CN116531924A - Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater - Google Patents
Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater Download PDFInfo
- Publication number
- CN116531924A CN116531924A CN202310587215.7A CN202310587215A CN116531924A CN 116531924 A CN116531924 A CN 116531924A CN 202310587215 A CN202310587215 A CN 202310587215A CN 116531924 A CN116531924 A CN 116531924A
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- Prior art keywords
- ammonia
- gas
- tail gas
- wastewater
- recovery system
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 207
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 91
- 239000002351 wastewater Substances 0.000 title claims abstract description 62
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000005955 Ferric phosphate Substances 0.000 title claims abstract description 32
- 229940032958 ferric phosphate Drugs 0.000 title claims abstract description 32
- 229910000399 iron(III) phosphate Inorganic materials 0.000 title claims abstract description 32
- 238000011084 recovery Methods 0.000 title claims description 65
- 239000007789 gas Substances 0.000 claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 239000002912 waste gas Substances 0.000 claims abstract description 27
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 21
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 21
- 229910000398 iron phosphate Inorganic materials 0.000 claims abstract description 21
- 238000004064 recycling Methods 0.000 claims abstract description 13
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000012535 impurity Substances 0.000 claims abstract description 10
- 239000002184 metal Substances 0.000 claims abstract description 10
- 229910052751 metal Inorganic materials 0.000 claims abstract description 10
- 230000002378 acidificating effect Effects 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 230000002209 hydrophobic effect Effects 0.000 claims description 11
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 11
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 11
- 230000001376 precipitating effect Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims 1
- 230000003301 hydrolyzing effect Effects 0.000 claims 1
- 238000010992 reflux Methods 0.000 claims 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 18
- 239000007788 liquid Substances 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 239000002253 acid Substances 0.000 abstract 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 150000003017 phosphorus Chemical class 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/58—Ammonia
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention relates to a method and a system for recycling tail gas of an ammonia pretreatment process of iron phosphate wastewater, wherein the method utilizes the iron phosphate wastewater with the pH value of about 2 to be acidic, the iron phosphate wastewater passes through an ammonia recycling system, enters a mixing reaction tank to adjust the pH value to 8-9 for mixed reaction, a large amount of metal impurities are precipitated, part of ammonia nitrogen is solidified, part of ammonia water is hydrolyzed to form ammonia gas, then the ammonia gas flows back to the ammonia recycling system, and the ammonia gas fully reacts with the follow-up entering iron phosphate wastewater to purify tail gas, and the tail gas is intensively discharged after reaching standards. According to the invention, ammonia in the waste gas is recycled, so that the use cost of ammonia water is reduced; the ferric phosphate wastewater is used for replacing sulfuric acid, ammonia is solidified, the use cost of the sulfuric acid is reduced, and the wastewater treatment capacity is reduced; meanwhile, the cost of manual equipment is reduced, a tail gas absorbing and collecting device is replaced, and the acid absorbing liquid does not need to be replaced periodically.
Description
Technical Field
The invention belongs to the technical field of industrial tail gas treatment, relates to nitrogen-containing tail gas treatment, and particularly relates to a tail gas recovery method and system for an ammonia pretreatment process of ferric phosphate wastewater.
Background
The ammonia pretreatment process is a prepositive process for recycling industrial reclaimed water, ammonia water is used for adjusting the PH of the ferric phosphate industrial wastewater, and partial ammonia water volatilizes during treatment to form ammonia escape.
A large amount of wastewater is generated in the ferric phosphate production process, and the wastewater contains a large amount of metal impurities, phosphorus elements, sulfate ions, ammonia nitrogen and PH of about 2. The treatment process of the ferric phosphate wastewater is generally divided into three parts: namely a pretreatment part, an RO part and an MVR evaporation part; in the pretreatment part, a large amount of ammonia water is needed to enable the PH of the wastewater to reach 8.5, and metal impurities, phosphorus elements and ammonia nitrogen in the ferric phosphate wastewater react to generate phosphorus salt precipitate; in the process, a large amount of ammonia water is hydrolyzed to form ammonia gas escape, and the escaped ammonia gas can be collected for centralized treatment for organized emission.
The traditional ammonia-containing tail gas treatment generally uses an absorption method, free ammonia gas is absorbed and solidified by sulfuric acid to form ammonium sulfate, then the ammonium sulfate wastewater is pretreated, and liquid ammonium sulfate is evaporated and crystallized by an RO system and an MVR evaporation system to form a compound fertilizer, so that the compound fertilizer has certain economic value; the disadvantage of the traditional process is that a large amount of dilute sulfuric acid needs to be prepared for the equipment every day to absorb and solidify ammonia gas; when the dilute sulfuric acid is prepared, a large amount of tap water or reclaimed water is needed, and after the ammonia gas is absorbed by the dilute sulfuric acid, the dilute sulfuric acid is treated by an RO system and an MVR evaporation system, so that the running cost is increased.
Therefore, the treatment process of the ammonia-containing waste gas needs to be further optimized and perfected so as to improve the recovery efficiency and reduce the consumption.
Disclosure of Invention
The invention aims to solve the problems in the prior art, and provides a method and a system for recycling tail gas of an ammonia pretreatment process of iron phosphate wastewater, which are used for solidifying ammonia by utilizing the iron phosphate wastewater and recycling the ammonia in the waste gas.
The invention is realized by the following technical scheme:
the method for recycling the tail gas of the ammonia pretreatment process of the iron phosphate wastewater utilizes the iron phosphate wastewater with the pH value of about 2, the iron phosphate wastewater passes through an ammonia recycling system, enters a mixing reaction tank to adjust the pH value to 8-9 for mixed reaction, a large amount of metal impurities are precipitated, part of ammonia nitrogen is solidified, part of ammonia water is hydrolyzed to form ammonia gas, then the ammonia gas flows back to the ammonia recycling system, ammonia is fully reacted with the follow-up entering iron phosphate wastewater to purify the tail gas, and the tail gas is intensively discharged after reaching standards.
The method for recovering tail gas of the ammonia pretreatment process of the ferric phosphate wastewater comprises the following operation steps:
firstly, the ferric phosphate wastewater enters a mixing reaction tank through an ammonia recovery system;
secondly, adding ammonia water into the mixing reaction tank, adjusting the pH to 8-9, precipitating a large amount of metal impurities, and generating ammonia-containing waste gas;
thirdly, ammonia-containing waste gas is recycled to an ammonia recovery system, fully reacts with the subsequently entered ferric phosphate waste water, solidifies ammonia to purify tail gas, and is intensively discharged after reaching the standard.
The system for the tail gas recovery method of the ammonia pretreatment process of the ferric phosphate wastewater comprises an ammonia gas recovery system, a fan and a mixed reaction tank which are connected through pipelines; the ammonia gas recovery system is connected with an outlet of a workshop wastewater pipeline; the mixing reaction tank is connected with an outlet of the ammonia gas recovery system; the inlet of the fan is connected with the gas outlet of the mixing reaction tank, and the outlet is connected with the ammonia recovery system.
The tail gas recovery system of the ammonia pretreatment process of the ferric phosphate wastewater comprises the following components: the ammonia gas recovery system comprises a recovery tower and a PTFE hydrophobic and breathable film; the upper part of the recovery tower is provided with a water inlet and a water outlet, the lower part of the recovery tower is provided with a water inlet and a water outlet, and the water outlet is lower than the water inlet; the water outlet is connected with the mixing reaction tank; the air inlet is connected with the fan; the PTFE hydrophobic breathable film is provided with at least three layers, and the PTFE hydrophobic breathable film is arranged in parallel along the radial direction of the recovery tower.
Advantageous effects
The invention utilizes the ferric phosphate wastewater with the pH value of about 2 to be acidic, can be neutralized with alkaline substances, has certain solidifying capacity for ammonia nitrogen, and enters a mixing reaction tank for mixing reaction after passing through an ammonia recovery device; because the PH of the ferric phosphate wastewater is acidic and the ammonia water is alkaline, acid-base neutralization reaction can occur together, the water temperature rises, and at the moment, the PH of the mixed reaction tank is 8.5, and partial ammonia water can be hydrolyzed to form ammonia gas; the mixing reaction tank forms negative pressure through the fan, ammonia-containing waste gas is pumped to the ammonia recovery system through the pipeline, and ammonia and phosphoric acid ferrite wastewater fully contact and absorb in the ammonia recovery system, so that the tail gas purification function is achieved, and the tail gas is intensively discharged after reaching the standard. The ammonia in the waste gas is recycled, so that the use cost of the ammonia water is reduced; the ferric phosphate wastewater is used for replacing sulfuric acid, ammonia is solidified, the use cost of the sulfuric acid is reduced, and the wastewater treatment capacity is reduced; meanwhile, the cost of manual equipment is reduced, a tail gas recovery device is replaced, and periodic replacement is not needed.
Drawings
FIG. 1 is a schematic diagram of the tail gas recovery system of the ammonia pretreatment process of the iron phosphate wastewater.
FIG. 2 is a schematic diagram of an ammonia recovery system of an ammonia pretreatment process tail gas recovery system of iron phosphate wastewater according to the invention.
