CN212222702U - High-efficient low temperature negative pressure ammonia nitrogen waste water strip system - Google Patents
High-efficient low temperature negative pressure ammonia nitrogen waste water strip system Download PDFInfo
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- CN212222702U CN212222702U CN202020748013.8U CN202020748013U CN212222702U CN 212222702 U CN212222702 U CN 212222702U CN 202020748013 U CN202020748013 U CN 202020748013U CN 212222702 U CN212222702 U CN 212222702U
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Abstract
The utility model discloses a high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system, which comprises an ammonia distillation tower, an ammonia absorption tower, a steam ejector, a flash tank, a condenser, a gas-liquid separator and a pipeline; the ammonia still is arranged at the front end of the ammonia absorption tower, a vacuum pump arranged in front of the ammonia absorption tower is used for providing negative pressure for the ammonia still, under the negative pressure operation, the pressure in the ammonia still is lower, the solubility of ammonia in water is reduced, and the ammonia is easier to evaporate, so that the steam consumption is saved; the ammonia distillation wastewater from the ammonia distillation tower is partially vaporized by adopting the ammonia distillation ejector and the flash tank, secondary steam is recovered, the direct steam consumption of ammonia distillation is reduced, and the energy consumption problem of ammonia distillation is improved. The utility model discloses make full use of aqueous ammonia heat exchange technology utilizes the negative pressure operation, carries out the heat transfer with raw materials ammonia nitrogen waste water and the discharged ammonia still waste water at the bottom of the tower, retrieves the heat of ammonia still waste water, the low temperature waste heat resource of make full use of ammonia still waste water.
Description
Technical Field
The utility model relates to a waste water treatment facility specifically is a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system.
Background
In recent years, with the development of economy, more and more nitrogen-containing pollutants are randomly discharged to cause great harm to the environment. The nitrogen exists in various forms such as organic nitrogen, ammonia nitrogen, nitrate nitrogen, nitrite nitrogen and the like in the wastewater, and the ammonia nitrogen is one of the most main existing forms. The ammonia nitrogen in the wastewater refers to nitrogen existing in two forms of free ammonia and ionic ammonium salt, and mainly comes from industrial wastewater such as decomposition of nitrogenous organic matters in domestic sewage, coking, synthetic ammonia and the like, farmland drainage and the like. The ammonia nitrogen pollution sources are many, the discharge amount is large, and the discharge concentration change is large. The concentration and the water quantity of the ammonia nitrogen wastewater discharged by enterprises in different industries and scales are greatly different, and in treatment, the high-concentration ammonia nitrogen wastewater needs to be treated by using a process, and can reach the treatment standard by combining various processes or adding auxiliary agents for treatment. The high ammonia nitrogen wastewater mainly comes from industries and the like, and the ammonia nitrogen content of the high ammonia nitrogen wastewater reaches 1000-10000 mg/L. The high-concentration ammonia nitrogen wastewater mainly comes from industrial production processes of steel, oil refining, chemical fertilizers, inorganic chemical industry, ferroalloy, glass manufacturing, meat processing, feed production, garbage leachate, monosodium glutamate production, coal chemical industry, nonferrous metal smelting and the like.
At present, ammonia nitrogen wastewater treatment technologies can be divided into two major categories: one type of technology is a biological denitrification technology, for example, Chinese patent invention publication No. CN105600923A with publication No. of 2016, 6, 25 and 2016 discloses a biological denitrification process for high ammonia nitrogen wastewater, which generally has the disadvantages of long flow, large reactor, large occupied area, frequent need of additional carbon source, high energy consumption and high cost, and generally can only treat low ammonia nitrogen wastewater; the other is a physicochemical treatment technology, including stripping (steam stripping), precipitation, membrane absorption, wet oxidation and the like, wherein the stripping method has the advantages of simple process, stable effect and low investment, and is a commonly used physicochemical denitrification technology at present. However, the stripping method has some disadvantages, such as frequent scaling in the stripping tower, low ammonia nitrogen removal efficiency at low temperature, high energy consumption, high treatment cost, and about 20-30 yuan/ton water treatment cost. The ammonia nitrogen in the effluent is about 50-200 mg/L, the emission requirement cannot be met, and the emission can reach the standard only by adding subsequent advanced treatment.
