal miscellaneous salt wastewater directly by using steam, which is provided by the prior art comparative example 2;
in the figure: 1 is a feed pump, 2 is a first preheater, 3 is a second preheater, 4 is a deamination tower, 5 is a gas-liquid separator, 6 is a reboiler, 7 is a tower bottom discharge pump, 8 is a tower bottom liquid cooler, 9 is an ammonia water product pump, 10 is an ammonia water cooler, 11 is an ammonia water product storage tank, 12 is an ammonia water reflux pump, 91 is a tower top condenser, and 101 is a condensate tank.
Detailed Description
The present invention is described in terms of particular embodiments, other advantages and features of the utility model will become apparent to those skilled in the art from the following disclosure, and it is to be understood that the described embodiments are merely exemplary of the utility model and that it is not intended to limit the utility model to the particular embodiments disclosed. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Embodiment a system for evaporating ammonia to ammonia-containing nitrogen-doped salt wastewater
As shown in fig. 1, the system according to an embodiment of the present invention includes a feed pump 1, a first preheater 2, a second preheater 3, a deamination tower 4, a gas-liquid separator 5, a reboiler 6, a tower bottom discharge pump 7, a tower bottom cooler 8, an ammonia water product pump 9, an ammonia water cooler 10, and an ammonia water product storage tank 11;
the feeding pump 1 performs steam heat exchange with the top end of the gas-liquid separator 5 through the first preheater 2, gas in the gas-liquid separator 5 is connected with the ammonia water product pump 9 through the first preheater 2 by the gas-liquid separator 5, and ammonia gas discharged from the ammonia water product pump 9 enters the ammonia water product storage tank 11 through the ammonia water cooler 10;
the feed pump 1 exchanges heat with a discharge hole at the bottom end of the deamination tower 4 through the first preheater 2, the second preheater 3 and the tower kettle discharge pump 7, and the tower bottom of the deamination tower 4 is connected with the tower kettle liquid cooler 8 through the tower kettle discharge pump 7 and the second preheater 3; the feed pump 1 is connected with a deamination tower 4 through a first preheater 2 and a second preheater 3; the tower bottom of the deamination tower 4 is connected with a reboiler 6 to keep hydraulic stability;
the method for carrying out ammonia distillation treatment on ammonia-containing aza-salt wastewater based on the system shown in figure 1 comprises the following specific materials and steps:
a system for carrying out ammonia distillation treatment on ammonia-containing nitrogen-doped salt wastewater and a using method thereof are disclosed, and a system diagram is shown in figure 1, and the specific steps are as follows:
the ammonia-containing aza-salt wastewater has a flow of 56625.3kg/h, a temperature of 30 ℃, a pH value of 11, an ammonia nitrogen content of 0.884 percent and Na2SO4The content was 13.82%, the Ni content was 0.013%, the Co content was 30.87ppm, and the Mn content was 30.87 ppm.
Waste water is pressurized by the feed pump 1 and then subjected to steam heat exchange with the top end of the gas-liquid separator 5 through the first preheater 2, the temperature of the waste water is increased to 69.56 ℃, and then the waste water is subjected to heat exchange with the bottom discharge of the deamination tower 4 through the second preheater 3, and the temperature of the waste water is increased to 95.25 ℃.
The deamination tower 4 is a plate tower, the number of theoretical plates is 30, a gas-liquid separator 5 is arranged at the top of the tower, and the gas-liquid separator 5 is a wire mesh demister; the feed plate was theoretical plate 1 and the top operating pressure was 100 kPa. A reboiler 6 is arranged at the bottom of the deamination tower 4, and the reboiler 6 is a vertical thermosyphon reboiler; the steam at the top of the gas-liquid separator 5 is fully extracted, the extraction amount is 3300kg/h, and the temperature is 96.27 ℃; the steam at the top of the gas-liquid separator 5 is subjected to heat exchange by the first preheater 2 and then condensed into ammonia water, the condensation temperature is 35.44 ℃, the condensed ammonia water is pressurized by the ammonia water product pump 9 and then enters the ammonia water cooler 10 to be subjected to heat exchange with circulating water, the temperature of the condensed ammonia water is reduced to 32 ℃, and the condensed ammonia water enters the ammonia water product storage tank 11 for recycling.
The discharged material at the bottom of the deamination tower 4 enters a second preheater 3 after being pressurized by a tower kettle discharge pump 7 to exchange heat with the wastewater, the discharged material is cooled to 73.33 ℃, and then is cooled to below 32 ℃ by a tower kettle liquid cooler 8, and enters a downstream working section to carry out operations such as dosing, precipitation, evaporative crystallization and the like.
