CN113230833A - Novel ammonia absorption and crystallized salt separation method - Google Patents
Novel ammonia absorption and crystallized salt separation method Download PDFInfo
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- CN113230833A CN113230833A CN202110593566.XA CN202110593566A CN113230833A CN 113230833 A CN113230833 A CN 113230833A CN 202110593566 A CN202110593566 A CN 202110593566A CN 113230833 A CN113230833 A CN 113230833A
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- ammonium sulfate
- tank
- working
- circulating tank
- ammonia
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 42
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 40
- 238000000926 separation method Methods 0.000 title claims abstract description 21
- 150000003839 salts Chemical class 0.000 title claims abstract description 11
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 124
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 124
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 124
- 239000007788 liquid Substances 0.000 claims abstract description 58
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000013078 crystal Substances 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims abstract description 31
- 239000000243 solution Substances 0.000 claims abstract description 23
- 239000011550 stock solution Substances 0.000 claims abstract description 17
- AWADHHRPTLLUKK-UHFFFAOYSA-N diazanium sulfuric acid sulfate Chemical compound [NH4+].[NH4+].OS(O)(=O)=O.[O-]S([O-])(=O)=O AWADHHRPTLLUKK-UHFFFAOYSA-N 0.000 claims description 14
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 11
- 238000001704 evaporation Methods 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 11
- 239000002351 wastewater Substances 0.000 claims description 10
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 9
- 239000011259 mixed solution Substances 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 9
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 7
- 238000004065 wastewater treatment Methods 0.000 claims description 6
- 238000012544 monitoring process Methods 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 239000012452 mother liquor Substances 0.000 description 7
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 239000000945 filler Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
- C01C1/242—Preparation from ammonia and sulfuric acid or sulfur trioxide
-
- 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
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a novel method for absorbing ammonia and separating crystallized salt. Two ammonium sulfate circulating tanks are alternately used as a working ammonium sulfate circulating tank and a standby ammonium sulfate circulating tank to carry out the following work: 1) conveying sulfuric acid in a working ammonium sulfate circulating tank into an ammonia absorption tower through a circulating pump; 2) when the height of a crystal liquid interface in the working ammonium sulfate circulating tank rises to a specified height, sending the ammonium sulfate solution at the bottom of the working ammonium sulfate circulating tank into a cyclone separator through a pump for crystal liquid separation; 3) detecting the pH value of the working ammonium sulfate circulating tank in real time; 4) discharging the ammonium sulfate crystal mixed liquor in the ammonium sulfate circulating tank after absorption to an ammonium sulfate adjusting tank; 5) re-dissolving the separated ammonium sulfate crystal by using new water or condensate, and automatically flowing into an ammonium sulfate stock solution pool to be evaporated; 6) replenishing the sulfuric acid solution in the working ammonium sulfate circulating tank for later use; and repeating the steps by taking the original standby ammonium sulfate circulating tank as a working ammonium sulfate circulating tank. The method realizes the recycling of resources while solving the problem of ammonia gas absorption blockage.
Description
Technical Field
The invention relates to a technology for treating concentrated ammonia nitrogen wastewater, in particular to a method for continuously operating, preventing filler of a tail gas absorption tower in an ammonia stripping process from being blocked and recovering resources.
