CN111892222A - Ammonium sulfate wastewater recycling method - Google Patents
Ammonium sulfate wastewater recycling method Download PDFInfo
- Publication number
- CN111892222A CN111892222A CN202010754919.5A CN202010754919A CN111892222A CN 111892222 A CN111892222 A CN 111892222A CN 202010754919 A CN202010754919 A CN 202010754919A CN 111892222 A CN111892222 A CN 111892222A
- Authority
- CN
- China
- Prior art keywords
- ammonium sulfate
- water
- recycling
- ammonia
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses a method for recycling ammonium sulfate wastewater, which comprises the following steps: carrying out membrane treatment on the ammonium sulfate wastewater, concentrating to obtain ammonium sulfate concentrated water, and then reacting with sodium hydroxide until the pH value is 10-12; separating ammonia gas from liquid by adopting a stripping method, absorbing the obtained ammonia gas by using water or ammonia water, and recycling the ammonia gas until metatitanic acid is neutralized by adding ammonia water, wherein the ammonia gas is obtained in the wet desulphurization process; carrying out MVR treatment on the solution subjected to the stripping treatment, and separating and concentrating to obtain sodium sulfate; preparing sodium sulfate into high-salt water, and further preparing the high-salt water into sodium hydroxide for recycling to the step S2. According to the invention, ammonium sulfate which is often used as a fertilizer is recycled, so that the waste and side pair recycling is realized while the environment-friendly treatment pressure of high ammonia nitrogen wastewater is reduced, the corresponding raw material cost is reduced, and the waste and side pair recycling in production is promoted.
Description
[ technical field ] A method for producing a semiconductor device
The invention belongs to the technical field of waste and side recycling, and particularly relates to a method for recycling ammonium sulfate wastewater.
[ background of the invention ]
In recent years, with the rapid development of industry and the increasing severity of environmental problems, the emission standards of chemical enterprises are more strict, and low emission of ammonia nitrogen is frequently required. Ammonia nitrogen refers to ammonia (NH) existing in water in a free state3) And ammonium ion (NH)4 +) Excessive ammonia nitrogen is discharged into the water body, so that the water body is eutrophicatedAquatic plants and animals die. The traditional treatment method of ammonia nitrogen in water body includes stripping method, zeolite deamination method and breakpoint chlorination method. Wherein, the stripping method (including air or water vapor) has simple process, stable effect and large energy consumption, especially the stripping process (adopting water vapor stripping) and the effluent ammonia nitrogen is still higher; the zeolite deamination needs to consider the regeneration problem of the zeolite; the breakpoint chlorination process is costly and produces harmful gases.
Titanium dioxide has the characteristics of excellent whiteness, covering power, weather resistance, chemical stability and the like, and is widely applied to the fields of coatings, plastics, papermaking, printing ink and the like.
The traditional sulfuric acid method titanium dioxide production process comprises the following steps:
(1) acid hydrolysis: carrying out acidolysis reaction on the titanium concentrate or the acid-soluble waste residue and sulfuric acid to obtain titanyl sulfate;
(2) hydrolysis: hydrolyzing titanyl sulfate to obtain metatitanic acid slurry;
(3) first washing: washing the hydrolyzed metatitanic acid slurry with water;
(4) bleaching and secondary washing: bleaching and washing the metatitanic acid after washing with calcined crystal seeds to obtain metatitanic acid slurry qualified in washing;
(5) salt treatment: performing salt treatment on the metatitanic acid qualified by washing, and performing filter pressing to obtain a filter cake before the kiln;
(6) and (3) calcining: feeding the filter cake in front of the kiln into a rotary kiln for calcining to obtain a kiln product;
(7) and (3) post-treatment: and carrying out organic/inorganic coating and other processes on the kiln product to obtain a finished titanium dioxide product.
The calcination process in the step (6) is divided into four stages of dehydration, desulfurization, crystal form conversion and particle growth, and in production practice, it is found that about 7% of chemisorption sulfuric acid (including a part of bound acid) is still contained in the metatitanic acid qualified by bleaching and washing in the step (4), the part of sulfuric acid cannot be removed in the washing process, and can be removed only at high temperature in the calcination kiln, and simultaneously, the rutile conversion and particle growth can be inhibited, so that the cost of tail gas treatment is increased, the calcination energy consumption is increased, material sintering is easily caused at high temperature, and the post-grinding is difficult.
A method of wet desulfurization by neutralization with aqueous ammonia is disclosed in patent publication No. CN 108408770A. In the method, the metatitanic acid is neutralized by ammonia water, so that the sulfur content in the titanium dioxide is reduced. In the process, although the content of sulfur oxides generated in the calcining process is reduced and the pressure for treating calcining tail gas is reduced, a large amount of ammonium sulfate waste water is generated, and the pressure for treating the ammonium sulfate waste water is brought. At present, a plurality of treatment methods are adopted as membrane treatment methods, although the ammonium sulfate wastewater can be treated by membrane treatment, the method is simple and convenient to operate and free of secondary pollution, but because a filtering membrane has the requirement of the upper limit of ammonia nitrogen in inlet water in the membrane treatment process, the treatment concentration is limited, and the yield is not high.
[ summary of the invention ]
The invention aims to provide a method for recycling ammonium sulfate wastewater to overcome the defects of the prior art.
The purpose of the invention is realized by the following technical scheme:
a method for recycling ammonium sulfate wastewater comprises the following steps:
s1: firstly, carrying out membrane treatment on the ammonium sulfate wastewater, and concentrating to obtain ammonium sulfate concentrated water;
s2: taking the ammonium sulfate concentrated water obtained in the step S1 to react with sodium hydroxide until the pH value is 10-12, and generating ammonia gas;
s3: separating ammonia gas from liquid by adopting a stripping method, absorbing the obtained ammonia gas by using water or ammonia water, and recycling the ammonia gas until metatitanic acid is neutralized by adding ammonia water, wherein the ammonia gas is obtained in the wet desulphurization process;
s4: carrying out MVR evaporation concentration system treatment on the solution subjected to the stripping treatment in the step S3, and separating and concentrating to obtain sodium sulfate;
s5: and (4) preparing high-salt water from the sodium sulfate treated by the MVR evaporation concentration system in the step S4, and further preparing the high-salt water into sodium hydroxide for recycling to the step S2.
Preferably, the ammonia nitrogen content of the concentrated ammonium sulfate water subjected to the membrane treatment in the step S1 is 7000-12000 mg/L.
Preferably, the mass fraction of the sodium hydroxide used in step S2 is 20-50%.
Preferably, the air stripping method of step S3 uses air for air stripping.
Preferably, the ammonia gas removal rate of the solution subjected to the stripping treatment in the step S3 is 50-90%.
Preferably, the membrane treatment of step S1 is a reverse osmosis membrane treatment.
Preferably, the ammonium sulfate wastewater is generated in the wet desulphurization process by adding ammonia water to neutralize metatitanic acid
According to the invention, the ammonium sulfate which is often used as a fertilizer is recycled on the basis of the prior art, so that the waste and the auxiliary are recycled while the environment-friendly treatment pressure of the high-ammonia nitrogen wastewater is reduced, the corresponding raw material cost is reduced, and the recycling of the waste and the auxiliary in production is promoted.
[ detailed description ] embodiments
The invention provides a method for recycling ammonium sulfate wastewater, which comprises the following steps:
s1: firstly, treating the ammonium sulfate wastewater by a membrane to improve the concentration of ammonium sulfate and obtain concentrated ammonium sulfate water;
s2: taking the ammonium sulfate concentrated water obtained in the step S1 to react with sodium hydroxide generated in a chlor-alkali process until the pH value is 10-12, and generating ammonia gas;
s3: separating ammonia gas from liquid by adopting a stripping method, absorbing the obtained ammonia gas by using water or ammonia water, and recycling the ammonia gas until metatitanic acid is neutralized by adding ammonia water, wherein the ammonia gas is obtained in the wet desulphurization process; removing ammonia gas by a stripping method, wherein the removal rate is 50-90%; specifically, ammonia-containing ammonium sulfate concentrated water is blown off by air or steam, ammonia continuously escapes from the solution in the blowing-off process and is discharged from an ammonia outlet, most of ammonia nitrogen in the solution after blowing-off is removed, and the ammonia-containing ammonium sulfate concentrated water also contains a small amount of ammonia nitrogen and a large amount of sulfate radicals and sodium ions;
s4: carrying out MVR evaporation concentration system treatment on the solution subjected to the air stripping treatment in the step S3, separating ammonia nitrogen, sulfate radical and sodium ions, allowing the ammonia nitrogen to enter an evaporation condensate system, separating out sodium sulfate in a solid salt form, and centrifuging to obtain sodium sulfate solid and mother liquor containing sodium sulfate, so that the solution subjected to the air stripping treatment can be separated and concentrated to obtain sodium sulfate and evaporation condensate containing ammonia nitrogen after the air stripping treatment; specifically, the MVR evaporation and concentration system generally comprises a preheater, an evaporator, a gas-liquid separator, a crystallizer, a centrifuge, a compressor, a pump set and other components, secondary steam which is compressed, heated and boosted is recycled, ammonia nitrogen can be evaporated and enter an evaporation and condensation water system under the alkaline high-temperature condition, and further separation of the ammonia nitrogen and a sodium sulfate solution is realized; separating the sodium sulfate solution after ammonia nitrogen to obtain a concentrated solution, and when the concentrated solution reaches a certain saturated state, allowing the concentrated solution to flow into a crystallizer for crystallization, and further separating the crystallized solution by a centrifuge to obtain sodium sulfate solid and sodium sulfate mother liquor; the MVR evaporation concentration system fully utilizes the latent heat of the steam, so that the heat exchange efficiency is high, and the energy consumption and the operation cost are low;
s5: the sodium sulfate solid obtained after the treatment of the MVR evaporation concentration system in the step S4 basically does not contain ammonia nitrogen, and can be recycled to a chlor-alkali process to prepare high salt water, the high salt water is further prepared to obtain sodium hydroxide, and the sodium hydroxide is recycled to the step S2; the sodium sulfate mother liquor after the sodium sulfate solid is separated out has lower ammonia nitrogen content and can be conveyed to an evaporation concentration system again for circular treatment; the evaporated condensed water containing ammonia nitrogen may be recycled to step S3 for absorbing ammonia gas.
The ammonium sulfate wastewater can be ammonium sulfate wastewater generated by adding ammonia water to neutralize metatitanic acid slurry and performing wet desulphurization disclosed in the patent with the publication number of CN 108408770A.
The chlor-alkali process is a method for preparing sodium hydroxide (NaOH) and chlorine (Cl) by using an electrolytic saturated sodium chloride solution industrially2) And hydrogen (H)2). The method can not leave a chlor-alkali workshop in the production process of the titanium dioxide and is used for producing sodium hydroxide and chlorine.
The method firstly carries out membrane treatment and concentration on the high-concentration ammonium sulfate wastewater generated in the wet desulfurization process of metatitanic acid to obtain high-concentration ammonium sulfate concentrated water, then uses sodium hydroxide to adjust the pH value, and then carries out stripping to separate ammonia gas in liquid. The ammonium sulfate concentration of the high-concentration ammonium sulfate wastewater is further improved by adopting membrane treatment, so that the reaction efficiency with sodium hydroxide can be improved, the alkali consumption is saved, the stripping efficiency can be improved, the energy consumption is reduced, and the ammonia gas with higher concentration is obtained. And absorbing the ammonia gas after stripping separation by water or ammonia water, and recycling the ammonia gas to the wet desulfurization process of the metatitanic acid. The solution after stripping still contains ammonia nitrogen with higher concentration, so the solution after stripping is treated by an MVR evaporation concentration system, and sodium sulfate is obtained by separation and concentration. The obtained sodium sulfate does not contain ammonia nitrogen basically, has high purity, is recycled to the chlor-alkali process to prepare high-salt water, and then is used for preparing sodium hydroxide, and the sodium hydroxide can be recycled to the step S2. Step S2 adopts sodium hydroxide to adjust pH, and compared with the prior art that more calcium hydroxide is used, the generated calcium sulfate has lower solubility, the generated calcium sulfate precipitate needs to be separated from the solution, and the calcium sulfate precipitate cannot be recycled to the chlor-alkali process to prepare high-salt water.
According to the invention, a stripping method, a membrane treatment and an MVR evaporation concentration system are combined, compared with the prior art that only a stripping method is adopted, the concentration of ammonium sulfate is concentrated by adopting the membrane treatment before stripping, high-concentration ammonia gas can be quickly and efficiently separated by subsequent stripping, and the removal rate of ammonia nitrogen is improved, so that the content of ammonia nitrogen in liquid after stripping is lower, in addition, the ammonia nitrogen in a sodium sulfate solution is separated by adopting the MVR treatment after stripping, and the later stripping time can be reduced (along with the reduction of the concentration of ammonia nitrogen, the stripping efficiency is lower). And if only adopt MVR evaporation concentration system, to high concentration ammonia nitrogen desorption efficiency lower than blowing and taking off, consequently use membrane treatment, blow and take off and MVR evaporation concentration system jointly, can synthesize and blow off and get off the higher advantage of high concentration ammonia nitrogen desorption efficiency, and MVR processing system energy consumption is lower to high concentration ammonia nitrogen desorption efficiency, and can solve prior art and only adopt membrane treatment, have the requirement to the ammonia nitrogen upper limit of intaking, the problem that concentration of handling is limited, the yield is not high.
From the analysis, the invention comprehensively utilizes the high-concentration ammonium sulfate wastewater generated in the metatitanic acid production process, and comprehensively utilizes the technologies of sodium hydroxide, air stripping method, membrane treatment, MVR evaporation concentration and the like produced in the existing titanium dioxide production chlor-alkali workshop, has the advantages of the existing air stripping method, membrane treatment and MVR evaporation concentration, efficiently and quickly decomposes the ammonium sulfate into recyclable sodium sulfate and ammonia water, realizes closed loop in the whole treatment process, does not use an additional treating agent, does not discharge any waste, and has good economic benefit and environmental benefit.
Preferably, the ammonia nitrogen content of the concentrated ammonium sulfate water subjected to the membrane treatment in the step S1 is 7000-12000 mg/L. Under the concentration, the method is favorable for quickly and efficiently separating ammonia gas by a stripping method.
Preferably, the concentration of sodium hydroxide used in step S2 is 20 to 50% (mass fraction ω). The concentration of sodium hydroxide generated by the chlor-alkali process is about 30-50%, and the sodium hydroxide can be directly used.
Preferably, the air stripping method in step S3 uses air for stripping, which can save energy consumption compared with steam.
Preferably, in the solution subjected to the air stripping treatment in the step S3, the ammonia removal rate is 50-90%, the air stripping time is short in the removal range, the efficiency is high, the ammonia nitrogen content of the solution subjected to air stripping is appropriate, and the efficiency of subsequent MVR treatment can be improved.
Preferably, step S1 is a reverse osmosis membrane treatment. Reverse osmosis is a process of separating a solvent from a solution by taking pressure difference as a driving force, and has the advantages of low energy consumption, no pollution, simple use and wide application; the reverse osmosis membrane can be a polyamide composite reverse osmosis membrane, a cellulose acetate membrane and the like, and the aperture is 0.5-10 nm.
Example 1
S1: according to the method disclosed in the patent with the publication number of CN108408770A, wet desulphurization is carried out on metatitanic acid slurry, the concentration of ammonium sulfate in the obtained ammonium sulfate wastewater is 9.26g/L, and the content of ammonia nitrogen is 2500 mg/L; then carrying out reverse osmosis membrane treatment on the ammonium sulfate wastewater to obtain ammonium sulfate concentrated water, wherein after the ammonium sulfate concentrated water is subjected to reverse osmosis membrane treatment, the concentration of ammonium sulfate in the ammonium sulfate concentrated water is increased to 25.9g/L, and the content of ammonia nitrogen is 7000 mg/L;
s2: the concentrated ammonium sulfate water reacts with 30 percent NaOH solution produced by a chlor-alkali process until the pH value is 10.8;
s3: air is adopted for stripping, the stripping time is 3 hours, the gas-liquid ratio is 2100, ammonia gas is separated from liquid, the ammonia nitrogen content in the solution obtained after ammonia gas separation is 1050mg/L, the ammonia nitrogen removal rate is 85%, the separated ammonia gas is absorbed by water to obtain ammonia water, and the ammonia water enters a storage tank and is used in wet desulfurization in metatitanic acid desulfurization in the step S1;
s4: carrying out MVR evaporation concentration system treatment on the liquid subjected to stripping treatment, and further evaporating the residual ammonia nitrogen after stripping to enter an evaporation condensate water system; separating out sodium sulfate, and centrifuging to obtain a sodium sulfate solid and a sodium sulfate mother solution;
s5: step S4, sodium sulfate solid obtained after being processed by an MVR evaporation concentration system enters a chlor-alkali process, high salt water is prepared according to the method disclosed in the publication No. CN108675499A, the high salt water is further reacted to obtain sodium hydroxide, and the sodium hydroxide is returned to the step S2 to react with concentrated ammonium sulfate water; and (5) conveying the sodium sulfate mother liquor to an MVR evaporation concentration system again for circulation treatment.