Comparative example 1 Single-tower System for Ammonia distillation of Ammonia-containing miscellaneous salt wastewater and method for Ammonia distillation of Ammonia-containing miscellaneous salt wastewater by Using the same
The system is shown in fig. 2, and comprises a feed pump 1, a first preheater 2, a second preheater 3, a deamination tower 4, a gas-liquid separator 5, a reboiler 6, a tower bottom discharge pump 7, a tower bottom liquid cooler 8, a tower top condenser 91, a condensate tank 101, an ammonia water product pump 9, an ammonia water reflux pump 12, an ammonia water cooler 10 and an ammonia water product storage tank 11;
the treatment method comprises the following specific steps:
an ammonia-containing miscellaneous salt wastewater with flow rate of 56625.3kg/h, temperature of 30 deg.C, pH value of 11, ammonia nitrogen content of 0.884%, and Na content2SO4The content was 13.82%, the Ni content was 0.013%, the Co content was 30.87ppm, and the Mn content was 30.87 ppm.
The wastewater is pressurized by a feed pump 1, then exchanges heat with the bottom discharge of a deamination tower 4 through a first preheater 2 via a tower kettle discharge pump 7, the temperature rises to 68 ℃, and then exchanges heat with the condensate water of the deamination tower 4 and a reboiler 6 through a second preheater 3, and the temperature rises to 95.25 ℃;
the deamination tower 4 is a plate tower, the number of theoretical plates is 30, the feeding plate is a 15 th theoretical plate, and the operation pressure at the top of the tower is 100 kPa; the top of the gas-liquid separator 5 is provided with a tower top condenser 91, the steam at the tower top is totally condensed into ammonia water in the tower top condenser 91 and enters a condensate tank 101, then the ammonia water is extracted by an ammonia water product pump 9, and part of the steam flows back to the tower top by an ammonia water reflux pump 12, the reflux ratio is 3, and the reflux temperature is 55.42 ℃; the extraction amount at the top of the tower is 3300kg/h, and the product at the top of the tower exchanges heat with circulating water through an ammonia water cooler 10 and is cooled to 32 ℃, and then enters an ammonia water product storage tank 11 for recycling; a reboiler 6 is arranged at the bottom of the deamination tower 4, and the reboiler 6 is a vertical thermosyphon reboiler;
the discharged material at the bottom of the deamination tower 4 enters a first preheater 2 after being pressurized by a tower kettle discharge pump 7 to exchange heat with the raw material and reduce the temperature to 35 ℃, and then is reduced to below 32 ℃ by a tower kettle liquid cooler 8 and enters a downstream working section to carry out operations such as dosing precipitation, evaporative crystallization and the like.
Comparative example 2 Single-tower System for Ammonia distillation of Ammonia-containing miscellaneous salt wastewater and method for Ammonia distillation treatment of Ammonia-containing miscellaneous salt wastewater by utilizing the System
The system is shown in fig. 3, and comprises: the system comprises a feed pump 1, a first preheater 2, a second preheater 3, a deamination tower 4, a gas-liquid separator 5, a tower kettle discharge pump 7, a tower kettle liquid cooler 8, an ammonia water product pump 9, an ammonia water cooler 10 and an ammonia water product storage tank 11;
the treatment method comprises the following specific steps:
an ammonia-containing miscellaneous salt wastewater with flow rate of 56625.3kg/h, temperature of 30 deg.C, pH value of 11, ammonia nitrogen content of 0.884%, and Na content2SO4The content was 13.82%, the Ni content was 0.013%, the Co content was 30.87ppm, and the Mn content was 30.87 ppm.
The raw materials are pressurized by a feed pump 1 and then subjected to heat exchange with the steam discharged from the top of a gas-liquid separator 5 through a first preheater 2, the temperature is raised to 69.58 ℃, and then the raw materials are subjected to heat exchange with the discharged material from the bottom of a deamination tower 4 through a second preheater 3, and the temperature is raised to 95.25 ℃.
The deamination tower 4 is a plate tower, the number of theoretical plates is 30, a gas-liquid separator 5 is arranged at the top of the tower, and the gas-liquid separator 5 is a wire mesh demister; the feed plate was theoretical plate 1 and the overhead operating pressure was 97.2 kPa. Steam is fed from the bottom of the tower, the flow rate of the steam is 3610kg/h, the temperature is 101 ℃, and the pressure is 105 kPa; the steam at the top of the gas-liquid separator 5 is fully extracted, the extraction amount is 3300kg/h, and the temperature is 95.5 ℃; steam at the top of the gas-liquid separator 5 is subjected to heat exchange and condensation by the first preheater 2 to form ammonia water at the temperature of 34.62 ℃, then is pressurized by the ammonia water product pump 9 to enter the ammonia water cooler 10 to perform heat exchange with circulating water and reduce the temperature to 32 ℃, and then enters the ammonia water product storage tank 11 for recycling.
The discharged material at the bottom of the deamination tower 4 enters a second preheater 3 after being pressurized by a tower kettle discharge pump 7 to exchange heat with the raw material and reduce the temperature to 74.44 ℃, and then is reduced to below 32 ℃ by a tower kettle liquid cooler 8 and enters a downstream working section to carry out operations such as dosing, precipitation, evaporative crystallization and the like.
Examples of the experiments
The energy consumption, the ammonia recovery rate and the water content of the discharged material of the tower bottom of the ammonia distillation tower in the whole process of the embodiment, the comparative example 1 and the comparative example 2 of the utility model are measured, and the results are shown in the table 1.
TABLE 1 comparison table of energy consumption, ammonia recovery rate and water content in tower bottom discharge
| Energy consumption of ammonia still | Recovery of ammonia | Water content in tower bottom discharge | |
| Examples of the utility model | 8378256.77kj/h | 99.9％ | 45469.68kg/h |
| Comparative example 1 | 31822856.7kj/h | 99.9％ | 45469.96kg/h |
| Comparative example 2 | 9322553.02kj/h | 99.9％ | 49079.95kg/h |
As can be seen from Table 1, the energy consumption of the examples of the present invention is much smaller than that of comparative examples 1 and 2; the water content was also lower than that of comparative examples 1 and 2.
Although the utility model has been described in detail above with reference to a general description and specific examples, it will be apparent to one skilled in the art that modifications or improvements may be made thereto based on the utility model. Accordingly, such modifications and improvements are intended to be within the scope of the utility model as claimed.
Claims (5)
1. A system for carrying out ammonia distillation treatment on ammonia-containing nitrogen-containing salt wastewater is characterized by comprising a feeding pump (1), a first preheater (2), a second preheater (3), a deamination tower (4), a gas-liquid separator (5), a reboiler (6), a tower kettle discharge pump (7), a tower kettle liquid cooler (8), an ammonia water product pump (9), an ammonia water cooler (10) and an ammonia water product storage tank (11);
the feeding pump (1) is connected with a gas-liquid separator (5) through a first preheater (2), the gas-liquid separator (5) is connected with an ammonia water product pump (9) through the first preheater (2), and the ammonia water product pump (9) is connected with an ammonia water product storage tank (11) through an ammonia water cooler (10);
the feed pump (1) is connected with the top end of the deamination tower (4) through the first preheater (2) and the second preheater (3), and the bottom of the deamination tower (4) is connected with the tower bottom liquid cooler (8) through the tower bottom discharge pump (7) and the second preheater (3); the bottom of the deamination tower (4) is connected with a reboiler (6).
2. The system for carrying out ammonia distillation treatment on the waste water containing ammonia nitrogen salt according to claim 1, characterized in that the deamination tower (4) is a packed tower.
3. The system for carrying out ammonia distillation treatment on the waste water containing ammonia nitrogen salts according to claim 1, characterized in that the deamination tower (4) is a plate tower.
4. The system for the ammonia distillation treatment of the waste water containing ammonia and nitrogen heterocyclic salt as claimed in claim 1, characterized in that the gas-liquid separator (5) is a wire mesh demister.
5. The system for ammonia distillation treatment of wastewater containing ammonia and nitrogen heterocyclic salt as claimed in claim 1, characterized in that the reboiler (6) is a vertical thermosiphon reboiler.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121586178.0U CN215403194U (en) | 2021-07-13 | 2021-07-13 | System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater |
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| CN202121586178.0U CN215403194U (en) | 2021-07-13 | 2021-07-13 | System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113651380A (en) * | 2021-07-13 | 2021-11-16 | 北京航天环境工程有限公司 | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113651380A (en) * | 2021-07-13 | 2021-11-16 | 北京航天环境工程有限公司 | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater |
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Granted publication date: 20220104 |