CN210885335U - Waste battery waste acid recovery production line - Google Patents

Abstract

The utility model discloses a spent battery waste acid recovery production line, main reation kettle, freezing agitator tank, stiff ware, distillation concentrator, neutralization jar, the spray drying tower including connecting gradually, the clear solution export of stiff ware links up with the inlet of distillation concentrator, be provided with the PH detector in the neutralization jar, neutralization jar passes through the diaphragm pump with the material pump to the spray drying tower, the steam pipe connection liquid storage pot of distillation concentrator jar, the inlet of neutralization jar is connected to the liquid outlet of liquid storage pot, and the liquid outlet of liquid storage pot is equipped with the valve, is equipped with the agitator in the neutralization jar, and neutralization jar upper portion is equipped with the dog-house. The recovery equipment and the process solve the problem of treatment of waste acid of the waste lead storage battery, utilize the technical means of regeneration circulation and use the harmless replacement process to synthesize and produce valuable chemical raw materials, realize zero-pollution treatment of the waste acid, and are economical and environment-friendly.

Description

Waste battery waste acid recovery production line

Technical Field

The utility model belongs to the technical field of chemical industry equipment, especially, relate to a waste battery waste acid recovery production line.

Background

At present, the treatment of waste acid from waste lead-acid storage batteries is a great economic problem, and the waste acid is usually subjected to electrolytic purification, concentration purification, simple acid-base neutralization and the like in the past to meet the discharge standard, so that resources are wasted, a large amount of manpower and material resources are wasted, the waste acid still belongs to consumable treatment, and if the waste acid can be changed into valuables, the waste acid is formed into a product with economic value through a series of processes, so that the situation of high cost and waste of data of the traditional recovery and disposal process can be changed.

Disclosure of Invention

In view of the not enough of above-mentioned prior art, the utility model aims at providing a waste battery waste acid recovery production line can accomplish zero pollution of spent acid, and the economic recovery of accessory substance.

For solving the above technical problem, the utility model discloses the technical scheme who adopts is:

the utility model relates to a waste battery waste acid recovery production line, main reation kettle, freezing agitator tank, stiff ware, distillation concentrator, neutralization tank, the spray drying tower including connecting gradually, the clear solution export of stiff ware links up with the inlet of distillation concentrator, be provided with the PH detector in the neutralization tank, the neutralization tank passes through the diaphragm pump with the material pump send to the spray drying tower.

The utility model discloses a steam pipe connection liquid storage pot of distillation concentrator, the inlet of neutralization jar is connected to the liquid outlet of liquid storage pot, and the liquid outlet of liquid storage pot is equipped with the valve.

The utility model discloses a be equipped with the agitator in the neutralization tank, neutralization tank upper portion is equipped with the dog-house.

The utility model discloses a waste battery waste acid recovery production technology, concrete process steps are:

① after long-term use, the residual acid amount and acidity are different, the waste acid is collected uniformly and is filtered to remove impurities;

② adding soda and sodium chloride into a reaction kettle in an order of first soda and then acid for reaction, then putting the mixed solution into a freezing and stirring tank, after uniformly mixing, cooling the mixture to 5 ℃ in the freezing and stirring tank, then putting the mixed solution into a thickener, and separating clear liquid and precipitated sodium sulfate crystals;

③ distilling the separated clear liquid to obtain dilute hydrochloric acid by using the waste heat of the lead smelting furnace, and conveying to a liquid storage tank for storage;

④ adding quicklime powder into a neutralization tank, adding distilled dilute hydrochloric acid until the pH value of the mixed slurry is 6-8 to obtain slurry containing calcium chloride, conveying the slurry containing calcium chloride to a spray drying tower through a diaphragm pump, and drying by using waste heat generated by lead smelting as a heat source to obtain solid powder of calcium chloride.

