CN109850972A - A kind of processing system improving ammonia recovery in ternary precursor production waste water - Google Patents
A kind of processing system improving ammonia recovery in ternary precursor production waste water Download PDFInfo
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- CN109850972A CN109850972A CN201910044113.4A CN201910044113A CN109850972A CN 109850972 A CN109850972 A CN 109850972A CN 201910044113 A CN201910044113 A CN 201910044113A CN 109850972 A CN109850972 A CN 109850972A
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- ammonia
- condenser
- ammonium hydroxide
- processing system
- vacuum pump
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Abstract
The invention discloses a kind of processing systems of ammonia recovery in raising ternary precursor production waste water, which includes steam stripping ammonia-removing tower and ammonium hydroxide condenser；Steam stripping ammonia-removing tower is connected with ammonium hydroxide condenser；Jet vacuum pump is set in ammonium hydroxide condenser rear end, jet vacuum pump is connected with tail gas absorption tank；The system equipment is simple, by the way that jet vacuum pump is arranged, greatly increases ammonia recovery, ammonia recovery reaches 98% or more, has a good application prospect.
Description
Technical field
The invention belongs to recovery ammonias in sewage advanced treatment field more particularly to a kind of raising ternary precursor production waste water
The processing system of rate.
Background technique
It is well known that the waste water of ternary precursor production enters in stripping rectifying deammoniation tower, ammonia nitrogen is in the form of molecules of ammonia
It is separated from the water volatilization, the form that ammonia and water vapour mix is discharged from tower top, and is cooled to room temperature as high-purity by condenser
Ammonium hydroxide is recycled, and production can be back to.But in condensation process, usually level-one condensed absorbent, absorption are not exclusively, in addition outer
Ammonia can be mingled in row's tail gas, since the volatilization and condensation of ammonium hydroxide are incomplete, the only ammonium hydroxide of 50-60% is recovered, and causes ammonia
The rate of recovery is low,.
Summary of the invention
In view of the above-mentioned problems, the present invention provides a kind of processing systems of ammonia recovery in raising ternary precursor production waste water
System, the processing system are mainly provided with jet stream in the rear end of ammonium hydroxide condenser on the basis of existing stripping rectifying deamination system
Vacuum pump, jet vacuum pump draw tail gas not condensed in ammonium hydroxide condenser, make to strip rectifying deammoniation tower formation tiny structure,
Convenient for Ammonia valatilization, to improve ammonia recovery；In addition, dilute sulfuric acid absorbing liquid is recycled, cost is not only reduced, and improve
Assimilation effect.
To achieve this purpose, the present invention adopts the following technical scheme:
A kind of processing system improving ammonia recovery in ternary precursor production waste water, the system comprises steam stripping ammonia-removing towers
With ammonium hydroxide condenser；The steam stripping ammonia-removing tower is connected with ammonium hydroxide condenser；
Jet vacuum pump is set in ammonium hydroxide condenser rear end, the jet vacuum pump is connected with tail gas absorption tank.
The system also includes concentrated ammonia liquor storage tank, the concentrated ammonia liquor storage tank is connected with ammonium hydroxide condenser, for laying in ammonium hydroxide condenser
The concentrated ammonia liquor of discharge.
Waste water enters steam stripping ammonia-removing tower, ammonia nitrogen be separated from the water in the form of molecules of ammonia after volatilization and vapor mixing from
Tower top ammonia outlet enters ammonium hydroxide condenser.
Ammonia gas mixture into ammonium hydroxide condenser is condensed into weak aqua ammonia, and weak aqua ammonia is exported by weak aqua ammonia and is discharged, by vapour
The weak aqua ammonia entrance for mentioning deamination tower bottom enters, and further strips rectifying concentrate.
The concentrated ammonia liquor condensed through ammonium hydroxide condenser enters concentrated ammonia liquor storage tank.
Not condensed tail gas enters jet vacuum pump in the ammonium hydroxide condenser, reacts with sulfuric acid solution and generates sulfuric acid
Ammonium.
The tail gas that jet vacuum pump generates is discharged into tail gas absorption filling.
The overall recovery of ammonia can achieve 98% or more after this system is handled.