Technical Field
The high-concentration ammonia nitrogen wastewater has wide sources, large discharge amount and great harm to the environment. The stripping method is one of effective methods for treating high-ammonia-nitrogen wastewater, the high-ammonia-nitrogen wastewater enters an ammonia-nitrogen stripping tower to realize separation of ammonia nitrogen and water by blowing, then separated ammonia nitrogen gas is sent into an ammonia gas absorption tower to be in contact reaction with sulfuric acid spray to generate ammonium sulfate, after absorption is finished, ammonium sulfate-sulfuric acid mixed liquor is generated to adjust PH, and then ammonium sulfate crystals are formed by evaporation crystallization, so that resource recycling is realized. The main current process for absorbing ammonia gas by using sulfuric acid at the present stage adopts a method of circulating and absorbing ammonia gas by using an ammonium sulfate circulating tank and a circulating pump, and mainly has the following problems: 1. the filling material in the ammonia absorption tower is seriously blocked, so that the efficiency of absorbing ammonia by sulfuric acid is influenced; 2. ammonium sulfate crystals generated in the circulating tank need to be manually cleaned, which is difficult; 3. the subsequent evaporation crystallization grade of the ammonium sulfate can not reach the national standard of ammonium sulfate crystal products, and the utilization is difficult. 4. The end point of ammonia gas absorption by sulfuric acid is PH 2-3, and more ammonia water is consumed for neutralization.
Disclosure of Invention
In order to overcome the defects, the invention aims to provide a method for continuously operating, preventing the filling material of the tail gas absorption tower in the ammonia stripping process from being blocked and recovering resources.
In order to achieve the purposes, the novel method for absorbing ammonia and separating crystallized salt adopts two ammonium sulfate circulation tanks as a working ammonium sulfate circulation tank and a standby ammonium sulfate circulation tank alternately, and performs the following work:
1) conveying sulfuric acid in a working ammonium sulfate circulating tank into an ammonia absorption tower through a circulating pump;
refluxing the sulfuric acid-ammonium sulfate mixed solution after ammonia gas is absorbed to a working ammonium sulfate circulating tank;
2) in the step 1) executing process, continuously monitoring the change of the solution density in the working ammonium sulfate circulating tank, and when the height of the crystal liquid interface in the working ammonium sulfate circulating tank rises to a specified height, pumping the ammonium sulfate solution at the bottom of the working ammonium sulfate circulating tank into a cyclone separator for crystal liquid separation until the height of the crystal liquid interface in the working ammonium sulfate circulating tank is reduced to the specified height;
3) detecting the pH value of the working ammonium sulfate circulating tank in real time, and closing the working ammonium sulfate circulating tank when the pH value of the working ammonium sulfate circulating tank is 5-6; pumping the stock solution of the working ammonium sulfate circulating tank which is just closed into an ammonium sulfate adjusting tank, adding ammonia water to adjust the PH value to 6.5-7, and then sending the liquid in the ammonium sulfate adjusting tank into a cyclone separator for separation; enabling the supernatant to flow to an ammonia nitrogen wastewater stock solution pool for temporary storage, entering a subsequent wastewater treatment process, filtering residual liquid in a cyclone separator through a filter, enabling separated weak solution to be subjected to subsequent wastewater treatment, dissolving the trapped crystals through evaporation condensate, and then flowing to an ammonium sulfate stock solution pool for evaporation treatment;
4) replenishing the sulfuric acid solution to the emptied working ammonium sulfate circulating tank again to serve as a standby ammonium sulfate circulating tank for standby; and repeating the steps by taking the original standby ammonium sulfate circulating tank as a working ammonium sulfate circulating tank.
Further, the liquid inlet pipe of the circulating pump is connected to the middle part of the ammonium sulfate circulating tank; refluxing the sulfuric acid-ammonium sulfate mixed solution after the ammonia gas is absorbed by the sulfuric acid to the top of the working ammonium sulfate circulating tank; ammonium sulfate crystals are precipitated at the bottom of the circulation tank.
Furthermore, a filter for intercepting ammonium sulfate crystals mixed in the sulfuric acid solution is arranged on a connecting pipe between the cyclone separator and the reflux valve.
Further, the supernatant liquid obtained after the separation of the crystal liquid in the step 2) flows to a working ammonium sulfate circulation tank, the residual liquid in the cyclone separator is filtered by a filter, the light liquid obtained by the separation of the liquid flows to the working ammonium sulfate circulation tank, and the intercepted crystal is dissolved by the evaporation condensate and then flows to an ammonium sulfate stock solution pool.
The invention relates to a novel ammonia absorption and crystal salt separation system, which comprises two ammonium sulfate circulation tanks and an ammonia gas absorption tower; wherein, the liquid inlet pipe of a circulating pump is connected to the middle part of the ammonium sulfate circulating tank through two liquid inlet controlled pipelines respectively, and the liquid outlet pipe of the circulating pump is connected with the ammonia absorption tower; the bottom of the ammonia absorption tower is provided with a return pipe, the outlet of the return pipe is connected to each ammonium sulfate circulating tank through two return controlled pipelines, so that the sulfuric acid-ammonium sulfate mixed solution after absorbing ammonia is returned to the working ammonium sulfate circulating tank; and the control device controls the two liquid inlet controlled pipelines and the reflux controlled pipeline to be alternately opened and closed according to preset working time so that the two ammonium sulfate circulating tanks alternately perform circulating operation with the ammonia absorption tower.
The system further comprises cyclone separators, each ammonium sulfate circulating tank is also provided with a pumping pipeline communicated with the cyclone separators, and the upper parts of the cyclone separators are provided with two supernatant return pipelines respectively communicated with the ammonium sulfate circulating tanks; the control device controls a pumping pipeline and a supernatant liquid return pipeline which are communicated with an ammonium sulfate circulating tank in work to be in a working state.
The ammonium sulfate adjusting tank is an ammonium sulfate stock solution transferring tank, the number of the ammonium sulfate adjusting tank is 4, firstly, the liquid in the circulating tank is emptied, and sulfuric acid solution is filled into the circulating tank to be in a standby state as soon as possible; ② storing ammonium sulfate stock solution; and thirdly, adding ammonia water to adjust the pH of the stock solution. The method realizes the recycling of the ammonium sulfate while solving the problem of blockage of the ammonia absorption filler, does not discharge pollutants in the process, and is an environment-friendly process.
Drawings
FIG. 1 is a process flow diagram of the present invention
1A, an ammonium sulfate circulating tank A; 1B ammonium sulfate circulation tank B; 2A, A tank circulation pump; 2B, B tank circulation pump; 3A, A tank mother liquor delivery pump; 3B, B tank mother liquor delivery pump; 4. a cyclone separator; 5. an ammonia nitrogen wastewater stock solution tank; 6. an ammonium sulfate adjusting tank; 7. adjusting a tank mother liquor delivery pump; 8. an ammonia water storage tank; 9. an ammonia water delivery pump; 10. a mother liquor delivery pump; 11. an ammonium sulfate stock solution pool; 12. an ammonia gas absorption tower; 13. a pipeline filter.
Detailed Description
The method is described in detail below with reference to the drawings, but the invention can be embodied in many different ways as defined and covered by the claims.
The system comprises two ammonium sulfate circulating tanks and an ammonia absorption tower; wherein, the liquid inlet pipe of a circulating pump is connected to the middle part of the ammonium sulfate circulating tank through two liquid inlet controlled pipelines respectively, and the liquid outlet pipe of the circulating pump is connected with the ammonia absorption tower; the bottom of the ammonia absorption tower is provided with a return pipe, the outlet of the return pipe is connected to each ammonium sulfate circulating tank through two return controlled pipelines, so that the sulfuric acid-ammonium sulfate mixed solution after absorbing ammonia is returned to the working ammonium sulfate circulating tank; the control device controls the two liquid inlet controlled pipelines and the reflux controlled pipeline to be alternately opened and closed according to preset working time so as to enable the two ammonium sulfate circulating tanks to alternately and circularly operate with the ammonia absorption tower; the system also comprises cyclone separators, each ammonium sulfate circulating tank is also provided with a pumping pipeline communicated with the cyclone separators, and the upper parts of the cyclone separators are provided with two supernatant liquid return pipelines respectively communicated with the ammonium sulfate circulating tanks; the control device controls a pumping pipeline and a supernatant liquid return pipeline which are communicated with an ammonium sulfate circulating tank in work to be in a working state.
Example 1
(1) In order to realize the continuous operation of the ammonia absorption process, two ammonium sulfate circulating tanks are adopted in the method, when the circulating tank 1A is used as a working ammonium sulfate circulating tank to work, the circulating tank 1B is used as a standby ammonium sulfate circulating tank to stand by; the sulfuric acid solution (sulfuric acid with concentration less than or equal to 50% and new acid concentration-50%) in the circulation tank 1A is sent into the ammonia absorption tower 12 through the circulation pump 2A, the sulfuric acid-ammonium sulfate mixed solution after ammonia absorption is refluxed to the circulation tank 1A through the top of the circulation tank 1A between the ammonia absorption tower 12 and the circulation tank 1A (during actual production, the ammonia absorption tower can be placed at a high position, and then the sulfuric acid solution flows to the circulation tank 1A through the top of the circulation tank 1A by utilizing the height difference of the ammonia absorption tower).
(2) In the continuous cycle work of the 1A tank, the amount of the crystallized salt in an ammonium sulfate-sulfuric acid system is controlled by monitoring the elevation change of an ammonium sulfate-sulfuric acid crystal liquid interface in the 1A tank, the crystallized salt is discharged in time, the blocking condition of a filler in an absorption tower is relieved, and the efficiency of absorbing ammonia gas by sulfuric acid is accelerated. When the elevation of the ammonium sulfate-sulfuric acid crystal liquid interface in the tank 1A rises to a specified elevation, the mother liquor conveying pump 3A is started in an interlocking manner to convey the ammonium sulfate solution at the bottom of the tank 1A into the cyclone separator 4 for crystal liquid separation, and ammonium sulfate crystals generated by the system are discharged out of the system in time. And when the crystal liquid interface elevation in the tank 1A is reduced to a designated elevation, the mother liquid delivery pump 3A is automatically closed. The above process is repeated until the pH in the 1A tank is neutral.
(3) And when the pH value of the 1A tank is 5-6, the sulfuric acid is basically consumed, at the moment, the valve of the 1A tank circulating pipeline is closed, the valve of the 1B tank circulating pipeline is opened, and the 1B tank starts to work. The circulating liquid in the tank 1A is pumped into an ammonium sulfate adjusting tank 6 through a mother liquid delivery pump 3A, ammonia water is added to adjust the PH to 6.5-7, then the liquid in the ammonium sulfate adjusting tank 6 is sent to a cyclone separator 4 for separation, and the supernatant automatically flows to an ammonia nitrogen wastewater stock solution pool 5 for temporary storage, and enters a subsequent wastewater treatment process.
(4) The emptied 1A tank is replenished with 50% sulfuric acid solution, and the ammonium sulfate circulation tank is in standby state. The circulation tank 1B is used as a working ammonium sulfate circulation tank to start to operate, and the steps are repeated, so that the continuous operation of the ammonia absorption process is realized.
Example 2
(1) In order to realize the continuous operation of the ammonia absorption process, two ammonium sulfate circulating tanks are adopted in the method, when the circulating tank 1A is used as a working ammonium sulfate circulating tank to work, the circulating tank 1B is used as a standby ammonium sulfate circulating tank to stand by; the sulfuric acid solution (sulfuric acid with concentration less than or equal to 50% and new acid concentration-50%) in the circulating tank 1A is sent to an ammonia absorption tower 12 through a circulating pump 2A, and the sulfuric acid-ammonium sulfate mixed solution after ammonia absorption is refluxed to the circulating tank 1A through the top of the circulating tank 1A by utilizing the space between the ammonia absorption tower 12 and the circulating tank 1A (during actual production, the ammonia absorption tower can be placed at a high position, and then the high-difference sulfuric acid-ammonium sulfate mixed solution of the ammonia absorption tower is refluxed to the top of the circulating tank 1A).
(2) In the continuous circulating work of the tank 1A, the density of the solution in the tank 1A is monitored by monitoring the density of the solution in the tank 1A and an online densimeter, when the density of the solution in the tank 1A changes all the time, the ammonium sulfate is in a dissolved state, when the density of the solution in the tank 1A stops changing, crystallization is generated in the tank 1A, at the moment, a mother liquor conveying pump 3A is started in an interlocking manner to convey the ammonium sulfate solution at the bottom of the tank 1A to a cyclone separator 4 for crystal liquid separation, until the density of the solution in the tank 1A changes continuously, the crystallization disappears, the mother liquor conveying pump 3A can be closed, the dilute liquid after the crystal liquid separation flows to the circulating tank 1A automatically, the residual liquid in the cyclone separator 4 is filtered by a filter 13, the dilute liquid after the liquid separation flows to the circulating tank 1A automatically, the intercepted crystal is dissolved by evaporation condensate and then flows to an ammonium sulfate raw liquid pool 11 by utilizing the height difference between the cyclone separator 4 and the ammonium sulfate raw liquid pool 11, the pipeline filter 13 is made of corrosion-resistant materials, pressure gauges are arranged at the front and the back of the pipeline filter, the back washing of the pipeline filter is automatically emptied according to the pressure difference, and the discharged liquid returns to the ammonium sulfate circulating tank 1A.
(3) And when the pH value of the 1A tank is 5-6, the sulfuric acid is basically consumed, at the moment, the valve of the 1A tank circulating pipeline is closed, the valve of the 1B tank circulating pipeline is opened, and the 1B tank starts to work. Circulating liquid in the tank 1A is pumped into an ammonium sulfate adjusting tank 6 through a circulating pump 3A, ammonia water is added to adjust PH to 6.5-7, liquid in the ammonium sulfate adjusting tank 6 is sent to a cyclone separator 4 for separation, supernate flows to an ammonia nitrogen wastewater stock solution pool 5 for temporary storage, a subsequent wastewater treatment process is carried out, residual liquid in the cyclone separator 4 is filtered through a filter 13, separated dilute liquid is treated to subsequent wastewater, and intercepted crystals flow to the ammonium sulfate stock solution pool 11 for evaporation treatment after being dissolved through evaporation condensate.
(4) The emptied 1A tank is replenished with 50% sulfuric acid solution, and the ammonium sulfate circulation tank is in standby state. The circulation tank 1B is used as a working ammonium sulfate circulation tank to start to operate, and the steps are repeated, so that the continuous operation of the ammonia absorption process is realized.
Claims (4)
1. A novel method for absorbing ammonia and separating crystallized salt is characterized in that two ammonium sulfate circulation tanks are alternately used as a working ammonium sulfate circulation tank and a standby ammonium sulfate circulation tank to carry out the following work:
1) conveying sulfuric acid in a working ammonium sulfate circulating tank into an ammonia absorption tower through a circulating pump;
refluxing the sulfuric acid-ammonium sulfate mixed solution after ammonia gas is absorbed to a working ammonium sulfate circulating tank;
2) in the step 1) executing process, continuously monitoring the change of the elevation of the crystal liquid interface in the working ammonium sulfate circulating tank, when the elevation of the crystal liquid interface in the working ammonium sulfate circulating tank rises to a specified elevation, pumping the ammonium sulfate-sulfuric acid mixed liquid at the bottom of the working ammonium sulfate circulating tank into a cyclone separator for crystal liquid separation until the elevation of the crystal liquid interface in the working ammonium sulfate circulating tank drops to the specified elevation;
3) detecting the pH value of the working ammonium sulfate circulating tank in real time, and closing the working ammonium sulfate circulating tank when the pH value of the working ammonium sulfate circulating tank is 5-6; pumping the stock solution of the working ammonium sulfate circulating tank which is just closed into an ammonium sulfate adjusting tank, adding ammonia water to adjust the PH value to 6.5-7, and then sending the liquid in the ammonium sulfate adjusting tank into a cyclone separator for separation; enabling the supernatant to flow to an ammonia nitrogen wastewater stock solution pool for temporary storage, entering a subsequent wastewater treatment process, filtering residual liquid in a cyclone separator through a filter, enabling separated weak solution to be subjected to subsequent wastewater treatment, dissolving the trapped crystals through evaporation condensate, and then flowing to an ammonium sulfate stock solution pool for evaporation treatment;
4) replenishing the sulfuric acid solution to the emptied working ammonium sulfate circulating tank again to serve as a standby ammonium sulfate circulating tank for standby; and repeating the steps by taking the original standby ammonium sulfate circulating tank as a working ammonium sulfate circulating tank.
2. The novel ammonia absorption and separation method of crystallized salt as claimed in claim 1, wherein the liquid inlet pipe of the circulating pump is connected to the middle part of the ammonium sulfate circulating tank; the sulfuric acid-ammonium sulfate mixed solution of the ammonia nitrogen absorption tower flows to the top of the ammonium sulfate circulation tank; ammonium sulfate crystals are precipitated at the bottom of the circulation tank.
3. The novel ammonia absorption, crystalline salt separation method as claimed in claim 1, wherein a filter for intercepting ammonium sulfate crystals entrained in the sulfuric acid solution is provided on the connection pipe of the cyclone separator and the reflux valve.
4. The novel method for absorbing ammonia and separating crystallized salt as claimed in claim 1, wherein the supernatant after the separation of the crystal liquid in the step 2) flows to a working ammonium sulfate circulation tank, the residual liquid in the cyclone separator is filtered by a filter, the light liquid after the liquid separation flows to the working ammonium sulfate circulation tank, and the trapped crystals are dissolved by the evaporation condensate and then flow to an ammonium sulfate stock solution pool.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110593566.XA CN113230833A (en) | 2021-05-28 | 2021-05-28 | Novel ammonia absorption and crystallized salt separation method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110593566.XA CN113230833A (en) | 2021-05-28 | 2021-05-28 | Novel ammonia absorption and crystallized salt separation method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115159760A (en) * | 2022-08-02 | 2022-10-11 | 攀钢集团钒钛资源股份有限公司 | Method for precipitating deamination nitrogen and byproducts of sodium sulfate and ammonium sulfate in vanadium precipitation wastewater |
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| CN108069439A (en) * | 2016-11-16 | 2018-05-25 | 刘应华 | The operating procedure of coal gas sulphur ammonium is quickly realized in Furniture Factory's heat supply |
-
2021
- 2021-05-28 CN CN202110593566.XA patent/CN113230833A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| DE10119991A1 (en) * | 2001-04-23 | 2002-10-24 | Stephan Pieper | Purification of biogas containing hydrogen sulfide and ammonia, removes hydrogen sulfide at least partially by absorption into alkaline wash solution |
| CN102107887A (en) * | 2010-12-16 | 2011-06-29 | 昆山科技大学 | Ammonia gas recovery method, concentration measuring method of ammonium sulfate solution, and concentration control method of ammonium sulfate solution |
| CN102580484A (en) * | 2012-02-27 | 2012-07-18 | 中南大学 | Method for purifying and recovering smoke containing sulfur dioxide |
| CN102976358A (en) * | 2012-11-30 | 2013-03-20 | 淄博鲁华泓锦化工股份有限公司 | Production technology and equipment for preparing ammonium sulfate through byproduct of tert-butylamine production process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115159760A (en) * | 2022-08-02 | 2022-10-11 | 攀钢集团钒钛资源股份有限公司 | Method for precipitating deamination nitrogen and byproducts of sodium sulfate and ammonium sulfate in vanadium precipitation wastewater |
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