The ammonia nitrogen wastewater treatment method based on stripping and simple stripping has the problems of secondary pollution, high operation cost and the like, and the ammonia water recovery method is generally adopted in the ammonia still stripping process at the present stage and is widely applied to ammonia nitrogen wastewater treatment in production. At present, the ammonia distillation process faces a series of problems of large steam consumption, general ammonia distillation effect, high operation cost and the like, wherein the problem of energy consumption in the ammonia distillation process is very interesting. The method has better practical significance for the research on energy conservation of the ammonia distillation process, particularly the research on the aspect of reducing the unit consumption of steam.
SUMMERY OF THE UTILITY MODEL
The utility model discloses there is steam consumption height, waste water to traditional ammonia nitrogen waste water strip technology, contains the high scheduling problem of ammonia, provides a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system, and this system can obviously reduce the degree of corrosion of aqueous ammonia to ammonia still, alleviates subsequent processing's pressure simultaneously, can also reduce direct steam consumption, reduces direct steam unit consumption under negative pressure operating condition.
The technical scheme of the utility model as follows:
the utility model provides a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system which characterized in that: mainly comprises an ammonia still, an ammonia absorption tower, a steam ejector, a flash tank, a condenser, a gas-liquid separator and a wastewater preheater;
a waste water inlet at the upper part of the ammonia still is connected with waste water through a pipeline, and a steam inlet at the lower part of the ammonia still is connected to steam sprayed at a high speed by a steam ejector through a pipeline;
the deamination wastewater outlet at the bottom of the ammonia still is respectively connected with two pipelines, one pipeline is connected to a wastewater outlet pipe through heat exchange equipment, and the other pipeline is connected to a steam ejector through the flash tank;
ammonia-containing gas in the ammonia still is discharged through a gas outlet at the top of the ammonia still, the gas outlet at the top of the ammonia still is connected to a gas inlet of a condenser, ammonia and water vapor condensed by the condenser are discharged through a gas-liquid outlet at the bottom of the condenser, the gas-liquid outlet at the bottom of the condenser is connected to an inlet of a gas-liquid separator, and a liquid outlet at the bottom of the gas-liquid separator is connected to a concentrated ammonia water inlet at the upper part of the ammonia still through a pipeline;
the ammonia gas that vapour and liquid separator separated is discharged through the gas outlet at vapour and liquid separator top, gets into the ammonia absorption tower through the vacuum pump, is provided with the ammonia water pump on the ammonia water exit linkage's of ammonia absorption tower bottom the pipeline, divide into through the ammonia water pump and connect two way pipelines, is ammonia water product outlet pipeline all the way, is connected to the ammonia entry on the ammonia absorption tower all the way and forms ammonia water circulation absorption pipeline.
Steam connected to a steam pipeline and mixed steam formed by secondary evaporation of the flash tank are collected in the steam ejector and are connected to the ammonia still; the operating pressure in the flash tank is controlled by a steam ejector.
The front end of the waste water inlet on the upper part of the ammonia still is connected with a waste water preheater, the front end of the waste water preheater is provided with a proportional mixer, the proportional mixer is connected with corresponding medicament and waste water, in the proportional mixer, the waste water passes through the medicament to adjust the pH value, and the waste water after the pH value is adjusted enters the ammonia still through the waste water preheater.
And a high-temperature deamination wastewater outlet at the bottom of the ammonia distillation tower is connected with a heat exchange device to form the wastewater preheater, and the heat of the high-temperature deamination wastewater is utilized to exchange heat to preheat and heat the wastewater with the pH value adjusted.
Be provided with the deamination water pump between the high temperature deamination waste water export of ammonia distillation tower bottom and the waste water pre-heater, through the deamination water pump most high temperature deamination waste water pump income waste water pre-heater.
And a reflux pump is arranged on a pipeline connected with a liquid outlet at the bottom of the gas-liquid separator, and the separated concentrated ammonia water is totally refluxed into the ammonia still through the reflux pump.
And the ammonia gas discharged from an ammonia gas outlet at the upper end of the condenser and the ammonia gas separated by the gas-liquid separator are converged into a pipeline and pumped into an ammonia gas absorption tower through a vacuum pump. Wherein, the mass concentration of the ammonia gas pumped by the vacuum pump reaches the corresponding order of magnitude according to the operation condition.
And after an ammonia water outlet of the ammonia gas absorption tower passes through an ammonia water pump, a part of concentrated ammonia water is taken as a product and is sent out through an ammonia water product pipeline, and the other part of concentrated ammonia water is cooled by a cooler and is circularly connected to an ammonia gas inlet on the ammonia gas absorption tower, so that the ammonia absorption effect is enhanced.
A wastewater pump is arranged on a wastewater feeding pipeline at the front end of the proportional mixer, and wastewater is pumped into the proportional mixer through the wastewater pump; and a medicament pump is arranged at the medicament feeding end at the front end of the proportional mixer, and the medicament is pumped into the proportional mixer through the medicament pump.
The low-temperature negative-pressure steam stripping working principle of the system is as follows:
firstly, ammonia-containing wastewater is pumped into a proportional mixer through a wastewater feeding pipeline and a wastewater pump, a medicament (namely a pH regulator) is pumped into the proportional mixer through a medicament feeding pipeline and a medicament pump, the ammonia-containing wastewater and the medicament are mixed in the proportional mixer to regulate the pH value of the wastewater, and the ammonia-containing wastewater after the pH value is regulated exchanges heat with high-temperature deamination wastewater at the bottom of an ammonia still in a wastewater preheater and then enters the ammonia still after being heated;
in the stripping section of the ammonia still, ammonia-containing wastewater moves from top to bottom, and is converted into ammonia gas to be removed after being in countercurrent contact with direct steam from the bottom of the ammonia still, and high-temperature deamination wastewater is generated at the bottom of the ammonia still; most of the high-temperature deamination wastewater enters a wastewater preheater through a deamination water pump for heat exchange and temperature reduction, the deamination wastewater after temperature reduction is sent to a wastewater outlet pipeline, and the other part of the high-temperature deamination wastewater enters a flash tank from the bottom of an ammonia still so that the part of the high-temperature deamination wastewater is secondarily evaporated in the flash tank to form secondary ammonia-containing steam, and then the secondary ammonia-containing steam is recovered to a steam ejector;
meanwhile, high-pressure steam as a working medium enters a steam ejector through a steam pipeline, steam kinetic energy is converted into static pressure energy through high-speed injection, the static pressure energy is mixed with recycled secondary ammonia-containing steam to form mixed steam, the mixed steam enters an ammonia still to evaporate ammonia, and the secondary ammonia-containing steam is recycled;
in the ammonia still, the ammonia-containing gas enriched at the top of the tower enters a condenser, ammonia and water vapor in the condenser are condensed by circulating water and then enter a gas-liquid separator, and the separated strong ammonia water completely flows back to the ammonia still through a reflux pump.
Pumping high-concentration ammonia gas extracted from the condenser and the gas-liquid separator into an ammonia gas absorption tower through a vacuum pump; then the absorption liquid from outside enters an ammonia absorption tower through an absorption liquid pipeline, ammonia is absorbed into conventional concentrated ammonia water (the concentration of the conventional concentrated ammonia water is about 20 percent (wt), which is generally determined according to the operation condition), a part of the concentrated ammonia water is taken as a product through an ammonia water pump and is delivered out of a factory through an ammonia water product pipeline, and a part of the concentrated ammonia water is cooled by a cooler to enhance the ammonia absorption effect.
The utility model provides a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system has following advantage:
(1) the vacuum pump is adopted to provide negative pressure for the front-end ammonia still, and under the negative pressure operation, the ammonia gas is easier to evaporate due to the lower pressure in the ammonia still and the reduced solubility of the ammonia gas in water, thereby saving the steam consumption. Along with the reduction of the pressure, the operation temperature in the ammonia still is reduced, the temperature of the ammonia-containing gas coming out from the top of the tower is lower, and the pressure on a condenser is reduced.
(2) The ammonia distillation wastewater is partially vaporized by adopting the ammonia distillation ejector and the flash tank, secondary steam is recovered, the direct steam consumption of the ammonia distillation is further reduced, the problem of high energy consumption of the ammonia distillation is solved, and the steam unit consumption of the system is at the level of 80kg/t (wastewater).
(3) Part of volatile residual ammonia in the ammonia distillation wastewater is recycled in the process of secondary evaporation of the ammonia distillation wastewater in the flash tank, so that the ammonia content of the ammonia distillation wastewater is further reduced; meanwhile, the latent heat of the wastewater is utilized, the recovery rate of ammonia gas is improved, and the content of ammonia nitrogen in the wastewater is reduced to below 15 mg/L.
(4) The ammonia-nitrogen wastewater as the raw material is subjected to heat exchange with the ammonia distillation wastewater discharged from the bottom of the tower by adopting an ammonia-water heat exchange technology, so that the heat of the ammonia distillation wastewater is recovered, and the low-temperature waste heat resource of the ammonia distillation wastewater is fully utilized.
Drawings
Fig. 1 is a schematic diagram of a system structure of the present invention.
Wherein the reference numerals are: 1 lye pump, 2 waste water pump, 3 proportioner, 4 waste water preheater, 5 steam ejector, 6 ammonia still, 7 flash tanks, 8 deamination water pump, 9 condenser, 10 vapour and liquid separator, 11 reflux pump, 12 vacuum pump, 13 ammonia absorption tower, 14 cooler, 15 ammonia pump, 16 alkali lye feed pipes, 17 waste water feed pipes, 18 steam conduit, 19 waste water outlet pipe, 20 condenser's cooling water inlet pipe, 21 condenser's cooling water outlet pipe, 22 absorption liquid pipeline, 23 cooler's cooling water inlet pipe, 24 cooler's cooling water outlet pipe, 25 ammonia product pipeline.
Detailed Description
The invention will be described in further detail with reference to the following detailed description and accompanying drawings:
example 1
The utility model discloses a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system mainly includes ammonia still 6, ammonia absorption tower 13, steam ejector 5, flash tank 7, condenser 9, vapour and liquid separator 10, waste water pre-heater 4.
The specific connection design of main equipment and pipelines in the system is as follows:
the upper part of the ammonia still 6 is provided with a wastewater inlet, the wastewater inlet is connected with wastewater through a corresponding pipeline, the lower part of the ammonia still 6 is provided with a steam inlet, the steam inlet is connected with the steam ejector 5 through a corresponding pipeline, and steam is ejected at a high speed through the steam ejector 5;
the bottom of the ammonia still 6 is provided with a high-temperature deamination wastewater outlet which is respectively connected with two pipelines, one pipeline is connected to a wastewater outlet pipeline 19 through heat exchange equipment, and the other pipeline is connected to the steam ejector 5 through a flash tank 7; in the embodiment, the temperature of the high-temperature deamination wastewater at the bottom of the ammonia still 6 can reach 85 ℃;
the ammonia-containing gas in the ammonia still 6 is discharged through a gas outlet at the top of the ammonia still 6, the gas outlet at the top of the ammonia still 6 is connected to a gas inlet of a condenser 9, the ammonia and water vapor condensed by the condenser 9 are discharged through a gas-liquid outlet at the bottom of the condenser 9, the gas-liquid outlet at the bottom of the condenser 9 is connected to an inlet of a gas-liquid separator 10, and a liquid outlet at the bottom of the gas-liquid separator 10 is connected to a concentrated ammonia water inlet at the upper part of the ammonia still 6 through a pipeline;
the top of the condenser 9 is respectively provided with a cooling water inlet pipeline 20 of the condenser and a cooling water outlet pipeline 21 of the condenser;
the ammonia gas separated by the gas-liquid separator 10 enters an ammonia gas absorption tower 13 through a gas outlet at the top of the gas-liquid separator 10;
an ammonia water pump 15 is arranged on a pipeline connected with an ammonia water outlet at the bottom of the ammonia gas absorption tower 13, the ammonia water pump 15 is divided into two pipelines, one pipeline is an ammonia water product outlet pipeline, and the other pipeline is connected to an ammonia gas inlet on the ammonia gas absorption tower 13 to form an ammonia water circulating absorption pipeline.
Example 2
Based on the structural design of the embodiment 1, steam is connected to a steam inlet of the steam ejector 5 through a steam pipeline 18, and the part of steam and steam secondarily evaporated by the flash tank 7 are converged to the steam ejector 5 to form mixed steam; subsequently, the mixed steam is introduced into an ammonia still 6.