Description of the embodiments
The invention relates to a method for recycling tail gas of an ammonia pretreatment process of ferric phosphate wastewater, which utilizes ferric phosphate wastewater with an acidic pH value of 2.2-2.6, the ferric phosphate wastewater passes through an ammonia recycling system, enters a mixing reaction tank to adjust the pH value to 8-9 for mixed reaction, a large amount of metal impurities are precipitated, part of ammonia nitrogen is solidified, part of ammonia water is hydrolyzed to form ammonia gas, then the ammonia gas flows back to the ammonia recycling system, fully reacts with the follow-up entering ferric phosphate wastewater, the ammonia is solidified to purify tail gas, and the tail gas is intensively discharged after reaching standards.
The method comprises the following operation steps:
firstly, ferric phosphate wastewater with the pH value of 2.2-2.6 enters a mixing reaction tank through an ammonia recovery system;
secondly, adding ammonia water into the mixing reaction tank, adjusting the pH to 8-9, precipitating a large amount of metal impurities, and generating ammonia-containing waste gas;
thirdly, ammonia-containing waste gas is recycled to an ammonia recovery system, fully reacts with the subsequently entered ferric phosphate waste water, solidifies ammonia to purify tail gas, and is intensively discharged after reaching the standard.
As shown in 1 and fig. 2, the tail gas recovery system for the ammonia pretreatment process of the iron phosphate wastewater comprises an ammonia gas recovery system 1, a mixing reaction tank 2 and a fan 3 which are connected through pipelines;
the ammonia gas recovery system 1 is connected with an outlet of a workshop waste water pipeline through a pipeline and comprises a recovery tower 11 and a PTFE hydrophobic and breathable film 12; the upper part of the recovery tower 11 is provided with a water inlet 111 and an air outlet 112, and the lower part is provided with an air inlet 113 and a water outlet 114, wherein the air outlet 112 is lower than the water inlet 111; the PTFE hydrophobic and breathable film 12 is provided with at least three layers and is arranged in parallel along the radial direction of the recovery tower 11;
the mixing reaction tank 2 is connected with a water outlet 111 of the ammonia recovery system 1 through a pipeline;
the fan 3 is connected with a gas outlet of the mixing reaction tank 2 through a pipeline inlet, and the outlet is connected with a gas inlet 113 of the ammonia recovery system 1.
According to the tail gas recovery system for the ammonia pretreatment process of the ferric phosphate wastewater, when the ferric phosphate wastewater enters from the water inlet at the upper part of the ammonia recovery system 1, the ammonia-containing waste gas generated by the mixing reaction tank 2 flows above the PTFE hydrophobic breathable film 12, and the ammonia-containing waste gas enters from the bottom of the PTFE hydrophobic breathable film 12 and passes through the air permeability of the PTFE hydrophobic breathable film 12, a large number of tiny bubbles are formed to fully contact with the ferric phosphate wastewater, so that a large amount of ammonia in the ammonia-containing waste gas is absorbed and solidified, the waste gas is purified, and the waste gas is intensively discharged after reaching standards.
Examples
The PH of the ferric phosphate wastewater is 2.48, and the PH of the wastewater after entering an ammonia recovery system is 2.95;
ammonia water is added after the effluent of the ammonia recovery system enters a mixing reaction tank, and the PH is adjusted to 8.47;
the concentration of the ammonia-containing waste gas generated by the mixing reaction tank is 617mg/m, and after the ammonia-containing waste gas enters an ammonia recovery device for ammonia nitrogen recovery, the concentration of the tail gas is 7.24 mg/m.
Examples
The PH of the ferric phosphate wastewater is 2.45, and the PH of the wastewater after entering an ammonia recovery system is 2.73;
ammonia water is added after the effluent of the ammonia recovery system enters a mixing reaction tank, and the PH is adjusted to 8.35;
the concentration of the ammonia-containing waste gas generated by the mixing reaction tank is 659mg/m, and the concentration of the tail gas is 7.43mg/m after the ammonia-containing waste gas enters an ammonia recovery device for ammonia nitrogen recovery;
examples
The PH of the ferric phosphate wastewater is 2.34, and the PH of the wastewater after entering an ammonia recovery system is 2.78;
ammonia water is added after the effluent of the ammonia recovery system enters a mixing reaction tank, and the PH is adjusted to 8.56;
the concentration of ammonia-containing waste gas generated by the mixing reaction tank is 645mg/m, and after the ammonia-containing waste gas enters an ammonia recovery device for ammonia nitrogen recovery, the concentration of tail gas is 7.11 mg/m;
by adopting the system provided by the invention, the iron phosphate wastewater with the pH value of 2.4 passes through an ammonia recovery system, enters a mixing reaction tank, is regulated to pH value of 8.5 for mixed reaction, a large amount of metal impurities are precipitated, part of ammonia nitrogen is solidified, part of ammonia water is hydrolyzed into ammonia at the moment, ammonia-containing waste gas is formed and recycled to the ammonia recovery system by a fan, the ammonia-containing waste gas reacts with the continuously entering iron phosphate wastewater, ammonia of the waste gas is absorbed to purify the waste gas, the waste gas is intensively discharged after reaching the standard, and the comparison of the consumption of the ammonia water for one week before and after the improvement of recording equipment is shown in Table 1:
table 1 comparison of Ammonia usage before and after device modification
From Table 1, it can be seen that the ammonia water usage after the equipment modification was reduced by 0.65 ton per day on average.