Implement the utility model provides a difficult problem of processing of waste lead accumulator spent acid, utilize regeneration cycle's technical means, can utilize waste sulfuric acid is whole among the waste lead accumulator, changed traditional recovery processing technology's high cost, the resource wasting situation, with innoxious replacement technology, valuable industrial chemicals is produced in the synthesis, and spent acid recovery 100%, more economic environmental protection.

Description of the drawings:

fig. 1 is a schematic structural view relating to the present invention;

fig. 2 is a schematic structural view of the medium thickener according to the present invention.

The specific implementation mode is as follows:

the present invention will be further described with reference to the accompanying drawings.

Referring to fig. 1, a waste battery waste acid recovery production line mainly comprises a reaction kettle 1, a freezing stirring tank 2, a thickener 3, a distillation concentrator 4, a neutralization tank 5 and a spray drying tower 6 which are connected in sequence, and the specific process steps are as follows:

① after long-term use, the residual acid amount and acidity are different, the waste acid is collected uniformly and is filtered to remove impurities;

② adding sodium carbonate and sodium chloride into the reaction kettle 1 in an order of first alkali and then acid to react to form a mixed solution of sodium sulfate and hydrochloric acid, then feeding the mixed solution into the freezing and stirring tank 2, cooling the mixture to 5 ℃ in the freezing and stirring tank 2 after uniform mixing, feeding the mixed solution into the thickener 3, and separating clear liquid and separated sodium sulfate crystals;

③ distilling the separated clear liquid in a distillation concentrator 4 to obtain dilute hydrochloric acid by using the waste heat of the lead smelting furnace, and conveying to a liquid storage tank for storage;

④ quicklime powder is put into a neutralization tank 5, then distilled dilute hydrochloric acid is added until the pH value of the mixed slurry reaches 6-8 to obtain slurry containing calcium chloride, the slurry containing calcium chloride is conveyed to a spray drying tower 6 through a diaphragm pump 56, and waste heat generated by lead smelting is used as a heat source for drying to obtain solid powder of calcium chloride.

Wherein, the clear liquid export of stiff ware 3 links up with the inlet of distillation concentrator 4 for clear liquid material shifts, is provided with PH detector 51 in neutralization tank 5 for the PH value of calcium chloride thick liquids among the real-time detection reaction process, and neutralization tank 5 is pumped the material to spray drying tower 6 through diaphragm pump 56.

The steam conduit of the distillation concentrator 4 is connected with a liquid storage tank 45, the liquid storage tank 45 is used as a transfer station, the liquid outlet of the liquid storage tank 45 is connected with the liquid inlet of the neutralization tank 5, and the liquid outlet of the liquid storage tank 45 is provided with a valve for storing and releasing the distilled dilute sulfuric acid.

The neutralizing tank 5 is provided with a stirrer 50, and the upper part of the neutralizing tank 5 is provided with a feeding port 52 for feeding quicklime powder.

As shown in fig. 2, the thickener 3 mainly has a cylinder 7 with a conical lower portion, a stirrer 71 is arranged in the cylinder 7, a guide cylinder 72 is arranged in the cylinder 7, the guide cylinder 72 is connected with a feed pipe 721, materials enter the guide cylinder 72 from the feed pipe 721 and slowly rise in the guide cylinder 72, a first steam pipe 781 is connected to the lower portion of the guide cylinder 72 and used for leading in steam to grow crystals, overflow notches 73 are arranged on two sides of an opening above the guide cylinder 72, overflow weirs 8 are arranged above the guide cylinder 2, large and small crystals overflow from the overflow notches 73, and small crystals enter the overflow weirs 8 along with crystal slurry. The first steam pipe 781 is externally connected with an air pump and a steam generator, and the air inflow can be adjusted through an air inlet valve, so that the flow velocity of the fluidizing agent in the guide cylinder is adjusted, and the large crystals are screened in a grading manner.

Rails 9 are arranged on two sides of the guide cylinder 72, a sinking and floating groove body 96 which is horizontally arranged ascends and descends along the path of the rails 9, a floating ball 961 is assembled below the sinking and floating groove body 96, and the rails 9 are positioned right below the overflow notch 73. The inner wall of the barrel body 7 is provided with a convex strip which is symmetrical to the rail 9, one end of the sinking and floating groove body 96 is connected with the rail 9, the other end of the sinking and floating groove body 96 is connected with the convex strip, the lowest ends of the rail 9 and the convex strip are provided with a limiting plate, under an initial state, crystal pulp is not arranged in the barrel body 7, therefore, the sinking and floating groove body 96 is at a lower limit position, materials can fall into the sinking and floating groove body 96 after flowing out of an overflow notch 73 of the guide cylinder 72, and are buffered by the sinking and floating groove body 96, and then overflow into the bottom of the barrel body 7, so that the crystal pulp in the barrel body 7 slowly accumulates and rises, under the action of the floating ball 961, the sinking and floating groove body 96 is promoted to rise, even if the sinking and floating groove body 96 rises to the.

The floating tank 96 has two groups corresponding to the two overflow gaps 73, i.e. the guide cylinder 72 is used as a central point, one group of floating tank 96 is equivalent to a radius area crossing the cylinder 7, and the floating tank 96 corresponding to the overflow gaps 73 can effectively receive crystal slurry to form secondary buffering.

The outer wall of the cylinder 7 is provided with a gas-liquid separator 74, the overflow weir 8 is connected with the gas-liquid separator 74, when the liquid level rises to the limit position, the limit of the liquid level is positioned at the overflow weir 8, small crystals enter the overflow weir 8 and then are discharged into the gas-liquid separator 74, a liquid discharge port is arranged below the gas-liquid separator 74, and a gas discharge port is arranged above the gas-liquid separator 74.

A discharge port 711 is formed in one side of the lower portion of the cylinder 7, the discharge port 711 is connected with the steam concentrator 4, the discharge port 711 is connected with a second steam pipe 782, steam can be introduced, large crystals are prevented from being blocked at the discharge port 711, and discharging is smooth.

The bottom of the cylinder 7 is provided with a backflushing opening 712 which is convenient for backflushing cleaning.

The stirrer 71 is driven by the motor 710, the motor 710 is located above the cylinder 7, the rotating shaft of the stirrer 71 penetrates through the guide cylinder 72, the rotating shaft of the stirrer 71 is connected with the guide cylinder 72 through a bearing, and the stirrer 71 is used for stirring large crystals deposited at the bottom of the cylinder 7, so that the difficulty in discharging the crystals due to the fact that the crystals are accumulated in a large quantity is avoided.

It is to be understood that the technical scope of the present invention is not limited to the content of the specification, and that modifications or changes may be made by those skilled in the art based on the above description, and all such modifications and changes are intended to fall within the scope of the appended claims.

Claims (3)

1. The utility model provides a waste battery waste acid recovery production line which characterized in that: mainly including reation kettle (1), freezing agitator tank (2), stiff ware (3), distillation concentrator (4), neutralization tank (5), the spray drying tower (6) that connect gradually, the clear liquid export of stiff ware (3) links up with the inlet of distillation concentrator (4), be provided with PH detector (51) in neutralization tank (5), neutralization tank (5) are pumped the material to spray drying tower (6) through diaphragm pump (56).

2. The waste battery acid recycling production line of claim 1, characterized in that: the steam guide pipe of the distillation concentrator (4) is connected with the liquid storage tank (45), the liquid outlet of the liquid storage tank (45) is connected with the liquid inlet of the neutralization tank (5), and the liquid outlet of the liquid storage tank (45) is provided with a valve.

3. The waste battery acid recycling production line as claimed in claim 1 or 2, characterized in that: a stirrer (50) is arranged in the neutralization tank (5), and a feeding port (52) is arranged at the upper part of the neutralization tank (5).

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