Example 3
Based on the structural design of the embodiment 1 or 2, a waste water preheater 4 can be connected and arranged at the front end of a waste water inlet at the upper part of the ammonia still 6.
The front end of the waste water preheater 4 is provided with a proportional mixer 3, the proportional mixer is connected with corresponding medicament and waste water, the pH value of the waste water is adjusted in the proportional mixer, and the waste water with the adjusted pH value enters an ammonia still 6 through the waste water preheater 4.
Meanwhile, the high-temperature deamination waste water outlet at the bottom of the ammonia still 6 is connected with a heat exchange device, namely the waste water preheater 4, so that heat exchange is carried out by fully utilizing the heat of the high-temperature deamination waste water, and then the waste water after the pH value is adjusted is preheated and heated.
Example 4
Based on embodiment 3's structure, can set up deamination water pump 8 between the high temperature deamination waste water export of 6 bottoms in ammonia still and waste water pre-heater 4, through deamination water pump 8 with most high temperature deamination waste water pump in waste water pre-heater 4.
Example 5
Based on any structure of the above embodiments, a reflux pump 11 may be provided on the pipeline connected to the liquid outlet at the bottom of the gas-liquid separator 10, and the separated concentrated ammonia water is totally refluxed into the ammonia still 6 by the reflux pump 11.
Example 6
Based on any structure of the above embodiments, the ammonia gas discharged from the ammonia gas outlet at the upper end of the condenser 9 and separated by the gas-liquid separator 10 is collected into a pipeline, and is pumped into the ammonia gas absorption tower 13 through the vacuum pump 12 arranged on the pipeline. In the present embodiment, the mass concentration of the ammonia gas pumped by the vacuum pump 12 is about 90%.
Example 7
Based on any structure of the above embodiments, after the ammonia water outlet of the ammonia gas absorption tower 13 passes through the ammonia water pump 15, a part of concentrated ammonia water is sent out as a product through the ammonia water product pipeline, and the other part of concentrated ammonia water can be cooled by the cooler 14 and is circularly connected to the ammonia gas inlet on the ammonia gas absorption tower 13, so that the ammonia absorption effect is enhanced.
And a cooling water inlet pipeline 23 is arranged at the upper end of the side wall of the cooler 14, and a cooling water outlet pipeline 24 is arranged at the lower end of the side wall.
Example 8
Based on any structure of the embodiment, a wastewater pump 2 is arranged on a wastewater feeding pipeline at the front end of the proportional mixer, and wastewater is pumped into the proportional mixer through the wastewater pump 2; and a medicament pump is arranged at the medicament feeding end at the front end of the proportional mixer, and the medicament is pumped into the proportional mixer through the medicament pump.
By integrating the structure of the embodiment, the system realizes the low-temperature negative-pressure steam stripping work flow as follows:
(1) ammonia-containing wastewater is pumped into the proportional mixer through a wastewater feed pipe 17 by a wastewater pump 2;
(2) the reagent is a pH regulator, in this embodiment, an alkali liquor can be used, and is pumped into the proportioner 3 through the alkali liquor feeding pipeline 16 by the alkali liquor pump 1, the ammonia-containing wastewater and the reagent are mixed in the proportioner 3 to regulate the pH value of the wastewater, and the ammonia-containing wastewater after the pH value regulation exchanges heat with the high-temperature deamination wastewater at the bottom of the ammonia still 6 in the wastewater preheater 4 and then enters the ammonia still 6 after being heated;
(3) in a stripping section of the ammonia still 6, ammonia-containing wastewater moves from top to bottom, is in countercurrent contact with direct steam from the bottom of the tower and then is converted into ammonia gas to be removed, and high-temperature deamination wastewater is generated at the bottom of the tower;
(4) most of the high-temperature deamination wastewater enters a wastewater preheater 4 through a deamination water pump 8 to exchange heat and reduce the temperature, and then is sent to a wastewater outlet pipeline 19, and the other part of the high-temperature deamination wastewater enters a flash tank 7 from the bottom of an ammonia still 6, so that the ammonia still wastewater is secondarily evaporated in the flash tank 7 to form secondary steam, and then the secondary steam is recovered for recycling;
(5) high-pressure steam is adopted as a working medium, enters the steam ejector 5 through the steam pipeline 18, the kinetic energy of the steam is converted into static pressure energy through high-speed injection, secondary steam is sucked, and the obtained mixed steam is sent into the ammonia still 6 for ammonia distillation;
(6) the ammonia-containing gas enriched at the tower top of the ammonia still 6 enters a condenser 9, ammonia and water vapor in the condenser 9 are condensed by circulating water and then enter a gas-liquid separator 10, and the separated strong ammonia water completely flows back to the ammonia still 6 through a reflux pump 11;
(7) ammonia gas with the concentration of about 90 percent is extracted from the condenser 9 and the gas-liquid separator 10 and is pumped into an ammonia gas absorption tower 13 through a vacuum pump 12;
(8) the absorption liquid from outside enters the ammonia absorption tower 13 through an absorption liquid pipeline 22 to absorb ammonia into about 20 percent of concentrated ammonia water;
(9) the ammonia water pump 15 sends out a factory with a part of the strong ammonia water as a product through the ammonia water product pipeline 25, and a part of the strong ammonia water reduces the temperature of the absorption liquid through the cooler 14, so that the ammonia absorption effect is enhanced.
In the ammonia-containing wastewater treatment process, the ammonia still 6 is operated under negative pressure, the vacuum pump 12 arranged at the gas phase discharge position at the top of the tower is mainly used for forming negative pressure in the ammonia still, and in the negative pressure ammonia distillation process, the lower the pressure is, the less the steam consumption is. Under the negative pressure operation, the ammonia gas is easier to evaporate due to the lower pressure in the ammonia still 6 and the reduced solubility of the ammonia gas in water, thereby saving the steam consumption. As the pressure decreases, the operating temperature in the column decreases, and the temperature of the ammonia-containing gas coming out of the top of the column decreases, thereby relieving the pressure on the condenser 9. In addition, the operation temperature of the ammonia still 6 is reduced to reduce the corrosion degree of the ammonia still 6 caused by the ammonia water.
Compare traditional ammonia distillation flow, the utility model discloses be provided with steam ejector 5 and flash tank 7, operating pressure in the flash tank 7 is controlled by steam ejector 5, and the secondary steam of flash tank 7 export is sent into ammonia still 6 in through steam ejector 5 and direct steam mixture back and is evaporated ammonia. By utilizing the secondary steam, the problem of high energy consumption of ammonia distillation can be effectively improved, the unit consumption of direct steam is reduced, and the heat of ammonia distillation wastewater is recycled. And part of volatile residual ammonia in the wastewater is recovered in the secondary evaporation process of the ammonia distillation wastewater in the flash tank 7, so that the ammonia content of the ammonia distillation wastewater is further reduced. The steam consumption of each ton of wastewater of the system is about 80kg, and the ammonia nitrogen concentration of effluent is below 10 mg/ton.
The utility model adopts the flash evaporation means of steam injection to gasify part of ammonia distillation wastewater, and the latent heat in the wastewater is recovered; the heat of the ammonia distillation wastewater is used for heating the feeding ammonia water by adopting an ammonia water heat exchanger, and the sensible heat in the wastewater is recovered. The energy-saving benefit of the ammonia distillation energy-saving system using the steam injection flash evaporation device is much more than that of the ammonia distillation system only recovering sensible heat in wastewater through the heat exchanger, and the energy-saving benefit is very obvious in energy consumption saving aspect.
Claims (9)
1. The utility model provides a high-efficient low temperature negative pressure ammonia nitrogen waste water strip system which characterized in that: mainly comprises an ammonia still (6), an ammonia absorption tower (13), a steam ejector (5), a flash tank (7), a condenser (9) and a gas-liquid separator (10); a waste water inlet at the upper part of the ammonia still (6) is connected with waste water through a pipeline, and a steam inlet at the lower part of the ammonia still (6) is connected to steam sprayed by the steam ejector (5) through a pipeline; the high-temperature deamination wastewater outlet at the bottom of the ammonia still (6) is respectively connected with two pipelines, one pipeline is connected to a wastewater outlet pipeline (19) through heat exchange equipment, and the other pipeline is connected to a steam ejector (5) through a flash tank (7); ammonia-containing gas in the ammonia still (6) is discharged through a gas outlet at the top of the ammonia still (6), the gas outlet at the top of the ammonia still (6) is connected to a gas inlet of a condenser (9), ammonia and water vapor condensed by the condenser (9) are discharged through a gas-liquid outlet at the bottom of the condenser (9), the gas-liquid outlet at the bottom of the condenser (9) is connected to an inlet of a gas-liquid separator (10), and a liquid outlet at the bottom of the gas-liquid separator (10) is connected to an ammonia water inlet at the upper part of the ammonia still (6) through a pipeline; the ammonia gas that gas-liquid separator (10) separated out gets into ammonia absorption tower (13) through the gas outlet at gas-liquid separator (10) top, is provided with ammonia water pump (15) on the ammonia water exit linkage's of ammonia absorption tower (13) bottom the pipeline, divide into through ammonia water pump (15) and connect two way pipelines, be ammonia water product outlet pipeline all the way, be connected to the ammonia entry on ammonia absorption tower (13) all the way and form ammonia water circulation absorption pipeline.
2. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 1, characterized in that: steam collected by a steam collecting pipeline (18) in the steam ejector (5) and secondary evaporation of the flash tank (7) form mixed steam, and the mixed steam is connected to the ammonia still (6); the operating pressure in the flash tank (7) is controlled by a steam ejector (5).
3. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 1, characterized in that: the front end of a wastewater inlet on the upper part of the ammonia still (6) is connected with a wastewater preheater (4), the front end of the wastewater preheater (4) is provided with a proportional mixer (3), the proportional mixer (3) is connected with corresponding medicament and wastewater, and the wastewater coming out of the proportional mixer (3) enters the ammonia still (6) through the wastewater preheater (4).
4. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 3, characterized in that: the waste water preheater (4) is simultaneously used as heat exchange equipment connected with a high-temperature deamination waste water outlet at the bottom of the ammonia still (6).
5. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 3, characterized in that: a wastewater pump (2) is arranged on a wastewater feeding pipeline at the front end of the proportional mixer (3); a medicament pump is arranged at the medicament feeding end at the front end of the proportioning mixer (3).
6. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 3, characterized in that: and a deamination water pump (8) is arranged between the high-temperature deamination wastewater outlet at the bottom of the ammonia distillation tower (6) and the wastewater preheater (4).
7. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 1, characterized in that: and a reflux pump (11) is arranged on a pipeline connected with a liquid outlet at the bottom of the gas-liquid separator (10).
8. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 1, characterized in that: and an ammonia outlet at the upper end of the condenser (9) and an ammonia outlet of the gas-liquid separator (10) are connected to an ammonia absorption tower (13) through the same pipeline, and a vacuum pump (12) is arranged on the pipeline.
9. The high-efficiency low-temperature negative-pressure ammonia nitrogen wastewater stripping system according to claim 1, characterized in that: and an ammonia water outlet of the ammonia gas absorption tower (13) is connected with two paths of sending-out pipelines, one path of sending-out pipeline is a product pipeline passing through ammonia water, and the other path of sending-out pipeline is connected to a cooler (14) and is circularly connected to an ammonia gas inlet on the ammonia gas absorption tower (13) through the cooler (14).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113184936A (en) * | 2021-03-25 | 2021-07-30 | 宣化钢铁集团有限责任公司 | Efficient and energy-saving ammonia distillation deacidification system and method for recycling ammonia nitrogen |
| CN115200220A (en) * | 2022-06-22 | 2022-10-18 | 江苏科技大学 | High-temperature industrial waste water heat recovery and steam/hot water supply system and operation method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113184936A (en) * | 2021-03-25 | 2021-07-30 | 宣化钢铁集团有限责任公司 | Efficient and energy-saving ammonia distillation deacidification system and method for recycling ammonia nitrogen |
| CN115200220A (en) * | 2022-06-22 | 2022-10-18 | 江苏科技大学 | High-temperature industrial waste water heat recovery and steam/hot water supply system and operation method |
| CN115200220B (en) * | 2022-06-22 | 2023-11-21 | 江苏科技大学 | High-temperature industrial wastewater heat recovery and steam/hot water supply system and operation method |
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