Example 2
S1: according to the method disclosed in the patent with the publication number of CN108408770A, wet desulphurization is carried out on metatitanic acid slurry, and the concentration of ammonium sulfate in the obtained ammonium sulfate wastewater is 7.4g/L, and the content of ammonia nitrogen is 2000 mg/L; then carrying out reverse osmosis membrane treatment on the ammonium sulfate wastewater, concentrating to obtain ammonium sulfate concentrated water, and after membrane treatment, increasing the concentration of ammonium sulfate in the ammonium sulfate concentrated water to 33.3g/L and controlling the content of ammonia nitrogen to 9000 mg/L;
s2: the concentrated ammonium sulfate water reacts with 32 percent NaOH solution produced by a chlor-alkali process until the pH value is 11.4;
s3: air is adopted for blowing, the blowing time is 3 hours, the gas-liquid ratio is 2100, ammonia gas is separated from liquid, the ammonia nitrogen content in the solution obtained after ammonia gas separation is 980mg/L, the ammonia nitrogen removal rate is 89%, the separated ammonia gas is absorbed by water to obtain ammonia water, and the ammonia water enters a storage tank and is used in wet desulfurization in metatitanic acid desulfurization in the step S1;
s4: carrying out MVR evaporation concentration system treatment on the liquid subjected to stripping treatment, and further evaporating the residual ammonia nitrogen to enter an evaporation condensate water system; separating out sodium sulfate, and centrifuging to obtain a sodium sulfate solid and a sodium sulfate mother solution;
s5: step S4, sodium sulfate solid obtained after being processed by an MVR evaporation concentration system enters a chlor-alkali process, high salt water is prepared according to the method disclosed in the publication No. CN108675499A, the high salt water is further reacted to obtain sodium hydroxide, and the sodium hydroxide is returned to the step S2 to react with concentrated ammonium sulfate water; and (5) conveying the sodium sulfate mother liquor to an MVR evaporation concentration system again for circulation treatment.
Comparative example 1
S1: according to the method disclosed in the patent with the publication number of CN108408770A, wet desulphurization is carried out on metatitanic acid slurry, the concentration of ammonium sulfate in the obtained ammonium sulfate wastewater is 11.1g/L, and the content of ammonia nitrogen is 3000 mg/L;
s2: adjusting the pH value of the ammonium sulfate solution to 10.8 by using 30% NaOH solution;
s3: air is adopted for stripping, stripping time is 12h, the gas-liquid ratio is 2300, ammonia gas is separated from liquid, the ammonia nitrogen content in the solution obtained after ammonia gas separation is 1500mg/L, and the ammonia nitrogen removal rate is 50%;
s4: in the sodium sulfate liquid obtained after the stripping in the step S3, the ammonia nitrogen content in the solution is high, so that the sodium sulfate liquid cannot be directly applied to the chlor-alkali process, and the deamination treatment needs to be performed on the water sample again.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. Therefore, it is intended that the appended claims be interpreted as including preferred embodiments and all such alterations and modifications as fall within the scope of the invention. It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (7)
1. The ammonium sulfate wastewater recycling method is characterized by comprising the following steps:
s1: firstly, carrying out membrane treatment on the ammonium sulfate wastewater, and concentrating to obtain ammonium sulfate concentrated water;
s2: taking the ammonium sulfate concentrated water obtained in the step S1 to react with sodium hydroxide until the pH value is 10-12, and generating ammonia gas;
s3: separating ammonia gas from liquid by adopting a stripping method, absorbing the obtained ammonia gas by using water or ammonia water, and recycling the ammonia gas until metatitanic acid is neutralized by adding ammonia water, wherein the ammonia gas is obtained in the wet desulphurization process;
s4: carrying out MVR evaporation concentration system treatment on the solution subjected to the stripping treatment in the step S3, and separating and concentrating to obtain sodium sulfate;
s5: and (4) preparing high-salt water from the sodium sulfate treated by the MVR evaporation concentration system in the step S4, and further preparing the high-salt water into sodium hydroxide for recycling to the step S2.
2. The method for recycling ammonium sulfate wastewater as recited in claim 1,
and the ammonia nitrogen content of the ammonium sulfate concentrated water subjected to the membrane treatment in the step S1 is 7000-12000 mg/L.
3. The method for recycling ammonium sulfate wastewater as recited in claim 1,
the mass fraction of the sodium hydroxide adopted in the step S2 is 20-50%.
4. The method for recycling ammonium sulfate wastewater as recited in claim 1,
the blowing method of step S3 uses air for blowing.
5. The method for recycling ammonium sulfate wastewater as recited in claim 1,
and S3, the ammonia gas removal rate of the solution after the stripping treatment is 50-90%.
6. The method for recycling ammonium sulfate wastewater as recited in claim 1,
the step S1 is a reverse osmosis membrane treatment.
7. The method for recycling ammonium sulfate wastewater as recited in claim 1,
the ammonium sulfate wastewater is generated in the wet desulphurization process by adding ammonia water to neutralize metatitanic acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010754919.5A CN111892222B (en) | 2020-07-31 | 2020-07-31 | Ammonium sulfate wastewater recycling method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010754919.5A CN111892222B (en) | 2020-07-31 | 2020-07-31 | Ammonium sulfate wastewater recycling method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111892222A true CN111892222A (en) | 2020-11-06 |
| CN111892222B CN111892222B (en) | 2023-08-22 |
Family
ID=73182767
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010754919.5A Active CN111892222B (en) | 2020-07-31 | 2020-07-31 | Ammonium sulfate wastewater recycling method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111892222B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114715966A (en) * | 2022-04-08 | 2022-07-08 | 广州市迈源科技有限公司 | Method for separating and purifying ammonium sulfate and ammonium dihydrogen phosphate in wastewater |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331053A (en) * | 2000-06-28 | 2002-01-16 | 中国石油化工集团公司 | Process for reclaiming ammonia-contained sewage |
| CN101891330A (en) * | 2010-07-23 | 2010-11-24 | 深圳市能源环保有限公司 | Power plant wastewater treatment system and method |
| CN103183431A (en) * | 2013-04-03 | 2013-07-03 | 江苏夏航环境工程有限公司 | Ammonia-nitrogen wastewater treatment technology |
| CN104843816A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Method for combined production of ammonium sulfate and ammonia water through heat pump flash evaporation, stripping and deamination |
| CN107758960A (en) * | 2017-10-18 | 2018-03-06 | 江苏理工学院 | A kind of processing method of ammonia waste water |
| CN108675499A (en) * | 2018-05-30 | 2018-10-19 | 龙蟒佰利联集团股份有限公司 | A kind of method of chloride slag mashing waste water integrated treatment |
| US20180305221A1 (en) * | 2017-04-21 | 2018-10-25 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN108726611A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN109205941A (en) * | 2018-10-09 | 2019-01-15 | 浙江奇彩环境科技股份有限公司 | A kind of recycling processing method of high ammonia-nitrogen wastewater with high salt |
| US20190062188A1 (en) * | 2017-08-28 | 2019-02-28 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN208776506U (en) * | 2018-08-17 | 2019-04-23 | 江苏中研创星材料科技有限公司 | High ammonia-containing water zero-discharge treatment system in nano-titanium dioxide production |
| CN210481099U (en) * | 2019-06-14 | 2020-05-08 | 江苏卓博环保科技有限公司 | Recycling treatment device for waste water of recycling waste lithium battery anode material |
-
2020
- 2020-07-31 CN CN202010754919.5A patent/CN111892222B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331053A (en) * | 2000-06-28 | 2002-01-16 | 中国石油化工集团公司 | Process for reclaiming ammonia-contained sewage |
| CN101891330A (en) * | 2010-07-23 | 2010-11-24 | 深圳市能源环保有限公司 | Power plant wastewater treatment system and method |
| CN103183431A (en) * | 2013-04-03 | 2013-07-03 | 江苏夏航环境工程有限公司 | Ammonia-nitrogen wastewater treatment technology |
| CN104843816A (en) * | 2014-02-18 | 2015-08-19 | 中国石油化工股份有限公司 | Method for combined production of ammonium sulfate and ammonia water through heat pump flash evaporation, stripping and deamination |
| US20180305221A1 (en) * | 2017-04-21 | 2018-10-25 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN108726611A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| US20190062188A1 (en) * | 2017-08-28 | 2019-02-28 | China Petroleum & Chemical Corporation | Apparatus and Method for Treating Waste Water Containing Ammonium Salts |
| CN107758960A (en) * | 2017-10-18 | 2018-03-06 | 江苏理工学院 | A kind of processing method of ammonia waste water |
| CN108675499A (en) * | 2018-05-30 | 2018-10-19 | 龙蟒佰利联集团股份有限公司 | A kind of method of chloride slag mashing waste water integrated treatment |
| CN208776506U (en) * | 2018-08-17 | 2019-04-23 | 江苏中研创星材料科技有限公司 | High ammonia-containing water zero-discharge treatment system in nano-titanium dioxide production |
| CN109205941A (en) * | 2018-10-09 | 2019-01-15 | 浙江奇彩环境科技股份有限公司 | A kind of recycling processing method of high ammonia-nitrogen wastewater with high salt |
| CN210481099U (en) * | 2019-06-14 | 2020-05-08 | 江苏卓博环保科技有限公司 | Recycling treatment device for waste water of recycling waste lithium battery anode material |
Non-Patent Citations (4)
| Title |
|---|
| 冯辉等: "《工业纳污坑塘应急治理与综合修复》", 30 June 2020, 天津大学出版社, pages: 70 - 71 * |
| 刘利德等: "酸法联二脲生产中废水的回收利用", 《氯碱工业》, no. 1 * |
| 库尔特•果采著，诸祥坤等译: "《粘胶纤维》", 31 March 1964, 中国财政经济出版社, pages: 212 * |
| 马鹏起等: "《中国稀土强国之梦》", 31 October 2017, 冶金工业出版社, pages: 240 - 241 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114715966A (en) * | 2022-04-08 | 2022-07-08 | 广州市迈源科技有限公司 | Method for separating and purifying ammonium sulfate and ammonium dihydrogen phosphate in wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111892222B (en) | 2023-08-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108046295B (en) | Method for producing sodium bicarbonate and ammonium sulfate by using sodium sulfate solution | |
| CN105036438B (en) | A kind of sodium alkali desulfurization waste liquid method for innocent treatment | |
| CN115947486B (en) | Desulfurization waste liquid recycling treatment process and system | |
| CN102642970A (en) | Method for recycling waste water with high salinity by extracting vanadium from vanadium slag | |
| CN111003869A (en) | Hydrofluoric acid wastewater resource utilization method | |
| CN104355472A (en) | Inorganic ammonium salt-containing wastewater treatment system, treatment process and application of wastewater treatment system | |
| CN1990460A (en) | Comprehensive treatment of glycine crystallization mother liquid | |
| CN103318918A (en) | Method for purification and recovery of ammonia gas | |
| CN111892222B (en) | Ammonium sulfate wastewater recycling method | |
| CN107777691B (en) | Method for recovering fluorine resource in acidic fluorine-containing wastewater | |
| WO2023173776A1 (en) | Recovery method and recovery system for ternary precursor mother liquor | |
| CN111760457A (en) | Method and equipment for regenerating waste salt generated in flue gas desulfurization | |
| CN110844926A (en) | Production method of high-purity magnesium sulfite | |
| CN213060531U (en) | Ammonium sulfate effluent disposal system | |
| CN116102211A (en) | Method for treating synthesis wastewater of battery anode material precursor | |
| CN114560486B (en) | CO with leaching aid capable of being recycled 2 Indirect mineralization method | |
| CN113479985B (en) | Method for transformation deamination of ammonia nitrogen wastewater | |
| CN216073085U (en) | Household garbage incineration fly ash recycling treatment system | |
| CN109809582A (en) | A kind of potassium sulfate Sewage treatment utilizes method | |
| CN108946767B (en) | Method for separating potassium sulfate by using sodium-potassium-sulfur-chlorine quaternary system | |
| CN113896214A (en) | Method for preparing high-purity lithium carbonate by adsorbing and carbonizing lithium sulfate solution | |
| CN111392944A (en) | Treatment method of cuprous cyanide production wastewater | |
| CN105174287A (en) | Method for recovering ammonia and coproducing calcium sulfate through lime neutralization of T acid mother liquid | |
| CN215288069U (en) | System for SRG washing wastewater catalytic desalination | |
| CN112642173B (en) | Amine/ammonia evaporation and absorption integrated device and application method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: No.1669, Zhongjiao Road, jiaokezuo District, Henan Province Applicant after: Longbai Group Co.,Ltd. Address before: No.1669, Zhongjiao Road, jiaokezuo District, Henan Province Applicant before: LOMON BILLIONS GROUP Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |