CN111170389A - Ammonia stripping and distilling system and method for ammonia nitrogen wastewater - Google Patents
Ammonia stripping and distilling system and method for ammonia nitrogen wastewater Download PDFInfo
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- CN111170389A CN111170389A CN202010022318.5A CN202010022318A CN111170389A CN 111170389 A CN111170389 A CN 111170389A CN 202010022318 A CN202010022318 A CN 202010022318A CN 111170389 A CN111170389 A CN 111170389A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 288
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 144
- 239000002351 wastewater Substances 0.000 title claims abstract description 117
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000007791 liquid phase Substances 0.000 claims abstract description 56
- 238000004821 distillation Methods 0.000 claims abstract description 39
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 34
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 230000009615 deamination Effects 0.000 claims abstract description 13
- 238000006481 deamination reaction Methods 0.000 claims abstract description 13
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 33
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 15
- 239000012071 phase Substances 0.000 claims description 13
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- JGXQUVHKSJKROR-UHFFFAOYSA-N [N].N.N Chemical compound [N].N.N JGXQUVHKSJKROR-UHFFFAOYSA-N 0.000 claims 1
- 239000000498 cooling water Substances 0.000 description 8
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 206010028400 Mutagenic effect Diseases 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- XAYGUHUYDMLJJV-UHFFFAOYSA-Z decaazanium;dioxido(dioxo)tungsten;hydron;trioxotungsten Chemical compound [H+].[H+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].[NH4+].O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.O=[W](=O)=O.[O-][W]([O-])(=O)=O.[O-][W]([O-])(=O)=O.[O-][W]([O-])(=O)=O.[O-][W]([O-])(=O)=O.[O-][W]([O-])(=O)=O.[O-][W]([O-])(=O)=O XAYGUHUYDMLJJV-UHFFFAOYSA-Z 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000214 effect on organisms Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000243 mutagenic effect Toxicity 0.000 description 1
- 230000003505 mutagenic effect Effects 0.000 description 1
- XKLJHFLUAHKGGU-UHFFFAOYSA-N nitrous amide Chemical compound ON=N XKLJHFLUAHKGGU-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 231100000378 teratogenic Toxicity 0.000 description 1
- 230000003390 teratogenic effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
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Classifications
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- 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
- C02F1/048—Purification of waste water by evaporation
-
- 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
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- 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)
- Physical Water Treatments (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses an ammonia nitrogen wastewater stripping and ammonia distilling system, which comprises a preheater, a stripping tower and a reboiler, wherein an ammonia nitrogen wastewater outlet of the preheater is communicated with a liquid phase inlet at the upper end of the stripping tower; and a liquid phase outlet at the lower end of the stripping tower is communicated with a deamination nitrogen wastewater inlet of the preheater. The invention also discloses a method for steam stripping and ammonia distillation of ammonia nitrogen wastewater, which comprises the following steps: the ammonia nitrogen wastewater to be treated and the tower bottom liquid of the stripping tower enter the preheater from two inlets of the preheater respectively for heat exchange to obtain preheated ammonia nitrogen wastewater, the preheated ammonia nitrogen wastewater enters the stripping tower for ammonia distillation, mixed steam is obtained at the tower top, the mixed steam enters a reboiler for heat exchange, and generated secondary steam enters the stripping tower. According to the steam stripping ammonia distillation system and the method, the low-pressure steam consumption is reduced by more than 50%, the consumption of the condensed circulating water is reduced by more than 40%, and the discharge amount of the standard wastewater is reduced by 8-10%.
Description
Technical Field
The invention belongs to the field of ammonia nitrogen wastewater treatment, and particularly relates to a high-concentration ammonia nitrogen wastewater steam stripping ammonia distillation system and method, which provide a solution for energy conservation and consumption reduction in recovery and standard emission of ammonia nitrogen.
Background
With the rapid development of chemical industry, metallurgy, new materials and other industries, a large amount of ammonia nitrogen wastewater is discharged into the nature, which causes the influences of water eutrophication, water blackening and smelly, service life reduction of water supply systems and the like. In particular high-concentration ammonia nitrogen wastewater (NH)3N is more than 500mg/L), is easy to be converted into nitrosamine with strong carcinogenic, teratogenic and mutagenic effects, and has great toxic effect on human and organisms.
