CN113651380A - System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater - Google Patents
System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater Download PDFInfo
- Publication number
- CN113651380A CN113651380A CN202110791456.4A CN202110791456A CN113651380A CN 113651380 A CN113651380 A CN 113651380A CN 202110791456 A CN202110791456 A CN 202110791456A CN 113651380 A CN113651380 A CN 113651380A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tower
- wastewater
- preheater
- pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses a system and a method 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 method comprises the steps of waste water heat exchange, tower entering treatment, ammonia distillation and condensation recovery. According to the invention, 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. The tower bottom of the invention 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 invention relates to the field of wastewater treatment, in particular to a system and a method 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 invention provides a system and a method for carrying out ammonia distillation treatment on ammonia-containing nitrogen-doped salt wastewater, and 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 invention provides the following technical scheme:
according to one aspect of the invention, 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 a first preheater, the gas-liquid separator is connected with an ammonia water product pump through the first preheater, and the ammonia water product pump is connected with an ammonia water product storage tank through an 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 invention has the following advantages:
1. according to the invention, 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 invention 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 invention 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 invention and that it is not intended to limit the invention 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.
The embodiment of the invention provides a system for carrying out ammonia distillation treatment on ammonia-containing aza-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 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 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:
the flow rate of the waste water containing ammonia nitrogen salt is 56625.3kg/h, the temperature is 30 ℃, the pH value is 11, the content of ammonia nitrogen is 0.884 percent, and Na is added2SO4The 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 invention 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 invention | 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 invention 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 invention. Accordingly, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (10)
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.
6. A method for treating ammonia evaporation treatment of waste water containing ammonia nitrogen salt by using the system of any one of claims 1 to 5, which is characterized by comprising the following steps:
the wastewater is pressurized by a feed pump (1), passes through a first preheater (2) to exchange heat with the tower top steam of a gas-liquid separator (5), and then passes through a second preheater (3) and a tower kettle discharge pump (7) to exchange heat with the tower bottom discharge;
feeding the wastewater preheated by the two steps from the upper part of a first theoretical plate of the deamination tower (4), wherein secondary steam generated at the bottom of the deamination tower (4) and a reboiler (6) and liquid added above the first theoretical plate of the deamination tower (4) form gas-liquid balance; steam in the gas-liquid separator (5) is subjected to heat exchange with wastewater entering through the feed pump (1) through the first preheater (2) and condensed into ammonia water, then passes through the ammonia water product pump (9), is subjected to heat exchange with circulating water in the ammonia water cooler (10) and is cooled, and then enters the ammonia water product storage tank (11);
and the product at the bottom of the deamination tower (4) passes through a tower kettle discharge pump (7) and a second preheater (3), then passes through a tower kettle liquid cooler (8) to exchange heat with circulating water and be cooled, and finally is discharged out of the system.
7. The method for performing ammonia distillation treatment on ammonia-containing nitrogen-and-nitrogen-containing salt wastewater by using the system as claimed in claim 6, wherein the temperature of the wastewater is 90-100 ℃ after the wastewater is preheated twice.
8. The method for performing ammonia distillation treatment on ammonia-containing nitrogen-and-salt-containing wastewater by using the system as claimed in claim 6, wherein the steam in the gas-liquid separator (5) is subjected to heat exchange with the wastewater entering through the feed pump (1) through the first preheater (2) and condensed into ammonia water, and the condensation temperature of the ammonia water is 30-57 ℃.
9. The method for performing ammonia distillation treatment on ammonia-containing nitrogen-and-nitrogen salt-containing wastewater by using the system as claimed in claim 6, wherein the operation pressure at the top of the deamination tower (4) is 80-105 kPa, and the pressure drop of the whole deamination tower (4) is 0-20 kPa.