Compared with prior art, the invention has the following advantages:
1) the invention discloses a kind of new processing system of ammonia recovery in raising ternary precursor production waste water, the systems
Equipment is simple, and ammonia recovery reaches 98% or more；
2) present invention draws tail gas by jet vacuum pump, makes to strip rectifying deammoniation tower formation negative pressure, carries out multiple condensation
It absorbs, is convenient for Ammonia valatilization, recycle dilute sulfuric acid absorbing liquid, reduce cost, improve assimilation effect, before boundless application
Scape.
Detailed description of the invention
Fig. 1 is the processing system flow chart that the present invention improves ammonia recovery in ternary precursor production waste water.
In figure: 1- steam stripping ammonia-removing tower；2- ammonium hydroxide condenser；3- jet vacuum pump；4- tail gas absorption tank；The storage of 5- concentrated ammonia liquor
Tank.
Specific embodiment
In order to better illustrate the present invention, it is easy to understand technical solution of the present invention, of the invention is typical but non-limiting
Embodiment is as follows:
As shown in Figure 1, a kind of processing system for improving ammonia recovery in ternary precursor production waste water, which includes vapour
Mention deammoniation tower 1 and ammonium hydroxide condenser 2；Steam stripping ammonia-removing tower 1 is connected with ammonium hydroxide condenser 2；In 2 rear end of ammonium hydroxide condenser, setting is penetrated
Flow vacuum pump 3, jet vacuum pump 3 is connected with tail gas absorption tank 4.The system further includes concentrated ammonia liquor storage tank 5, concentrated ammonia liquor storage tank 5
It is connected with ammonium hydroxide condenser 2, for laying in the concentrated ammonia liquor of the discharge of ammonium hydroxide condenser 2.
In production application, nitrogen-containing wastewater enters steam stripping ammonia-removing tower 1, and ammonia nitrogen is divided from water in the form of molecules of ammonia
Enter ammonium hydroxide condenser 2 from tower top ammonia outlet from after volatilization and vapor mixing, the ammonia into ammonium hydroxide condenser 2 mixes
Gas is condensed into weak aqua ammonia, and weak aqua ammonia is exported by weak aqua ammonia and is discharged, and is entered by the weak aqua ammonia entrance of 1 bottom of steam stripping ammonia-removing tower, into
One step strips rectifying concentrate, by repeatedly returning to stripping rectifying deammoniation tower concentrate, ultimately forms concentrated ammonia liquor and enters concentrated ammonia liquor storage tank
5, which can return to production and reuse.
And tail gas not condensed in ammonium hydroxide condenser 2 enters jet vacuum pump 3, reacts with sulfuric acid solution and generates sulfuric acid
Ammonium, the tail gas that jet vacuum pump 3 generates at the same time are discharged into tail gas absorption tank 4.
The overall recovery of ammonia can achieve 98% or more after this system is handled.
The ternary precursor production waste water of certain enterprise enters in stripping rectifying deammoniation tower, and ammonia nitrogen is in the form of molecules of ammonia from water
The form of middle separation volatilization, ammonia and water vapour mixing is discharged from tower top, and is cooled to room temperature as weak aqua ammonia by condenser, dilute
Ammonium hydroxide strips rectifying deammoniation tower concentrate by repeatedly returning, and becomes concentrated ammonia liquor, can return in production and reuses；It is cold in condenser
During solidifying, due to ammonium hydroxide volatilization and condensation it is incomplete, the only ammonium hydroxide of 50-60% is recovered, after this system,
Uncooled tail gas is drawn from ammonium hydroxide condenser 2 by jet vacuum pump 3, is reacted with dilute sulfuric acid and is become ammonium sulfate, and ammonium sulfate is steady
Qualitative good, non-volatile and decomposition, in addition sulfate of ammoniac has very high water solubility, and such absorbing liquid can be recycled.Recycling
Ammonium sulfate can return to production, the preparation for metallic solution.Tail gas absorption process in this way, the overall recovery of ammonia can
To reach 98% or more.
The Applicant declares that the present invention is explained by the above embodiments method detailed of the invention, but the present invention not office
Be limited to above-mentioned method detailed, that is, do not mean that the invention must rely on the above detailed methods to implement.Technical field
Technical staff it will be clearly understood that any improvement in the present invention, equivalence replacement and auxiliary element to each raw material of product of the present invention
Addition, selection of concrete mode etc., all of which fall within the scope of protection and disclosure of the present invention.
Claims (6)
1. a kind of processing system for improving ammonia recovery in ternary precursor production waste water, which is characterized in that the system comprises
Steam stripping ammonia-removing tower (1) and ammonium hydroxide condenser (2)；The steam stripping ammonia-removing tower (1) is connected with ammonium hydroxide condenser (2)；
Jet vacuum pump (3) are set in ammonium hydroxide condenser (2) rear end, the jet vacuum pump (3) and tail gas absorption tank (4)
It is connected.
2. processing system as described in claim 1, which is characterized in that described dense the system also includes concentrated ammonia liquor storage tank (5)
Tank used for storing ammonia (5) is connected with ammonium hydroxide condenser (2), for laying in the concentrated ammonia liquor of ammonium hydroxide condenser (2) discharge.
3. processing system as claimed in claim 2, which is characterized in that waste water enters steam stripping ammonia-removing tower (1), and ammonia nitrogen is with molecules of ammonia
Form be separated from the water volatilization and vapor mixing after from tower top ammonia outlet enter ammonium hydroxide condenser (2).
4. processing system as claimed in claim 3, which is characterized in that the ammonia gas mixture for entering ammonium hydroxide condenser (2) is cold
It coagulates for weak aqua ammonia, weak aqua ammonia is exported by weak aqua ammonia and is discharged, and is entered by the weak aqua ammonia entrance of steam stripping ammonia-removing tower (1) bottom, further
Strip rectifying concentrate.
5. processing system as claimed in claim 4, which is characterized in that through ammonium hydroxide condenser (2) obtained concentrated ammonia liquor of condensation into
Enter concentrated ammonia liquor storage tank (5).
6. processing system as claimed in claim 5, which is characterized in that not condensed tail gas in the ammonium hydroxide condenser (2)
Into jet vacuum pump (3), is reacted with sulfuric acid solution and generate ammonium sulfate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910044113.4A CN109850972A (en) | 2019-01-17 | 2019-01-17 | A kind of processing system improving ammonia recovery in ternary precursor production waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910044113.4A CN109850972A (en) | 2019-01-17 | 2019-01-17 | A kind of processing system improving ammonia recovery in ternary precursor production waste water |
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| CN109850972A true CN109850972A (en) | 2019-06-07 |
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| CN201910044113.4A Pending CN109850972A (en) | 2019-01-17 | 2019-01-17 | A kind of processing system improving ammonia recovery in ternary precursor production waste water |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN104789273A (en) * | 2015-03-27 | 2015-07-22 | 山东钢铁股份有限公司 | System for recycling coke oven raw-gas benzene substances by using raw-gas waste heat |
| CN108325343A (en) * | 2018-04-17 | 2018-07-27 | 江苏凯利美环保科技有限公司 | Integrated high-efficiency ammonia recovery unit |
| CN207877296U (en) * | 2018-01-12 | 2018-09-18 | 宜宾光原锂电材料有限公司 | A kind of ternary precursor Coal Gas Washing Cycling Water ammonia water recovery device |
-
2019
- 2019-01-17 CN CN201910044113.4A patent/CN109850972A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN104789273A (en) * | 2015-03-27 | 2015-07-22 | 山东钢铁股份有限公司 | System for recycling coke oven raw-gas benzene substances by using raw-gas waste heat |
| CN207877296U (en) * | 2018-01-12 | 2018-09-18 | 宜宾光原锂电材料有限公司 | A kind of ternary precursor Coal Gas Washing Cycling Water ammonia water recovery device |
| CN108325343A (en) * | 2018-04-17 | 2018-07-27 | 江苏凯利美环保科技有限公司 | Integrated high-efficiency ammonia recovery unit |
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| PB01 | Publication | ||
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| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: No. 33, Changcheng Road, west of Changcheng road and north of Shiji Avenue, Dawukou District, Shizuishan City, Ningxia Hui Autonomous Region Applicant after: BASF Shanshan battery material (Ningxia) Co.,Ltd. Address before: Room 301, management committee office building, Shizuishan hi tech Industrial Development Zone, Ningxia Hui Autonomous Region Applicant before: SHANSHAN ENERGY (NINGXIA) Co.,Ltd. |
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| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190607 |
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