The ammonia nitrogen resources in the high-concentration ammonia nitrogen wastewater are rich, the recovery benefit is good, but the problems of high ammonia nitrogen removal difficulty and the like exist, and the current mainstream treatment process is a steam stripping ammonia evaporation method.
The traditional stripping ammonia-steaming method has high ammonia nitrogen removal rate and high concentration of recovered ammonia water, and is greatly popularized and applied in the industries of metallurgy, chemical engineering, new energy materials and the like. Generally, low-pressure steam is used as a heat source in stripping ammonia distillation, the operating temperature in the stripping tower is 95-105 ℃, ammonia nitrogen wastewater needs to be heated to the boiling point temperature to realize stripping operation, the mixed steam of ammonia and water at the tower top is directly condensed, a large amount of circulating cooling water is consumed in the condensation process, and a large amount of heat is wasted.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects and shortcomings in the background art, and provide an energy-saving high-concentration ammonia nitrogen wastewater stripping ammonia distillation system and method, so as to reduce the steam consumption of stripping ammonia distillation, reduce the total amount of wastewater discharge, reduce the consumption of circulating cooling water and the like.
In order to solve the technical problems, the technical scheme provided by the invention is as follows:
an ammonia nitrogen wastewater stripping and ammonia distilling system comprises a preheater, a stripping tower and a reboiler, wherein the stripping tower comprises an upper-end liquid phase inlet, a top steam outlet, a lower-end liquid phase outlet, a bottom liquid phase outlet and a lower-end steam inlet, and the preheater comprises an ammonia nitrogen wastewater inlet, an ammonia nitrogen wastewater outlet and an ammonia nitrogen wastewater outlet;
an ammonia nitrogen wastewater outlet of the preheater is communicated with a liquid phase inlet at the upper end of the stripping tower, a steam outlet at the top of the stripping tower is communicated with a reboiler, and a liquid phase outlet at the bottom of the stripping tower is communicated with a steam inlet at the lower end of the stripping tower through the reboiler; and a liquid phase outlet at the lower end of the stripping tower is communicated with a deamination nitrogen wastewater inlet of the preheater. The stripping column may also be externally connected to low pressure steam.
In the ammonia nitrogen wastewater stripping and ammonia distilling system, preferably, a steam compressor is arranged between the steam outlet at the top of the stripping tower and the reboiler.
In the ammonia nitrogen wastewater stripping and ammonia distilling system, preferably, the vapor compressor is a centrifugal compressor or a roots compressor.
Preferably, the ammonia nitrogen wastewater stripping and ammonia distilling system further comprises a flash tank and an ammonia concentration tower, wherein the ammonia concentration tower comprises a liquid phase inlet at the middle upper end, a gas phase inlet at the lower end, a steam outlet at the top, a low-pressure steam inlet and a liquid phase outlet at the bottom; and a liquid phase outlet of the reboiler is communicated with the flash tank, a condensed water outlet of the flash tank is communicated with a liquid phase inlet at the upper end of the ammonia concentration tower, and a steam outlet of the flash tank is communicated with a gas phase inlet at the lower end of the ammonia concentration tower.
Preferably, the liquid phase outlet at the bottom of the ammonia concentration tower is communicated with the ammonia nitrogen wastewater inlet of the preheater.
Preferably, the steam outlet at the top of the ammonia concentration tower is communicated with the condenser.
Preferably, the condenser is an all-welded plate condenser or a shell and tube condenser.
In the ammonia nitrogen wastewater stripping and ammonia distilling system, preferably, the tower type of the stripping tower is a plate tower, a packed tower or a plate-packed mixed tower;
the preheater is a plate heat exchanger, a tube type heat exchanger or a spiral plate type heat exchanger;
the reboiler is a thermosyphon reboiler or a kettle reboiler;
the concentration tower is a plate tower, a packed tower or a plate-packed mixed tower.