10. The method for treating ammonia-containing nitrogen-and-nitrogen-containing salt wastewater by ammonia distillation by using the system as claimed in claim 6, wherein the operating pressure of the reboiler (6) is 100 to 120 kPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110791456.4A CN113651380A (en) | 2021-07-13 | 2021-07-13 | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110791456.4A CN113651380A (en) | 2021-07-13 | 2021-07-13 | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113651380A true CN113651380A (en) | 2021-11-16 |
Family
ID=78478008
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110791456.4A Pending CN113651380A (en) | 2021-07-13 | 2021-07-13 | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113651380A (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101264948A (en) * | 2008-04-25 | 2008-09-17 | 北京化工大学 | Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method |
| CN101475842A (en) * | 2008-12-11 | 2009-07-08 | 中冶焦耐工程技术有限公司 | Ammonia distillation process |
| CN101863523A (en) * | 2010-05-21 | 2010-10-20 | 赛鼎工程有限公司 | Method for treating ammonia-containing waste water from crushed coal pressure gasification |
| CN103736286A (en) * | 2014-01-22 | 2014-04-23 | 象山医疗精密仪器有限公司 | High-efficiency and energy-saving concentrator and evaporation concentration method of liquid materials |
| CN104843813A (en) * | 2014-12-30 | 2015-08-19 | 中国天辰工程有限公司 | Coal gasification high ammonia nitrogen wastewater treatment process |
| US20210002147A1 (en) * | 2017-04-21 | 2021-01-07 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN215403194U (en) * | 2021-07-13 | 2022-01-04 | 北京航天环境工程有限公司 | System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater |
-
2021
- 2021-07-13 CN CN202110791456.4A patent/CN113651380A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101264948A (en) * | 2008-04-25 | 2008-09-17 | 北京化工大学 | Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method |
| CN101475842A (en) * | 2008-12-11 | 2009-07-08 | 中冶焦耐工程技术有限公司 | Ammonia distillation process |
| CN101863523A (en) * | 2010-05-21 | 2010-10-20 | 赛鼎工程有限公司 | Method for treating ammonia-containing waste water from crushed coal pressure gasification |
| CN103736286A (en) * | 2014-01-22 | 2014-04-23 | 象山医疗精密仪器有限公司 | High-efficiency and energy-saving concentrator and evaporation concentration method of liquid materials |
| CN104843813A (en) * | 2014-12-30 | 2015-08-19 | 中国天辰工程有限公司 | Coal gasification high ammonia nitrogen wastewater treatment process |
| US20210002147A1 (en) * | 2017-04-21 | 2021-01-07 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN215403194U (en) * | 2021-07-13 | 2022-01-04 | 北京航天环境工程有限公司 | System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108275819B (en) | Method for recycling ternary precursor washing wastewater | |
| CN207877494U (en) | Lithium battery nickel-cobalt-manganese ternary presoma waste water treatment system | |
| CN102642881B (en) | Device and method for steam stripping of condensate in water gas conversion process | |
| CN107235593A (en) | The system and method that a kind of coal gasification water system recovery ammonia is removed with sulphur | |
| CN103274489A (en) | Negative-pressure ammonia distillation process and device taking crude gas waste heat as heat source | |
| CN215403194U (en) | System for evaporating ammonia treatment to ammonia-containing aza-salt wastewater | |
| CN105366751A (en) | Energy-saving environment-friendly integrated recycling and utilization method of coal chemical gasification washing black water high-temperature flashing steam | |
| CN207877495U (en) | A kind of positive ternary precursor wastewater treatment equipment of lithium electricity | |
| CN104817481A (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN103588615B (en) | Device and technology for recovery of tetrachloroethylene | |
| CN105130079A (en) | Treatment process combining H acid mother solution and T acid mother solution | |
| CN114272871A (en) | System and method for preparing NMP (N-methyl pyrrolidone) by taking maleic anhydride as raw material | |
| CN113651380A (en) | System and method for ammonia distillation treatment of ammonia-containing aza-salt wastewater | |
| CN203402928U (en) | Resourceful treatment process system for ammonia-containing waste gas/steam in production process of ammonium paratungstate | |
| CN203307083U (en) | Negative pressure ammonia distiller by using raw gas waste heat as heat source | |
| CN205556409U (en) | Benzene hydrogenation waste water desulfurization deamination processing apparatus | |
| CN212222702U (en) | High-efficient low temperature negative pressure ammonia nitrogen waste water strip system | |
| CN108129266A (en) | A kind of process for detaching high-moisture low carbon mixed alcohol | |
| CN203916121U (en) | DMAC reclaims physical property index optimization system | |
| CN216756389U (en) | System for use maleic anhydride as raw materials preparation NMP | |
| CN105884106A (en) | Benzene hydrogenation wastewater desulfurization and deamination treatment method aiming at improving deamination and treatment device applying same | |
| CN105217654B (en) | Alkylation waste sulfuric acid recycling treatment device and method | |
| CN214973960U (en) | Production device for preparing high-molecular polymer intermediate through esterification reaction | |
| CN212532809U (en) | Pre-concentration device of urea low-pressure system | |
| CN212262410U (en) | Deamination tower system that TVR condensate water was retrieved |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |