CN213708033U - Lithium manganate effluent disposal system - Google Patents
Lithium manganate effluent disposal system Download PDFInfo
- Publication number
- CN213708033U CN213708033U CN202022604585.1U CN202022604585U CN213708033U CN 213708033 U CN213708033 U CN 213708033U CN 202022604585 U CN202022604585 U CN 202022604585U CN 213708033 U CN213708033 U CN 213708033U
- Authority
- CN
- China
- Prior art keywords
- pretreatment tank
- tank
- ammonia
- negative pressure
- lime pretreatment
- 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.)
- Active
Links
Images
Landscapes
- Removal Of Specific Substances (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
The utility model discloses a lithium manganate wastewater treatment system, which comprises a dosing system, and a heavy metal pretreatment tank, a primary lime pretreatment tank, a centrifugal device, a secondary lime pretreatment tank, a resolving device, a clarification tank and a negative pressure ammonia distillation system which are connected in sequence; the heavy metal pretreatment tank, the secondary lime pretreatment tank and the analysis device are all connected with a dosing system; the bottom of the second-stage lime pretreatment tank is provided with the concentrated slurry pipe, and the other end of the concentrated slurry pipe is communicated with the first-stage lime pretreatment tank.
Description
Technical Field
The utility model relates to a lithium manganate effluent treatment field especially relates to lithium ion battery waste water treatment.
Background
The lithium ion battery is a novel high-energy battery which is rapidly developed in recent years, is a high and new technology industry which is greatly supported by the nation and is widely applied to the fields of new energy automobiles and the like. However, in the production process, a large amount of ammonium sulfate wastewater containing heavy metals such as nickel, cobalt, manganese and the like is generated, the wastewater is acidic, the content of ammonium sulfate is extremely high, and the heavy metals in the wastewater and ammonia are easy to form metal-ammonia complexes.
Liquid caustic soda is mostly adopted for conventional treatment to adjust the pH value to be more than 12, heavy metals are fully removed and then deamination treatment is carried out, finally a membrane system is utilized to generate clear water, but the investment cost is high, the liquid caustic soda consumption is extremely high, the operation cost is high, the salt concentration in wastewater is extremely high, the metal is difficult to completely remove by the formed metal-ammonia complex, the heavy metals still can precipitate in the deamination treatment process to block equipment, and the membrane flux is greatly reduced by the high salt content in the wastewater. Therefore, it is very urgent to develop an efficient and low-cost treatment process.
SUMMERY OF THE UTILITY MODEL
The utility model aims at solving the problems in the prior art and providing a lithium manganate wastewater treatment system with scientific system design, low operation cost and good treatment effect.
In order to realize the purpose of the utility model, the technical proposal of the utility model is that:
a lithium manganate wastewater treatment system comprises a dosing system, and a heavy metal pretreatment tank, a primary lime pretreatment tank, a centrifugal device, a secondary lime pretreatment tank, a resolving device, a clarification tank and a negative pressure ammonia distillation system which are sequentially connected; the heavy metal pretreatment tank, the secondary lime pretreatment tank and the analysis device are all connected with a dosing system; the bottom of the second-stage lime pretreatment tank is provided with a concentrated slurry pipe, and the other end of the concentrated slurry pipe is communicated with the first-stage lime pretreatment tank.
Preferably, the negative-pressure ammonia distillation system comprises a preheater, a negative-pressure ammonia distillation tower, a condenser, a gas-liquid separation tank and an ammonia recovery device which are connected in sequence; the supernatant in the clarification tank is connected with a liquid inlet at the lower part of the preheater through a pipeline, and a liquid outlet at the top of the preheater is connected with an inlet at the upper part of the negative pressure ammonia distillation tower; the lower part of the negative pressure ammonia still is provided with a steam inlet and a high-temperature clear water outlet, the high-temperature clear water outlet is connected with a heat source inlet at the lower part of the preheater, and a water outlet at the upper part of the preheater is connected with a water outlet pool; an ammonia-containing steam outlet at the top of the negative-pressure ammonia distillation tower is connected with a condenser, a condensate outlet of the condenser is connected with the top of a gas-liquid separation tank, a dilute ammonia water outlet at the bottom of the gas-liquid separation tank is connected with an inlet at the upper part of the negative-pressure ammonia distillation tower, and an uncondensed ammonia gas outlet on the side wall of the gas-liquid separation tank is connected with an ammonia recovery device.