As a general inventive concept, the invention also provides a method for carrying out ammonia-nitrogen wastewater stripping and ammonia distillation by using the ammonia-nitrogen wastewater stripping and ammonia distillation system, which comprises the following steps:
s1: ammonia nitrogen wastewater to be treated and tower bottom liquid pumped out from a liquid phase outlet at the lower end of the stripping tower enter a preheater from an ammonia nitrogen wastewater inlet and a deaminizing nitrogen wastewater inlet of the preheater respectively for heat exchange to obtain preheated ammonia nitrogen wastewater and cooled deaminizing wastewater;
s2: preheating ammonia nitrogen wastewater enters the stripping tower from a liquid phase inlet at the upper end of the stripping tower for ammonia distillation, mixed ammonia and water steam is obtained at the top of the stripping tower, and deamination wastewater is obtained at the bottom of the stripping tower;
s3: part of the deamination waste water obtained by the stripping tower and the mixed steam of ammonia and water enter a reboiler for heat exchange, a liquid phase outlet of the reboiler generates secondary steam, the secondary steam enters the stripping tower through a steam inlet at the lower end of the stripping tower to maintain a stripping ammonia distillation process, and the condensed water outlet of the reboiler (3) discharges mixed condensed water of ammonia and water.
The method preferably further comprises the following steps:
s4: discharging the ammonia-water mixed condensate water into a flash tank for gas-liquid separation to obtain cooling condensate water and ammonia-water mixed steam;
s5: introducing the cooled condensed water obtained in the step S4 into an ammonia concentration tower from a liquid phase inlet at the upper end in the ammonia concentration tower, and introducing the mixed steam of ammonia and water obtained in the step S4 into the ammonia concentration tower from a gas phase inlet at the lower end of the ammonia concentration tower; simultaneously, introducing low-pressure steam into the ammonia concentration tower for concentration, obtaining steam at the tower top of the ammonia concentration tower and ammonia water containing ammonia nitrogen at the tower bottom;
s6: and (4) condensing steam at the top of the ammonia concentration tower in a condenser, and collecting ammonia water.
In the above method, preferably, the mixed steam of ammonia and water in S2 is compressed by a vapor compressor, pressurized, and heated, and then introduced into a reboiler.
In the above method, the temperature of the mixed steam of ammonia and water after the compression, pressurization and temperature rise by the vapor compressor is preferably 100 to 130 ℃.
In the above method, the compression ratio of the vapor compressor is preferably 1.0 to 2.2.
Preferably, in the S5, the ammonia water with ammonia nitrogen removed from the bottom of the ammonia concentration tower returns to S1, and is mixed with the ammonia nitrogen wastewater to be treated and then enters the preheater.
The method preferably comprises, in S1, NH of the ammonia-nitrogen wastewater to be treated3The concentration of-N is more than or equal to 500 mg/L;
in S2, the concentration of the obtained mixed steam of ammonia and water is 0.5-5%;
in S3, the concentration of the collected ammonia water is 5% -25%.
The process of the invention comprises the following steps: the method comprises the steps of mixing high-concentration ammonia nitrogen wastewater to be treated with tower bottom liquid of an ammonia concentration tower, sending the mixture to the upper part of a stripping tower, carrying out multistage mass transfer and heat exchange on the wastewater from top to bottom and the steam at the bottom of the stripping tower, discharging ammonia nitrogen wastewater with ammonia nitrogen concentration less than or equal to 15mg/L from the tower bottom, boosting and heating the tower top ammonia and water mixed steam through a steam compressor to serve as heat source steam of a reboiler of the stripping tower, conveying low-concentration condensed ammonia water of the reboiler to the middle upper part of the ammonia concentration tower for ammonia concentration, obtaining high-concentration ammonia water at the tower top, and returning the tower bottom liquid.
Compared with the prior art, the invention has the advantages that:
(1) the heat carried by the mixed steam at the top of the stripping tower accounts for about 90% of the total input energy, wherein the latent heat accounts for about 80%, and the system is provided with a steam compressor and a reboiler, so that the heat of the mixed steam at the top of the stripping tower is pressurized and heated by the steam compressor and then is recycled instead of being directly condensed, the heat can be fully utilized, and the consumption of low-pressure steam is reduced.
(2) In the ammonia distillation system, the steam stripping and ammonia distillation are carried out in two sections, including a steam stripping tower and an ammonia water concentration tower, wherein the steam stripping tower only has a steam stripping section, a rectification section and condensate backflow, so that the heat loss caused by condensate backflow can be reduced; the low-concentration ammonia and water mixed steam at the top of the stripping tower is pressurized and heated by a steam compressor and then heats a reboiler of the stripping tower, condensate (low-concentration ammonia water) of the reboiler is subjected to gas-liquid separation by a flash tank and then is conveyed to an ammonia water concentration tower for ammonia water concentration, tower bottom liquid of the concentration tower returns to the stripping tower for deamination stripping, and the stripping tower and the ammonia water concentration tower form circulation.
(3) According to the invention, the steam at the top of the stripping tower is subjected to positive pressure temperature rise by adopting the compressor and then is used as a heat source of the reboiler, so that the heat of the steam is fully utilized, and the mixed steam at the top of the stripping tower is condensed in the reboiler and the flash tank; the use of the reboiler reduces the amount of primary low pressure steam used, thereby reducing the effect of increased standard wastewater due to condensation of the primary steam in the column.
(4) By adopting the process for removing ammonia nitrogen and recovering concentrated ammonia water by the high-concentration ammonia nitrogen wastewater stripping ammonia distillation system, the consumption of low-pressure steam is reduced by more than 50%, the consumption of condensed circulating water is reduced by more than 40%, the discharge amount of standard wastewater is reduced by 8-10%, and the subsequent wastewater treatment cost can be further reduced.
Drawings
FIG. 1 is a schematic structural diagram of an ammonia nitrogen wastewater stripping and distilling system.
Illustration of the drawings:
1. a preheater; 2. a stripping column; 21. an upper liquid phase inlet; 22. a top steam outlet; 23. a lower liquid phase outlet; 24. a bottom liquid phase outlet; 25. a lower end steam inlet; 3. a reboiler; 4. a flash tank; 5. an ammonia concentration tower; 51. a liquid phase inlet at the middle upper end; 52. a gas phase inlet at the lower end; 53. a vapor outlet at the top; 54. a low pressure steam inlet; 55. a liquid phase outlet at the bottom; 6. a vapor compressor; 7. a condenser; 8. a pump A; 9. a pump B; 10. and a pump C.
Detailed Description
In order to facilitate an understanding of the invention, the invention will be described more fully and in detail below with reference to the accompanying drawings and preferred embodiments, but the scope of the invention is not limited to the specific embodiments below.
Unless otherwise defined, all terms of art used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the scope of the present invention.
Unless otherwise specifically stated, various raw materials, reagents, instruments, equipment and the like used in the present invention are commercially available or can be prepared by existing methods.
An ammonia nitrogen wastewater stripping and ammonia distilling system is shown in figure 1 and comprises a preheater 1, a stripping tower 2, a reboiler 3, a flash tank 4 and an ammonia concentration tower 5, wherein the stripping tower 2 comprises an upper end liquid phase inlet 21, a top steam outlet 22, a lower end liquid phase outlet 23, a bottom liquid phase outlet 24 and a lower end steam inlet 25, and the ammonia concentration tower 5 comprises a middle upper end liquid phase inlet 51, a lower end gas phase inlet 52, a top steam outlet 53, a low pressure steam inlet 54 and a bottom liquid phase outlet 55; the preheater 1 comprises an ammonia nitrogen wastewater inlet, a deamination nitrogen wastewater inlet, an ammonia nitrogen wastewater outlet and a deamination nitrogen wastewater outlet; an ammonia nitrogen wastewater outlet of the preheater 1 is communicated with a liquid phase inlet 21 at the upper end of the stripping tower 2, a steam outlet 22 at the top of the stripping tower 2 is communicated with a reboiler 3, and a liquid phase outlet 24 at the bottom of the stripping tower 2 is communicated with a steam inlet 25 at the lower end of the stripping tower 2 through the reboiler 3; the liquid phase outlet of the reboiler 3 is communicated with the flash tank 4, the condensed water outlet of the flash tank 4 is communicated with the liquid phase inlet 51 at the upper end of the ammonia concentration tower 5 through a pump B9, and the steam outlet of the flash tank 4 is communicated with the gas phase inlet 52 at the lower end of the ammonia concentration tower 5.
In the present invention, a vapor compressor 6 is provided between the steam outlet 22 at the top of the stripping tower 2 and the reboiler 3. The vapor compressor 6 is a centrifugal compressor or a roots compressor.
In the invention, a liquid phase outlet 23 at the lower end of the stripping tower 2 is communicated with a deamination nitrogen wastewater inlet of the preheater 1 through a pump A8.
In the invention, a liquid phase outlet 55 at the bottom of the ammonia concentration tower 5 is communicated with an ammonia nitrogen wastewater inlet of the preheater 1 through a pump C10.
In the present invention, the vapor outlet 53 at the top of the ammonia concentration tower 5 communicates with the condenser 7.
In the invention, the condenser 7 is a full-welded plate condenser or a shell and tube condenser; the tower type of the stripping tower 2 is a plate tower, a packed tower or a plate-packed mixed tower; the preheater 1 is a plate heat exchanger, a tubular heat exchanger or a spiral plate heat exchanger; the reboiler 3 is a thermosyphon reboiler or a kettle reboiler; the ammonia concentration tower 5 is a plate tower, a packed tower or a plate-packed mixed tower.
Example 1 (ammonia nitrogen wastewater stripping ammonia distillation method):
5000-10000mg/L of high-concentration ammonia nitrogen wastewater 240m generated in ammonium paratungstate production by tungsten smelting3And d, the pH value is 12.5, the wastewater is treated by adopting a traditional stripping ammonia distillation process and is carried out in an ammonia distillation tower with the diameter of 800mm, the treatment process flow is that raw wastewater and tower bottom liquid of the ammonia distillation tower enter the middle upper part of the ammonia distillation tower after heat exchange through a plate heat exchanger, the wastewater and low-pressure saturated steam entering from the bottom of the tower carry out mass transfer and heat transfer, mixed steam at the top of the tower enters a condenser to exchange heat with circulating cooling water for condensation, 80% of condensate returns to the top of the ammonia distillation tower to carry out reflux, and the condenser obtains ammonia water with the concentration of 15%. When the treatment process is operated, 1m of the treatment process is carried out3The ammonia nitrogen wastewater needs to consume 100kg of low-pressure steam (absolute pressure is 0.5MPa), the consumption of the low-pressure steam is 1000kg/h, and the circulating cooling water consumes 120m3/h。
The method for treating the ammonia-nitrogen wastewater steam stripping ammonia distillation by adopting the ammonia-nitrogen wastewater steam stripping ammonia distillation system comprises the following steps:
(1) ammonia nitrogen wastewater to be treated and tower bottom liquid pumped out from a liquid phase outlet 23 at the lower end of the stripping tower 2 enter the preheater 1 from an ammonia nitrogen wastewater inlet and a deammoniation nitrogen wastewater inlet of the preheater 1 respectively for heat exchange to obtain preheated ammonia nitrogen wastewater and cooled deammoniation nitrogen wastewater; discharging the cooled wastewater containing the ammonia and the nitrogen;
(2) the preheated ammonia nitrogen wastewater enters a liquid phase inlet 21 at the upper end of a stripping tower 2 and enters the stripping tower 2 for ammonia distillation, mixed steam of ammonia and water (the flow of the mixed steam of ammonia and water with the concentration of about 5 percent of ammonia is 1500kg/h and the temperature is 96 ℃) is obtained at the top of the stripping tower 2, and deamination standard wastewater is obtained at the bottom of the stripping tower (the ammonia nitrogen is removed to be less than or equal to 15 mg/L);
(3) the ammonia and water mixed steam is compressed by a centrifugal steam compressor with the gas passing amount of 1600kg/h and the temperature rising of 18 ℃ (the compression ratio of the steam compressor is 2.0, the pressure and the temperature rise are raised to 162kPa (corresponding to the saturated steam temperature of 113 ℃), the mixed steam enters a vertical thermosyphon reboiler 3 (the inlet flow is 15000kg/h), secondary steam (the gas phase fraction is 12%) is generated at a liquid phase outlet of the reboiler 3, the secondary steam enters a stripping tower 2 through a steam inlet 25 at the lower end of the stripping tower 2 to maintain a stripping ammonia evaporation process, and mixed condensate water of ammonia and water is discharged from a condensate water outlet of the reboiler 3;
(4) discharging the ammonia and water mixed condensate water into a flash tank 4 for gas-liquid separation to obtain cooling condensate water and ammonia and water mixed steam;
(5) introducing the cooled condensed water obtained in the step (4) into an ammonia concentration tower 5 from a liquid phase inlet 51 at the upper end of the ammonia concentration tower 5, and introducing the mixed steam of ammonia and water obtained in the step (4) into the ammonia concentration tower 5 from a gas phase inlet 52 at the lower end of the ammonia concentration tower 5;
(6) low-pressure steam is introduced into the ammonia concentration tower 5 through a low-pressure steam inlet for concentration, the steam obtained from the top of the ammonia concentration tower 5 enters a condenser 7 for condensation to obtain high-concentration ammonia water (high-purity ammonia water with the concentration of 16%), ammonia nitrogen removal ammonia water is obtained from the bottom of the tower, and the ammonia nitrogen removal ammonia water returns to the step 1 and is mixed with ammonia nitrogen wastewater to be treated and then enters the preheater 1.
The steam consumption of the ammonia concentration tower in the whole process is 350kg/h, the running power of a steam compressor is 60kW, and the circulating cooling water consumption is 52m3The overall steam consumption was reduced by 65%.
Example 2 (ammonia nitrogen wastewater stripping ammonia distillation method):
3000-8000mg/L high-concentration ammonia nitrogen wastewater 1600m generated in production of certain new energy materials3And d (the pH value of the wastewater is 13), treating the wastewater by adopting a traditional stripping ammonia distillation process, wherein the stripping ammonia distillation is carried out in an ammonia distillation tower with the diameter of 1900mm, the treatment process flow is that wastewater raw water and the tower bottom liquid of the ammonia distillation tower enter the middle upper part of the ammonia distillation tower after heat exchange through a plate heat exchanger, mass transfer and heat transfer are carried out on the wastewater and low-pressure saturated steam entering from the bottom of the tower, mixed steam at the top of the tower enters a condenser to exchange heat with circulating cooling water for condensation, 60% of condensate returns to the top of the ammonia distillation tower to carry out reflux, and the condenser obtains 10% concentration ammonia water. When the treatment process is operated, 1m of the treatment process is carried out3The ammonia nitrogen wastewater needs to consume 100kg of low-pressure steam (absolute pressure is 0.5MPa), the consumption of the low-pressure steam is 6600kg/h, and the consumption of circulating cooling water is 800m3/h。
The method for treating the ammonia-nitrogen wastewater steam stripping ammonia distillation by adopting the ammonia-nitrogen wastewater steam stripping ammonia distillation system comprises the following steps:
(1) ammonia nitrogen wastewater to be treated and tower bottom liquid pumped out from a liquid phase outlet 23 at the lower end of the stripping tower 2 enter the preheater 1 from an ammonia nitrogen wastewater inlet and a deammoniation nitrogen wastewater inlet of the preheater 1 respectively for heat exchange to obtain preheated ammonia nitrogen wastewater and cooled deammoniation nitrogen wastewater; discharging the cooled wastewater containing the ammonia and the nitrogen;
(2) the preheated ammonia nitrogen wastewater enters a liquid phase inlet 21 at the upper end of a stripping tower 2 and enters the stripping tower 2 for ammonia distillation, mixed steam of ammonia and water (the flow rate of the mixed steam of ammonia and water with the ammonia concentration of about 4.3 percent is 7800kg/h and the temperature is 96 ℃) is obtained at the top of the stripping tower 2, and deamination standard wastewater is obtained at the bottom of the stripping tower (the ammonia nitrogen is removed to be less than or equal to 15 mg/L);
(3) the ammonia-water mixed steam is compressed by a centrifugal steam compressor with the gas passing amount of 8000kg/h and the temperature rising of 18 ℃ (the compression ratio of the steam compressor is 2.0, the steam is increased to 162kPa (corresponding to the saturated steam temperature of 113 ℃), and then enters a vertical thermosyphon reboiler 3 (the inlet flow is 96t/h), secondary steam (the gas phase fraction is 9.8%) is generated at a liquid phase outlet of the reboiler 3, the secondary steam enters a stripping tower 2 through a steam inlet 25 at the lower end of the stripping tower 2 to maintain a stripping ammonia distillation process, and ammonia-water mixed condensate water (the concentration is 4.3%) is discharged from a condensate water outlet of the reboiler 3;
(4) discharging the ammonia and water mixed condensate water into a flash tank 4 for gas-liquid separation to obtain cooling condensate water and ammonia and water mixed steam;
(5) introducing the cooled condensed water obtained in the step (4) into an ammonia concentration tower 5 from a liquid phase inlet 51 at the upper end of the ammonia concentration tower 5, and introducing the mixed steam of ammonia and water obtained in the step (4) into the ammonia concentration tower 5 from a gas phase inlet 52 at the lower end of the ammonia concentration tower 5;
(6) low-pressure steam is introduced into the ammonia concentration tower 5 through a low-pressure steam inlet for concentration, the steam obtained from the top of the ammonia concentration tower 5 enters a condenser 7 for condensation to obtain high-concentration ammonia water (high-purity ammonia water with the concentration of 15%), ammonia nitrogen removal ammonia water is obtained from the bottom of the tower, and the ammonia nitrogen removal ammonia water returns to the step 1 and is mixed with ammonia nitrogen wastewater to be treated and then enters the preheater 1.
The steam consumption of the ammonia concentration tower is 2100kg/h, the running power of a steam compressor is 300kW, and the circulating cooling water consumption is 380m3Overall steam consumption was reduced by 68%.
Claims (15)
1. The ammonia nitrogen wastewater stripping and ammonia distilling system is characterized by comprising a preheater (1), a stripping tower (2) and a reboiler (3), wherein the stripping tower (2) comprises an upper end liquid phase inlet (21), a top steam outlet (22), a lower end liquid phase outlet (23), a bottom liquid phase outlet (24) and a lower end steam inlet (25), and the preheater (1) comprises an ammonia nitrogen wastewater inlet, a deamination nitrogen wastewater inlet, an ammonia nitrogen wastewater outlet and a deamination nitrogen wastewater outlet;
an ammonia nitrogen wastewater outlet of the preheater (1) is communicated with a liquid phase inlet (21) at the upper end of the stripping tower (2), a steam outlet (22) at the top of the stripping tower (2) is communicated with a reboiler (3), and a liquid phase outlet (24) at the bottom of the stripping tower (2) is communicated with a steam inlet (25) at the lower end of the stripping tower (2) through the reboiler (3); and a liquid phase outlet (23) at the lower end of the stripping tower (2) is communicated with a deamination nitrogen wastewater inlet of the preheater (1).
2. The ammonia nitrogen wastewater stripping and ammonia distilling system according to claim 1, wherein a vapor compressor (6) is arranged between the top vapor outlet (22) of the stripping tower (2) and the reboiler (3).
3. The ammonia nitrogen wastewater stripping and ammonia distilling system as set forth in claim 2, wherein the vapor compressor (6) is a centrifugal compressor or a roots compressor.
4. The ammonia nitrogen wastewater stripping and ammonia distilling system according to claim 1, further comprising a flash tank (4) and an ammonia concentrating tower (5), wherein the ammonia concentrating tower (5) comprises a liquid phase inlet (51) at the middle upper end, a gas phase inlet (52) at the lower end, a steam outlet (53) at the top, a low pressure steam inlet (54) and a liquid phase outlet (55) at the bottom; the liquid phase outlet of the reboiler (3) is communicated with the flash tank (4), the condensed water outlet of the flash tank (4) is communicated with the liquid phase inlet (51) at the upper end of the ammonia concentration tower (5), and the steam outlet of the flash tank (4) is communicated with the gas phase inlet (52) at the lower end of the ammonia concentration tower (5).
5. The ammonia nitrogen wastewater stripping and ammonia distilling system according to claim 4, wherein the liquid phase outlet (55) at the bottom of the ammonia concentrating tower (5) is communicated with the ammonia nitrogen wastewater inlet of the preheater (1).
6. The ammonia nitrogen wastewater stripping and ammonia distilling system according to claim 4, wherein the steam outlet (53) at the top of the ammonia concentrating tower (5) is communicated with the condenser (7).
7. The ammonia nitrogen wastewater stripping ammonia distillation system according to claim 6, wherein the condenser (7) is an all-welded plate condenser or a shell and tube condenser.
8. The ammonia nitrogen wastewater stripping and ammonia distilling system according to any one of claims 4 to 7, characterized in that the tower type of the stripping tower (2) is a plate tower, a packed tower or a plate-packed mixed tower;
the preheater (1) is a plate heat exchanger, a shell and tube heat exchanger or a spiral plate heat exchanger;
the reboiler (3) is a thermosyphon reboiler or a kettle reboiler;
the ammonia concentration tower (5) is a plate tower, a packed tower or a plate-packed mixed tower.
9. The ammonia nitrogen wastewater stripping and ammonia distillation method adopting the ammonia nitrogen wastewater stripping and ammonia distillation system as claimed in any one of claims 1 to 8, characterized by comprising the following steps:
s1: ammonia nitrogen wastewater to be treated and tower bottom liquid pumped out from a liquid phase outlet (23) at the lower end of the stripping tower (2) respectively enter the preheater (1) from an ammonia nitrogen wastewater inlet and a deaminized nitrogen wastewater inlet of the preheater (1) for heat exchange to obtain preheated ammonia nitrogen wastewater and cooled deaminized nitrogen wastewater;
s2: the preheated ammonia nitrogen wastewater enters the stripping tower (2) from a liquid phase inlet (21) at the upper end of the stripping tower (2) for ammonia distillation, mixed ammonia and water steam is obtained at the top of the stripping tower (2), and ammonia nitrogen wastewater is obtained at the bottom of the stripping tower;
s3: part of ammonia nitrogen wastewater obtained at the bottom of the stripping tower (2) and ammonia-water mixed steam enter the reboiler (3) for heat exchange, a liquid phase outlet of the reboiler (3) generates secondary steam, the secondary steam enters the stripping tower (2) through a steam inlet (25) at the lower end of the stripping tower (2) to maintain a stripping ammonia distillation process, and ammonia-water mixed condensate water is discharged from a condensate water outlet of the reboiler (3).
10. The method of claim 9, further comprising the steps of:
s4: discharging the ammonia and water mixed condensate water into a flash tank (4) for gas-liquid separation to obtain cooling condensate water and ammonia and water mixed steam;
s5: the cooling condensed water obtained in the step S4 is introduced into the ammonia concentration tower (5) from a liquid phase inlet (51) at the upper end of the ammonia concentration tower (5), the mixed steam of ammonia and water obtained in the step S4 is introduced into the ammonia concentration tower (5) from a gas phase inlet (52) at the lower end of the ammonia concentration tower (5), meanwhile, low-pressure steam is introduced into the ammonia concentration tower (5) for concentration, steam is obtained from the top of the ammonia concentration tower (5), and ammonia nitrogen ammonia water is obtained from the bottom of the tower;
s6: and the steam at the top of the ammonia concentration tower (5) enters a condenser (7) for condensation, and ammonia water is collected.
11. The method according to claim 9, wherein the mixed steam of ammonia and water in S2 is compressed by a vapor compressor (6), pressurized, heated and then enters the reboiler (3).
12. The method of claim 9, wherein the temperature of the mixed steam of ammonia and water after being compressed, pressurized and heated by the vapor compressor (6) is 100-130 ℃.
13. The method as claimed in claim 10, characterized in that the compression ratio of the vapor compressor (6) is 1.0 to 2.2.
14. The method as claimed in claim 10, wherein in S5, the ammonia water of the ammonia-nitrogen removal from the bottom of the ammonia concentration tower (5) is returned to S1, mixed with the ammonia-nitrogen wastewater to be treated and then enters the preheater (1).
15. The method of claim 10, wherein in S1, NH of the ammonia nitrogen wastewater to be treated3The concentration of-N is more than or equal to 500 mg/L;
in S2, the concentration of the obtained mixed steam of ammonia and water is 0.5-5%;
in S6, the concentration of the collected ammonia water is 5% -25%.
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