Claims (4)
1. The method for recovering tail gas of the ammonia pretreatment process of the iron phosphate wastewater comprises the steps of utilizing the iron phosphate wastewater with the pH value of about 2 to be acidic, enabling the iron phosphate wastewater to pass through an ammonia recovery system, enabling the iron phosphate wastewater to enter a mixing reaction tank to adjust the pH value to 8-9 for carrying out mixed reaction, precipitating a large amount of metal impurities, solidifying part of ammonia nitrogen, hydrolyzing part of ammonia water to form ammonia gas, then refluxing the ammonia gas to the ammonia recovery system, fully reacting with the follow-up entering iron phosphate wastewater to absorb ammonia so as to purify the tail gas, and intensively discharging the tail gas after reaching standards.
2. The method for recycling tail gas of the ammonia pretreatment process of the ferric phosphate wastewater according to claim 1 comprises the following operation steps:
firstly, the ferric phosphate wastewater enters a mixing reaction tank through an ammonia recovery system;
secondly, adding ammonia water into the mixing reaction tank, adjusting the pH to 8-9, precipitating a large amount of metal impurities, and generating ammonia-containing waste gas;
thirdly, ammonia-containing waste gas is recycled to an ammonia recovery system, fully reacts with the subsequently entered ferric phosphate waste water, solidifies ammonia to purify tail gas, and is intensively discharged after reaching the standard.
3. An iron phosphate wastewater ammonia pretreatment process tail gas recovery system is characterized in that: the system comprises an ammonia gas recovery system, a fan and a mixed reaction tank which are connected through pipelines;
the ammonia gas recovery system is connected with an outlet of a workshop wastewater pipeline;
the mixing reaction tank is connected with an outlet of the ammonia gas recovery system;
the inlet of the fan is connected with the gas outlet of the mixing reaction tank, and the outlet is connected with the ammonia recovery system.
4. The tail gas recovery system for an ammonia pretreatment process of ferric phosphate wastewater as claimed in claim 3, wherein: the ammonia gas recovery system comprises a recovery tower and a PTFE hydrophobic and breathable film;
the upper part of the recovery tower is provided with a water inlet and a water outlet, the lower part of the recovery tower is provided with a water inlet and a water outlet, and the water outlet is lower than the water inlet; the water outlet is connected with the mixing reaction tank; the air inlet is connected with the fan;
the PTFE hydrophobic breathable film is provided with at least three layers, and the PTFE hydrophobic breathable film is arranged in parallel along the radial direction of the recovery tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310587215.7A CN116531924A (en) | 2023-05-19 | 2023-05-19 | Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310587215.7A CN116531924A (en) | 2023-05-19 | 2023-05-19 | Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater |
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| Publication Number | Publication Date |
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| CN116531924A true CN116531924A (en) | 2023-08-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202310587215.7A Pending CN116531924A (en) | 2023-05-19 | 2023-05-19 | Tail gas recovery method and system for ammonia pretreatment process of ferric phosphate wastewater |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN216512933U (en) * | 2021-12-23 | 2022-05-13 | 中化(浙江)膜产业发展有限公司 | Waste water treatment device |
| CN115557481A (en) * | 2022-10-24 | 2023-01-03 | 安徽南都华铂新材料科技有限公司 | Recycling method of iron phosphate slag recycled by ammonia water |
| CN218188871U (en) * | 2021-12-25 | 2023-01-03 | 常州锂源新能源科技有限公司 | Material circulating system for iron phosphate synthesis |
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- 2023-05-19 CN CN202310587215.7A patent/CN116531924A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN216512933U (en) * | 2021-12-23 | 2022-05-13 | 中化(浙江)膜产业发展有限公司 | Waste water treatment device |
| CN218188871U (en) * | 2021-12-25 | 2023-01-03 | 常州锂源新能源科技有限公司 | Material circulating system for iron phosphate synthesis |
| CN115557481A (en) * | 2022-10-24 | 2023-01-03 | 安徽南都华铂新材料科技有限公司 | Recycling method of iron phosphate slag recycled by ammonia water |
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