Preferably, a buffer pool is further arranged between the secondary lime pretreatment tank and the analysis device.
Preferably, the centrifuge device is a gypsum centrifuge.
Preferably, the pH value in the primary lime pretreatment tank is adjusted to 7-8.
Preferably, the pH value in the secondary lime pretreatment tank is adjusted to 11-11.5.
The utility model has the advantages that:
firstly, the method comprises the following steps: the system design is scientific, the lime is used for adjusting the pH value, the operation cost can be greatly reduced, and the produced gypsum is treated to ensure that the gypsum does not contain heavy metal, does not have ammonia smell and can be recycled;
secondly, the method comprises the following steps: removing calcium ions in the pretreated wastewater by using ammonium bicarbonate, and introducing no other ions, wherein the introduced ammonia nitrogen can be recycled during ammonia distillation treatment;
thirdly, the method comprises the following steps: the ammonia distillation tower adopts negative pressure ammonia distillation, the material requirement is low, the steam consumption is 70-90kg/t less, the ammonia nitrogen removal rate is more than 99.5 percent, and the ammonia nitrogen of effluent is less than 15 mg/L; meanwhile, more than 20% of high-concentration ammonia water can be recovered.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 10 is a dosing system, 20 is a heavy metal pretreatment tank, 30 is a primary lime pretreatment tank, 40 is a centrifugal device, 50 is a secondary lime pretreatment tank, 51 is a thickening slurry pipe, 60 is a buffer tank, 70 is a resolving device, 80 is a clarification tank, 90 is a negative pressure ammonia distillation system, 91 is a preheater, 92 is a negative pressure ammonia distillation tower, 92.1 is a steam inlet, 92.2 is a high-temperature clear water outlet, 93 is a condenser, 94 is a gas-liquid separation tank, and 95 is an ammonia recovery device.
Detailed Description
The technical solution in the embodiment of the present invention is clearly and completely described below with reference to the accompanying drawings.
A lithium manganate wastewater treatment system comprises a dosing system 10, and a heavy metal pretreatment tank 20, a primary lime pretreatment tank 30, a centrifugal device 40, a secondary lime pretreatment tank 50, a resolving device 70, a clarification tank 80 and a negative pressure ammonia distillation system 90 which are sequentially connected; the heavy metal pretreatment tank 20, the secondary lime pretreatment tank 50 and the analysis device 70 are all connected with the dosing system 10; the bottom of the second-stage lime pretreatment tank 50 is provided with a concentrated slurry pipe 51, and the other end of the concentrated slurry pipe 51 is communicated with the first-stage lime pretreatment tank 30.
Preferably, the negative pressure ammonia distillation system 90 comprises a preheater 91, a negative pressure ammonia distillation tower 92, a condenser 93, a gas-liquid separation tank 94 and an ammonia recovery device 95 which are connected in sequence; the supernatant in the clarification tank 80 is connected with a liquid inlet at the lower part of the preheater 91 through a pipeline, and a liquid outlet at the top of the preheater 91 is connected with an inlet at the upper part of the negative pressure ammonia distillation tower 92; the lower part of the negative pressure ammonia still 92 is provided with a steam inlet 92.1 and a high temperature clean water outlet 92.2, the high temperature clean water outlet 92.2 is connected with a heat source inlet at the lower part of the preheater 91, and a water outlet (not shown in the figure) at the upper part of the preheater 91 is connected with a water outlet pool (not shown in the figure); an ammonia-containing steam outlet at the top of the negative pressure ammonia still 92 is connected with a condenser 93, a condensate outlet of the condenser 93 is connected with the top of a gas-liquid separation tank 94, a dilute ammonia water outlet at the bottom of the gas-liquid separation tank 94 is connected with an inlet at the upper part of the negative pressure ammonia still 92, and an uncondensed ammonia gas outlet on the side wall of the gas-liquid separation tank 94 is connected with an ammonia recovery device 95.
Preferably, a buffer tank 60 is further provided between the secondary lime pretreatment tank 50 and the analyzing device 70.
Preferably, the centrifuge apparatus 40 is a gypsum centrifuge.
Preferably, the pH value in the primary lime pretreatment tank 30 is adjusted to 7-8.
Preferably, the pH value in the secondary lime pretreatment tank 50 is adjusted to 11-11.5.
The dosing system 10 includes a plurality of dosing tanks, dosing pipes, and a metering pump as needed, which is the prior art and is not described herein again.
The heavy metal pretreatment tank 20, the primary lime pretreatment tank 30, and the secondary lime pretreatment tank 50 may be provided with a stirring device and a precipitation device as needed, which is the prior art and will not be described herein again.
The resolving device 70 may be a resolving tower, resolving tank, etc. which are prior art and will not be described herein.
The negative pressure ammonia distillation tower 92 is a negative pressure ammonia distillation tower with a self-cleaning tower plate and a self-cleaning mechanical claw, and Chinese patent CN209679534U discloses a distillation tower plate, a self-cleaning mechanism and a distillation tower for preventing distillation scaling, wherein the distillation tower is used for performing negative pressure ammonia distillation, scaling can be effectively prevented, a negative pressure steam stripping process is used, the consumed steam quantity is less, the operation temperature is low, and the problem of corrosion caused by high chlorine ion content in raw water is solved;
the ammonia recovery device 95 may be a device commonly used in the industry such as an ammonia recovery tank, which is the prior art and is not described herein again.
The working principle of the system is as follows:
firstly, the method comprises the following steps: heavy metal removal treatment: lithium manganate wastewater enters a heavy metal pretreatment tank 20 through a lift pump, a dosing system 10 adds a heavy metal capturing agent (the heavy metal capturing agent is preferably organic sulfur or lipid, and the adding amount is 1-5 per mill) into the heavy metal pretreatment tank 20, and the lithium manganate wastewater and the heavy metal capturing agent are fully stirred, mixed and reacted through a stirring device in the heavy metal pretreatment tank 20; removing most heavy metals in the lithium manganate wastewater, and carrying out precipitation separation;
secondly, the method comprises the following steps: first-stage lime pretreatment: after the heavy metals are removed, the lithium manganate wastewater overflows into a first-stage lime pretreatment tank 30 through an overflow pipe on the side wall of the heavy metal pretreatment tank 20; meanwhile, gypsum slurry precipitated at the bottom of the secondary lime pretreatment tank 50 enters the primary lime pretreatment tank 30 through a slurry pump (not shown in the figure) through a slurry pipe 51, the lithium manganate wastewater is subjected to primary treatment, and the pH value in the primary lime pretreatment tank 30 is adjusted to 7-8; heavy metals are prevented from forming precipitate and separating out, and the gypsum slag is not easy to emit ammonia odor;
thirdly, the method comprises the following steps: and (3) centrifugal treatment: the slag slurry wastewater in the first-stage lime pretreatment tank 30 enters a centrifugal device 40 through a slag slurry pump for separation treatment, so that gypsum slag is separated from the wastewater, and a centrifugate is discharged from the side part of the centrifugal device 40 and enters a second-stage lime pretreatment tank 50; washing the centrifuged gypsum with raw water, deaminated effluent and dilute acid in sequence in a centrifugal device 40 to ensure that the water content of the centrifuged gypsum is less than 20 percent, reduce the amount of slag and ensure that the centrifuged gypsum does not have ammonia smell and heavy metals;
fourthly: secondary lime pretreatment: adding the lime slurry into a secondary lime pretreatment tank 50 by a chemical adding system 20, stirring, and adjusting the pH value to 11-11.5; meanwhile, gypsum slurry is precipitated at the bottom of the secondary lime pretreatment tank 50, and enters the primary lime pretreatment tank 30 through a thick slurry pump through a thick slurry pipe 51, and supernatant enters a buffer tank 60;
fifth, the method comprises the following steps: intermediate buffering: the clear liquid is buffered, homogenized and equalized in the buffer pool 60, and is precipitated for the second time, and then the supernatant liquid enters the analysis device 70;
sixth: resolving and removing calcium: the chemical adding device 10 adds an analytic solution (the analytic solution is an ammonium bicarbonate solution) into the analytic device 70, carbonate ions in the ammonium bicarbonate solution react with calcium ions to generate calcium carbonate precipitate, the calcium ions are removed, ammonium ions are converted into ammonia monohydrate, and concentrated ammonia water is recovered during negative pressure ammonia evaporation treatment;
seventh: and (3) settling: discharging the reaction liquid (the concentration of calcium ions in the reaction liquid is less than or equal to 25 mg/L) in the analysis device 70 into a clarification tank 80, precipitating, and performing negative pressure ammonia distillation on the clear liquid;
eighth: and (3) negative pressure ammonia distillation: clear liquid in the clarification tank 80 enters a preheater 91 through a lift pump, enters a negative pressure ammonia distillation tower 92 from the upper part after being preheated (the operating pressure of the negative pressure ammonia distillation tower is-0.07 to-0.08 MPa, the operating temperature is 60 to 80 ℃), moves in a cross flow manner with saturated steam entering from the bottom of the tower from top to bottom, forms high-temperature clear water (the content of ammonia nitrogen in the high-temperature clear water is less than 15 mg/L) at the bottom of the tower after mass transfer and heat transfer, and forms ammonia-containing steam at the top of the tower; high-temperature clean water enters the preheater 91 from the tower bottom through a water outlet pump, exchanges heat with clear liquid in the clarification tank 80, is discharged from the upper part of the preheater 91, and enters a water outlet tank; the ammonia-containing steam enters a condenser 93 through a pipeline for condensation, the condensate enters a gas-liquid separation tank 94 to form dilute ammonia water, and the dilute ammonia water enters a negative pressure ammonia still 92 through a reflux pump through a pipeline for further concentration of ammonia concentration in the ammonia-containing steam; the uncondensed ammonia enters an ammonia recovery device 95 and is circularly absorbed in the ammonia recovery device to obtain high-concentration ammonia water (the concentration of the recovered ammonia water is more than or equal to 20%);
ninth: filter pressing separation: the calcium carbonate precipitate in the clarification tank 80 and the metal precipitate in the effluent pool are subjected to pressure filtration by a filter press (not shown in the figure), the filter residue is discharged outside, and the clear liquid respectively flows back to the clarification tank 80 and the effluent pool (not shown in the figure).
The described embodiments are only some, but not all embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Claims (6)
1. The utility model provides a lithium manganate effluent disposal system which characterized in that: comprises a dosing system (10), and a heavy metal pretreatment tank (20), a primary lime pretreatment tank (30), a centrifugal device (40), a secondary lime pretreatment tank (50), a resolving device (70), a clarification tank (80) and a negative pressure ammonia distillation system (90) which are connected in sequence; the heavy metal pretreatment tank (20), the secondary lime pretreatment tank (50) and the analysis device (70) are all connected with the dosing system (10); the bottom of the second-stage lime pretreatment tank (50) is provided with a concentrated slurry pipe (51), and the other end of the concentrated slurry pipe (51) is communicated with the first-stage lime pretreatment tank (30).
2. The lithium manganate wastewater treatment system of claim 1, wherein: the negative pressure ammonia distillation system (90) comprises a preheater (91), a negative pressure ammonia distillation tower (92), a condenser (93), a gas-liquid separation tank (94) and an ammonia recovery device (95) which are connected in sequence; the supernatant in the clarification tank (80) is connected with a liquid inlet at the lower part of the preheater (91) through a pipeline, and a liquid outlet at the top of the preheater (91) is connected with an inlet at the upper part of the negative pressure ammonia distillation tower (92); the lower part of the negative pressure ammonia still (92) is provided with a steam inlet (92.1) and a high-temperature clear water outlet (92.2), the high-temperature clear water outlet (92.2) is connected with a heat source inlet at the lower part of the preheater (91), and a water outlet at the upper part of the preheater (91) is connected with a water outlet pool; an ammonia-containing steam outlet at the top of the negative pressure ammonia still (92) is connected with a condenser (93), a condensate outlet of the condenser (93) is connected with the top of a gas-liquid separation tank (94), a dilute ammonia water outlet at the bottom of the gas-liquid separation tank (94) is connected with an inlet at the upper part of the negative pressure ammonia still (92), and an uncondensed ammonia gas outlet at the side wall of the gas-liquid separation tank (94) is connected with an ammonia recovery device (95).
3. The lithium manganate wastewater treatment system of claim 1, wherein: a buffer pool (60) is also arranged between the secondary lime pretreatment tank (50) and the analysis device (70).
4. The lithium manganate wastewater treatment system of claim 1, wherein: the centrifuge device (40) is a gypsum centrifuge.
5. The lithium manganate wastewater treatment system of claim 1, wherein: the PH value in the first-stage lime pretreatment tank (30) is adjusted to 7-8.
6. The lithium manganate wastewater treatment system of claim 1, wherein: the PH value in the secondary lime pretreatment tank (50) is adjusted to 11-11.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022604585.1U CN213708033U (en) | 2020-11-12 | 2020-11-12 | Lithium manganate effluent disposal system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022604585.1U CN213708033U (en) | 2020-11-12 | 2020-11-12 | Lithium manganate effluent disposal system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213708033U true CN213708033U (en) | 2021-07-16 |
Family
ID=76804831
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022604585.1U Active CN213708033U (en) | 2020-11-12 | 2020-11-12 | Lithium manganate effluent disposal system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213708033U (en) |
-
2020
- 2020-11-12 CN CN202022604585.1U patent/CN213708033U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109455885B (en) | Nitrogen resource heat extraction and recovery method | |
| CN106882884B (en) | A kind of method of chloride ion in recycling waste water | |
| CN111018221B (en) | Method for recycling smelting waste acid wastewater | |
| CN105110587A (en) | Sludge pretreatment technology with desalting effect | |
| CN106746102B (en) | Treatment process of fluorine-containing ammonia nitrogen wastewater | |
| WO2023036053A1 (en) | Cooperative treatment method and treatment system for high-salt solid waste ash and acidic wastewater of steel plant | |
| CN110981065A (en) | Treatment method of lithium battery industrial wastewater | |
| CN109455884A (en) | A kind of nitrogen resource thermal extraction recovery system | |
| CN112573704A (en) | System and method for treating strong brine by using micro-channel reactor | |
| CN202038939U (en) | Fluorine-contained wastewater treatment system | |
| CN111606487A (en) | Method for continuously treating and recycling manganese and ammonia nitrogen resources from electrolytic manganese wastewater | |
| CN113292187A (en) | Resourceful treatment method and device for high-concentration ammonia nitrogen wastewater | |
| CN105174532B (en) | One kind is used for good antiscale property pretreatment system and its processing method before industrial waste water with high ammoniac nitrogen ammonia still process | |
| CN111547922A (en) | Treatment method of manganese-containing ammonia nitrogen wastewater | |
| CN112125436A (en) | Wastewater treatment method for recovering copper and nickel from electroplating comprehensive wastewater | |
| CN101629249A (en) | Comprehensive treatment method of three wastes in extracting vanadium from stone coal navajoite | |
| CN213708033U (en) | Lithium manganate effluent disposal system | |
| CN109576494B (en) | Method for preparing sodium sulfate by utilizing metal surface treatment waste | |
| CN101503257B (en) | Method and apparatus for recovering and treating ammonium nitrate condensate liquid wastewater | |
| JP2020018951A (en) | Method for recovering phosphate from steel slag | |
| CN204897624U (en) | Sulphur ammonium waste water comprehensive control retrieval and utilization device is smelted to tombarthite | |
| CN109371243B (en) | Method for recycling waste acid of zinc smelting plant | |
| CN113735363A (en) | Treatment method of chrome tanning waste liquid | |
| CN109650646B (en) | Treatment method of glycine production wastewater | |
| CN114605017A (en) | Treatment process of ammonia nitrogen wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |