CN114504933A - System and method for treating waste gas in lithium hexafluorophosphate preparation process - Google Patents
System and method for treating waste gas in lithium hexafluorophosphate preparation process Download PDFInfo
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Abstract
The invention belongs to the field of waste gas treatment, and particularly relates to a system and a method for treating waste gas in a lithium hexafluorophosphate preparation process. The system for treating waste gas in the preparation process of lithium hexafluorophosphate has the following structure: the waste gas discharge pipeline is connected with the first heat exchanger; the first heat exchanger, the first stage hydrogen fluoride scrubbing tower, the second heat exchanger, the first stage hydrogen chloride scrubbing tower, the second stage hydrogen chloride scrubbing tower passes through the gas pipeline and connects in series in proper order. The waste gas is respectively subjected to heat exchange by the first heat exchanger and then absorbed by washing towers at all stages so as to achieve the purpose of treating hydrogen fluoride and hydrogen chloride gas. The invention has the beneficial effects that: the mixed acid amount generated in the lithium hexafluorophosphate production process is reduced, the concentration of hydrofluoric acid in the mixed acid is improved, the mixed acid is more beneficial to preparing byproducts, meanwhile, concentrated hydrochloric acid with higher purity can be collected, and the additional value of the hydrochloric acid is further improved.
Description
Technical Field
The invention belongs to the field of waste gas treatment, and particularly relates to a system and a method for treating waste gas in a lithium hexafluorophosphate preparation process.
Background
With the continuous breaking of expectations of the production and marketing acceleration of electric vehicles, the demand of upstream lithium ion batteries is greatly increased, and the capacity of lithium hexafluorophosphate products is rapidly released. However, a large amount of mixed waste gas of hydrogen chloride and hydrogen fluoride is generated in the process of producing lithium hexafluorophosphate, and the treatment method adopted at present is to convey the waste gas to a waste gas washing tower to be washed and absorbed by water so as to prepare mixed acid containing hydrogen chloride and hydrogen fluoride. The efficiency of the mixed waste gas absorption process in the existing lithium hexafluorophosphate production process is low, a large amount of water resources are wasted, the amount of generated mixed acid is large, the consumption is difficult, and the adverse effects on the production cost and the environment are caused.
CN215693069U a hydrofluoric acid production tail gas processing apparatus, the tubulation condenser air inlet is connected the tail gas pipeline, its gas outlet is connected to the jar of keeping in, the jar of keeping in is connected to the sprayer air inlet, jar of keeping in flowing back is connected to hydrofluoric acid recovery jar, the sprayer jet orifice is connected to graphite falling film absorber entry, graphite falling film absorber exit end is connected to the densification jar, the densification jar flowing back is connected to the sprayer inlet through jet pump and injection valve, the densification jar is connected to the scrubbing tower, the densification jar leakage fluid dram is connected to hydrofluoric acid recovery jar, the scrubbing tower gas outlet is connected to the caustic wash tower, the rigid coupling has the gas lift pipe above the caustic wash tower gas outlet, it discharges into the atmosphere to purify tail gas through the gas lift pipe, circulation caustic wash tank passes through liquid feed pump and return pump and supplies spray alkali lye for caustic wash tower and gas lift pipe circulation. This tail gas processing apparatus can improve tail gas absorption effect and purifying effect, reduces environmental pollution, retrieves remaining hydrofluoric acid, and it is extravagant to reduce the cost. However, if the method is used for producing lithium hexafluorophosphate, a large amount of mixed acid is generated, which is not beneficial to the production of byproducts.
In view of the above problems, it is necessary to provide a method having a low mixed acid content and a high absorption efficiency.
Disclosure of Invention
In order to solve the technical problems, the invention provides a system for treating waste gas in a lithium hexafluorophosphate preparation process and a method for treating waste gas in the lithium hexafluorophosphate preparation process, which is matched with the system.
The system for the waste gas in the preparation process of lithium hexafluorophosphate provided by the invention has the following structure:
the waste gas discharge pipeline is connected with the first heat exchanger;
the first heat exchanger is connected with the first-stage hydrogen fluoride washing tower, the second heat exchanger, the first-stage hydrogen chloride washing tower and the second-stage hydrogen chloride washing tower in series in sequence through gas pipelines.
The lower part of the first-stage hydrogen fluoride washing tower is sequentially connected with the first heat exchanger and the first liquid storage tank in series through an acid liquor pipeline;
the upper end of the third heat exchanger is connected with the upper end of the first-stage hydrogen fluoride washing tower through a first liquid pipeline;
the pipeline at the lower end of the third heat exchanger is divided into a first branch pipeline and a second branch pipeline, and the first branch pipeline and the second branch pipeline are respectively connected with the upper end and the lower end of the first liquid storage tank; the second branch pipeline is connected with a mixed acid discharge pipe;
an air pressure balance pipeline is arranged between the upper part of the first liquid storage tank and the lower part of the first-stage hydrogen fluoride washing tower.
The lower part of the second-stage hydrogen fluoride washing tower is connected with the second liquid storage tank through an acid liquor pipeline;
the upper end of the fourth heat exchanger is connected with the upper end of the second-stage hydrogen fluoride washing tower through a second liquid pipeline;
the pipeline at the lower end of the fourth heat exchanger is divided into a third branch pipeline and a fourth branch pipeline, and the third branch pipeline and the fourth branch pipeline are respectively connected with the upper end and the lower end of the second liquid storage tank; a pipeline for connecting the second liquid storage tank with the first liquid storage tank is arranged on the fourth branch pipeline;
the upper part of the second liquid storage tank is also provided with a hydrochloric acid pipeline, and an air pressure balance pipeline is arranged between the upper part of the second liquid storage tank and the lower part of the second-stage hydrogen fluoride washing tower.
The lower part of the first-stage hydrogen chloride washing tower is sequentially connected with the second heat exchanger and the third liquid storage tank in series through an acid liquor pipeline;
the upper end of the fifth heat exchanger is connected with the upper end of the first-stage hydrogen chloride washing tower through a third liquid pipeline;
the pipeline at the lower end of the fifth heat exchanger is divided into a fifth branch pipeline and a sixth branch pipeline, and the fifth branch pipeline and the sixth branch pipeline are respectively connected with the upper end and the lower end of the third liquid storage tank;
a hydrochloric acid discharge pipe is arranged on the fifth branch pipeline, and an air pressure balance pipeline is arranged between the upper part of the third liquid storage tank and the lower part of the third-stage hydrogen fluoride washing tower.
The lower part of the second-stage hydrogen chloride washing tower is connected with the fourth liquid storage tank through an acid liquor pipeline;
a fourth liquid pipeline at the upper part of the second-stage hydrogen chloride washing tower is divided into a seventh branch pipeline and an eighth branch pipeline which are respectively connected with the upper end and the lower end of a fourth liquid storage tank; a pipeline for connecting the fourth liquid storage tank with the third liquid storage tank is arranged on the eighth branch pipeline;
the upper part of the fourth liquid storage tank and the lower part of the second-stage hydrogen chloride washing tower are provided with air pressure balance pipelines;
a gas pipeline connected with the upper part of the second-stage hydrogen chloride washing tower is divided into two branch pipelines, one branch is connected with the third liquid storage tank, and the other branch pipeline is communicated with the first-stage alkaline washing tower; the first-stage alkaline washing tower is connected with the second-stage alkaline washing tower in series;
the upper part of the fourth liquid storage tank is provided with a water inlet pipeline.
And the second branch pipeline, the fourth branch pipeline, the sixth branch pipeline and the eighth branch pipeline are respectively provided with a pump for lifting acid liquor. The pumps described above are conventional devices and will not be described in greater detail herein.
All be provided with the valve on the pipeline among the above-mentioned system, ordinary check valve can, set up as the multi-ported valve in many pipe joints.
The lower parts of the first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger and the fifth heat exchanger are all provided with water inlet pipelines, the upper parts of the first heat exchanger, the second heat exchanger, the third heat exchanger, the fourth heat exchanger and the fifth heat exchanger are provided with water outlet pipelines, and valves are arranged on the water inlet pipelines and the water outlet pipelines respectively so as to facilitate heat exchange.
The method for treating the waste gas in the preparation process of the lithium hexafluorophosphate comprises the following steps:
after the lithium hexafluorophosphate waste gas enters a first heat exchanger through a waste gas discharge pipeline for heat exchange treatment, the lithium hexafluorophosphate waste gas is absorbed by concentrated hydrochloric acid in a first-stage hydrogen fluoride washing tower, and the residual gas after absorption enters a second-stage hydrogen fluoride washing tower and is absorbed by the concentrated hydrochloric acid again; and the rest gas containing hydrogen chloride enters a second heat exchanger for heat exchange, then enters a first-stage hydrogen chloride washing tower to be absorbed by water, and the unabsorbed gas enters a second-stage hydrogen chloride washing tower to be continuously absorbed by the water.
More specifically, the method for treating waste gas generated in the process of preparing lithium hexafluorophosphate comprises the following steps:
s1: introducing lithium hexafluorophosphate waste gas into a first heat exchanger through a waste gas discharge pipeline, carrying out heat exchange treatment, conveying the lithium hexafluorophosphate waste gas into a first-stage hydrogen fluoride washing tower, and absorbing the lithium hexafluorophosphate waste gas by using an absorption liquid, wherein the absorption liquid is 25-31% concentrated hydrochloric acid, most of hydrogen fluoride in the lithium hexafluorophosphate waste gas is absorbed by the concentrated hydrochloric acid, and the absorption liquid is converted into a mixed acid of hydrofluoric acid and hydrochloric acid with the concentration of 30%;
discharging the mixed acid through a mixed acid discharge pipe; or the waste gas enters a first-stage hydrogen fluoride washing tower for recycling after heat exchange through a first heat exchanger; or the waste heat enters the first heat exchanger for heat exchange and then flows back to the first liquid storage tank through the first branch pipeline;
s2: the gas absorbed by the first-stage hydrogen fluoride washing tower enters a second-stage hydrogen fluoride washing tower through a gas pipeline at the upper part of the first-stage hydrogen fluoride washing tower and is continuously absorbed by concentrated hydrochloric acid with the concentration of 25-31%;
the mixed acid obtained after the hydrogen fluoride is absorbed by the second-stage hydrogen fluoride washing tower enters a second liquid storage tank, and the mixed acid enters the first liquid storage tank or is discharged or recycled; or the mixed acid enters a second-stage hydrogen fluoride washing tower to continuously absorb the waste gas hydrogen fluoride after heat exchange in a fourth heat exchanger or flows back to a second liquid storage tank;
s3: the gas absorbed by the second-stage hydrogen fluoride washing tower enters a second heat exchanger for heat exchange, and then enters the first-stage hydrogen chloride washing tower to be absorbed by water;
the absorption liquid in the first-stage hydrogen chloride washing tower absorbs hydrogen chloride and is converted into concentrated hydrochloric acid, the concentrated hydrochloric acid enters a third liquid storage tank after being subjected to heat exchange through a second heat exchanger, or is collected through a hydrochloric acid discharge pipe or enters the first-stage hydrogen chloride washing tower after being subjected to heat exchange through a fifth heat exchanger for recycling, or flows back to the third liquid storage tank after being subjected to heat exchange through the fifth heat exchanger;
s4: the gas absorbed by the first-stage hydrogen chloride washing tower enters a second-stage hydrogen chloride washing tower to be continuously absorbed, and concentrated hydrochloric acid in the first-stage hydrogen chloride washing tower enters a fourth liquid storage tank, or is conveyed to a third liquid storage tank to be recycled, or enters the second-stage hydrogen chloride washing tower to be recycled;
s5: and the gas remained in the third liquid storage tank is conveyed to the first-stage alkaline tower and the second-stage alkaline tower through a gas pipeline at the upper part of the second-stage hydrogen chloride washing tower to be continuously absorbed.
Of course, in the absorption process, the mixed acid in the first liquid storage tank can also enter the second liquid storage tank for use; the low-concentration hydrochloric acid solution in the third liquid storage tank can also enter the fourth liquid storage tank for recycling.
The principle of the invention is as follows:
1. two-stage hydrogen fluoride washing towers and two-stage hydrogen chloride washing towers are connected in series, so that the tail gas can be fully absorbed.
2. The two-stage hydrogen fluoride washing tower adopts 25% -31% of concentrated hydrochloric acid as absorption liquid, only absorbs hydrogen fluoride to form mixed acid of hydrofluoric acid and hydrochloric acid with the concentration of 30% when mixed waste gas in the lithium hexafluorophosphate production process is washed, and adopts water to absorb hydrogen chloride, and collects 25% -31% of concentrated hydrochloric acid.
3. The heat generated by the heat exchanger for absorbing acid is added to the two-stage hydrogen fluoride washing tower, so that the temperature of the solution is raised to 60-70 ℃, and after the heat exchanger is added, the temperature of the solution is lowered to 40-50 ℃, thereby being beneficial to improving the absorption efficiency of the absorption liquid.
Compared with the whole mixed acid obtained by the prior art, the method has the advantages that the mixed acid amount is reduced, and a part of concentrated hydrochloric acid can be recycled.
The invention has the advantages that:
(1) the first-stage hydrogen fluoride washing tower, the second-stage hydrogen fluoride washing tower and the first-stage hydrogen chloride washing tower are arranged and connected in series, and concentrated hydrochloric acid obtained by using water as absorption liquid in the hydrogen chloride washing tower can be used as absorption liquid for the hydrogen fluoride washing tower, so that the cyclic utilization of the hydrochloric acid is realized, and resources are saved;
(2) the heat exchangers are arranged on the pipelines, so that the absorption temperature is kept at the optimal temperature, and the absorption efficiency is improved;
(3) the mixed acid amount generated in the lithium hexafluorophosphate production process is reduced, the concentration of hydrofluoric acid in the mixed acid is improved, the mixed acid is more beneficial to preparing byproducts, meanwhile, concentrated hydrochloric acid with higher purity can be collected, and the additional value of the hydrochloric acid is further improved.
Drawings
FIG. 1 is a system configuration diagram of embodiment 1;
FIG. 2 is a system configuration diagram according to embodiment 3.
In the figure: 1-a first heat exchanger, 2-a first hydrogen fluoride washing tower, 3-a second hydrogen fluoride washing tower, 4-a second heat exchanger, 5-a first hydrogen chloride washing tower, 6-a second hydrogen chloride washing tower, 7-a first liquid pipeline, 8-a second liquid pipeline, 9-a third liquid pipeline, 10-a fourth liquid pipeline, 11-a third heat exchanger, 12-a fourth heat exchanger, 13-a fifth heat exchanger, 14-a first liquid storage tank, 15-a second liquid storage tank, 16-a third liquid storage tank, 17-a fourth liquid storage tank, 18-a mixed acid discharge pipe, 19-a hydrochloric acid discharge pipe, 20-a hydrochloric acid pipeline, 21-a water inlet pipeline, 301-a first branch pipeline, 302-a second branch pipeline, 303-a third branch pipeline, 304-a fourth branch pipeline, 305-a fifth branch pipeline, 306-a sixth branch pipeline, 307-a seventh branch pipeline, 308-an eighth branch pipeline, 22-a first-stage alkaline washing tower and 23-a second-stage alkaline washing tower.
Detailed Description
The present invention will now be further described with reference to specific embodiments in order to enable those skilled in the art to better understand the present invention.
Example 1
The system for the waste gas in the preparation process of lithium hexafluorophosphate provided by the invention has the following structure:
the exhaust gas discharge pipeline is connected with the first heat exchanger 1;
the first heat exchanger 1 is connected with a first-stage hydrogen fluoride washing tower 2, a second-stage hydrogen fluoride washing tower 3, a second heat exchanger 4, a first-stage hydrogen chloride washing tower 5 and a second-stage hydrogen chloride washing tower 6 in series in sequence through gas pipelines.
The lower part of the first-stage hydrogen fluoride washing tower 2 is connected with the first heat exchanger 1 and the first liquid storage tank 14 in series in sequence through acid liquor pipelines;
the upper end of the third heat exchanger 11 is connected with the upper end of the first-stage hydrogen fluoride washing tower 2 through a first liquid pipeline 7;
the pipeline at the lower end of the third heat exchanger 11 is divided into a first branch pipeline 301 and a second branch pipeline 302, and the first branch pipeline 301 and the second branch pipeline 302 are respectively connected with the upper end and the lower end of the first liquid storage tank 14; the second branch pipeline 302 is connected with a mixed acid discharge pipe 18;
an air pressure balancing pipeline is arranged between the upper part of the first liquid storage tank 14 and the lower part of the first-stage hydrogen fluoride washing tower 2.
The lower part of the second-stage hydrogen fluoride washing tower 3 is connected with the second liquid storage tank 15 through an acid liquor pipeline;
the upper end of the fourth heat exchanger 12 is connected with the upper end of the second-stage hydrogen fluoride washing tower 3 through a second liquid pipeline 8;
the pipeline at the lower end of the fourth heat exchanger 12 is divided into a third branch pipeline 303 and a fourth branch pipeline 304, and the third branch pipeline 303 and the fourth branch pipeline 304 are respectively connected with the upper end and the lower end of the second liquid storage tank 15; the fourth branch pipe 304 is provided with a pipe for connecting the second liquid storage tank 15 with the first liquid storage tank 14;
the upper part of the second liquid storage tank 15 is also provided with a hydrochloric acid pipeline 20, and an air pressure balance pipeline is arranged between the upper part of the second liquid storage tank 15 and the lower part of the second-stage hydrogen fluoride washing tower 3.
The lower part of the first-stage hydrogen chloride washing tower 5 is connected with the second heat exchanger 4 and the third liquid storage tank 16 in series in sequence through acid liquor pipelines;
the upper end of the fifth heat exchanger 13 is connected with the upper end of the first-stage hydrogen chloride washing tower 5 through a third liquid pipeline 9;
the pipeline at the lower end of the fifth heat exchanger 13 is divided into a fifth branch pipeline 305 and a sixth branch pipeline 306, and the fifth branch pipeline 305 and the sixth branch pipeline 306 are respectively connected with the upper end and the lower end of the third liquid storage tank 16;
a hydrochloric acid discharge pipe 19 is arranged on the fifth branch pipeline 305, and an air pressure balance pipeline is arranged between the upper part of the third liquid storage tank 16 and the lower part of the third-stage hydrogen fluoride washing tower.
The lower part of the second-stage hydrogen chloride washing tower 6 is connected with the fourth liquid storage tank 17 through an acid liquor pipeline;
the fourth liquid pipeline 10 at the upper part of the second-stage hydrogen chloride washing tower 6 is divided into a seventh branch pipeline 307 and an eighth branch pipeline 308 which are respectively connected with the upper end and the lower end of the fourth liquid storage tank 17; the eighth branch pipeline 308 is provided with a pipeline for connecting the fourth liquid storage tank 17 with the third liquid storage tank 16;
the upper part of the fourth liquid storage tank 17 and the lower part of the second-stage hydrogen chloride washing tower 6 are provided with air pressure balance pipelines;
the gas pipeline connected with the upper part of the second-stage hydrogen chloride washing tower 6 is divided into two branch pipelines, one branch is connected with the third liquid storage tank 16, and the other branch is communicated with the first-stage alkaline washing tower 22; the first stage alkaline washing tower 22 is connected with the second stage alkaline washing tower 23 in series;
the upper part of the fourth liquid storage tank 17 is provided with a water inlet pipeline 21.
Pumps are respectively arranged on the second branch pipeline 302, the fourth branch pipeline 304, the sixth branch pipeline 306 and the eighth branch pipeline 308 and used for lifting acid liquor. The pumps described above are conventional devices and will not be described in greater detail herein.
All be provided with the valve on the pipeline among the above-mentioned system, ordinary check valve can, set up as the multi-ported valve in many pipe joints.
The lower parts of the first heat exchanger 1, the second heat exchanger 4, the third heat exchanger 11, the fourth heat exchanger 12 and the fifth heat exchanger 13 are all provided with a water inlet pipeline 21, the upper parts of the first heat exchanger and the second heat exchanger are provided with a water outlet pipeline, and the water inlet pipeline 21 and the water outlet pipeline are respectively provided with a valve so as to exchange heat.
The method for treating the waste gas in the preparation process of the lithium hexafluorophosphate comprises the following steps:
after the lithium hexafluorophosphate waste gas enters a first heat exchanger 1 through a waste gas discharge pipeline for heat exchange treatment, the lithium hexafluorophosphate waste gas is absorbed by concentrated hydrochloric acid in a first-stage hydrogen fluoride washing tower 2, and the residual gas after absorption enters a second-stage hydrogen fluoride washing tower 3 and is absorbed by the concentrated hydrochloric acid again; the residual gas containing hydrogen chloride enters a second heat exchanger 4 for heat exchange, then enters a first-stage hydrogen chloride washing tower 5 to be absorbed by water, and the gas which is not absorbed enters a second-stage hydrogen chloride washing tower 6 to be continuously absorbed by water.
More specifically, the method for treating waste gas generated in the process of preparing lithium hexafluorophosphate comprises the following steps:
s1: introducing lithium hexafluorophosphate waste gas into a first heat exchanger 1 through a waste gas discharge pipeline, carrying out heat exchange treatment, then conveying the lithium hexafluorophosphate waste gas into a first-stage hydrogen fluoride washing tower 2, and absorbing the lithium hexafluorophosphate waste gas by using an absorption liquid, wherein the absorption liquid is 25-31% concentrated hydrochloric acid, most of hydrogen fluoride in the lithium hexafluorophosphate waste gas is absorbed by the concentrated hydrochloric acid, and the absorption liquid is converted into a mixed acid of hydrofluoric acid and hydrochloric acid with the concentration of 30%;
the mixed acid is discharged through the mixed acid discharge pipe 18; or the waste water enters a first-stage hydrogen fluoride washing tower 2 for recycling after heat exchange through a first heat exchanger 1; or the waste heat enters the first heat exchanger 1 for heat exchange and then flows back to the first liquid storage tank 14 through the first branch pipeline 301;
s2: the gas absorbed by the first-stage hydrogen fluoride washing tower 2 enters the second-stage hydrogen fluoride washing tower 3 through a gas pipeline at the upper part of the first-stage hydrogen fluoride washing tower 2 and is continuously absorbed by concentrated hydrochloric acid with the concentration of 25-31%;
the mixed acid after absorbing the hydrogen fluoride in the second-stage hydrogen fluoride washing tower 3 enters the second liquid storage tank 15, and the mixed acid enters the first liquid storage tank 14 or is discharged or reused; or the mixed acid enters the second-stage hydrogen fluoride washing tower 3 to continuously absorb the waste gas hydrogen fluoride or flows back to the second liquid storage tank 15 after exchanging heat in the fourth heat exchanger 12;
s3: the gas absorbed by the second-stage hydrogen fluoride washing tower 3 enters a second heat exchanger 4 for heat exchange, and then enters a first-stage hydrogen chloride washing tower 5 to be absorbed by water;
the absorption liquid in the first-stage hydrogen chloride washing tower 5 absorbs hydrogen chloride and is converted into concentrated hydrochloric acid, the concentrated hydrochloric acid enters the third liquid storage tank 16 after being subjected to heat exchange through the second heat exchanger 4, or is collected through a hydrochloric acid discharge pipe 19 or enters the first-stage hydrogen chloride washing tower 5 after being subjected to heat exchange through the fifth heat exchanger 13 to be recycled, or returns to the third liquid storage tank 16 after being subjected to heat exchange through the fifth heat exchanger 13;
s4: the gas absorbed by the first-stage hydrogen chloride washing tower 5 enters the second-stage hydrogen chloride washing tower 6 to be continuously absorbed, and concentrated hydrochloric acid in the first-stage hydrogen chloride washing tower 5 enters the fourth liquid storage tank 17, or is conveyed to the third liquid storage tank 16 to be recycled, or enters the second-stage hydrogen chloride washing tower 6 to be recycled;
s5: the gas remained in the third liquid storage tank 16 is conveyed to the first-stage alkaline washing tower 22 and the second-stage alkaline washing tower 23 through the gas pipeline at the upper part of the second-stage hydrogen chloride washing tower 6 to be continuously absorbed.
Of course, in the above-mentioned absorption process, the mixed acid in the first liquid storage tank 14 can also enter the second liquid storage tank 15 for use; the low-concentration hydrochloric acid solution in the third storage tank 16 can also enter the fourth storage tank 17 for recycling.
Example 2
The system and the method have excellent effect in the actual use process, and the specific application and detection results are as follows:
taking the waste gas detection of the waste gas exhaust tube (No. 3) of the lithium workshop of a certain company in Jiangsu province as an example, the detection result is as follows:
TABLE 1 test parameters
TABLE 2 results of the tests
By adopting the improved system and the improved process (the invention), the detection results are summarized as follows:
TABLE 3 test parameters
TABLE 4 results of the tests
The detection instrument of the invention comprises the following instruments:
| name of instrument | Model number | Numbering |
| Acoustic calibrator | AWA6221A | ECJC/SB-021 |
| Multifunctional sound level meter | AWA6228 | ECJC/SB-020-02 |
| Intelligent double-path flue gas sampler | JF-2051 type | ECJC/SB-155-2 |
| Automatic smoke and fume tester | GH-60E | ECJC/SB-108 |
| Automatic smoke and fume tester | GH-60E | ECJC/SB-098-2 |
| Intelligent double-path flue gas sampler | JF-2051 type | ECJC/SB-155-1 |
| PH meter | PHBJ-260 | ECJC/SB-142 |
| Ion chromatograph | IC1826 | ECJC/SB-107 |
| Electronic balance (one in ten thousand) | BSA124S-CW | ECJC/SB-008-02 |
| Visible spectrophotometer | T6 Xinyue | ECJC/SB-007-02 |
| Ion meter | PXSJ-216 | ECJC/SB-104 |
| Gas chromatograph | A60 | ECJC/SB-119 |
| Ultraviolet visible spectrophotometer | T6 New century | ECJC/SB-006 |
| Infrared spectroscopic oil detector | 0L1010 | ECJC/SB-106 |
After the method is used for treating the waste gas in a lithium salt workshop of Jiangsu Xintai materials science and technology Limited company, the waste gas data of the exhaust funnel is detected, meanwhile, the waste gas detection data is collected at the exhaust funnel which does not use the method for treating the waste gas, the data of the method is compared with the data of the original waste gas treatment method (water washing), and the specific numerical values are summarized as follows:
TABLE 5 comparison of data of lithium salt workshop exhaust gas exhaust funnel of Jiangsu Xintai materials science and technology Limited
As can be seen from the data in the above table, the fluoride and chloride contents in the exhaust gas are significantly reduced, demonstrating that the absorption efficiency of the process of the present invention is high. By adopting the method disclosed by the invention to treat hydrogen fluoride and hydrogen chloride in the lithium hexafluorophosphate waste gas, the concentration of hydrofluoric acid in the mixed acid is improved, so that a byproduct can be conveniently prepared; meanwhile, the high-purity concentrated hydrochloric acid can be collected, and the additional value of the concentrated hydrochloric acid is improved.
Example 3
A system for treating waste gas in the preparation process of lithium hexafluorophosphate, which is characterized in that a waste gas discharge pipeline is connected with a first heat exchanger); the first heat exchanger 1 is connected with a first-stage hydrogen fluoride washing tower 2, a second-stage hydrogen fluoride washing tower 3, a second heat exchanger 4, a first-stage hydrogen chloride washing tower 5 and a second-stage hydrogen chloride washing tower 6 in series in sequence through gas pipelines.
The upper end of the first-stage hydrogen fluoride washing tower 2 is connected with a first liquid pipeline 7, the upper end of the second-stage hydrogen fluoride washing tower 3 is connected with a second liquid pipeline 8, the upper end of the first-stage hydrogen chloride washing tower 5 is connected with a third liquid pipeline 9, and the upper end of the second-stage hydrogen chloride washing tower 6 is connected with a fourth liquid pipeline 10.
The first-stage hydrogen fluoride washing tower 2 and the second-stage hydrogen fluoride washing tower 3 are communicated with each other and provided with a mixed acid discharge pipe 18; the first-stage hydrogen chloride washing tower 5 and the second-stage hydrogen chloride washing tower 6 are communicated with each other and provided with a hydrochloric acid discharge pipe 19.
The method for treating the waste gas in the preparation process of the lithium hexafluorophosphate comprises the following steps:
(1) adding absorption liquid, adding 25-31% concentrated hydrochloric acid into the first liquid pipeline 7 and the second liquid pipeline 8, and adding water into the third liquid pipeline 9 and the fourth liquid pipeline 10;
(2) waste gas is subjected to heat exchange by a first heat exchanger 1 and then is introduced into a first-stage hydrogen fluoride washing tower 2, and at the moment, a concentrated hydrochloric acid first liquid pipeline 7 with the concentration of 25-31% enters the first-stage hydrogen fluoride washing tower 2; mixed acid obtained after the absorption liquid reacts with the waste gas enters a mixed acid discharge pipe 18 to be discharged; the residual waste gas is continuously introduced into a second-stage hydrogen fluoride washing tower 3 for washing;
and adjusting the temperature of the waste gas to 40-50 ℃ by using a heat exchanger.
(3) The waste gas after the reaction in the second hydrogen fluoride washing tower enters the first-stage hydrogen chloride washing tower 5 after heat exchange in the second heat exchanger 4 and reacts with the water entering the third liquid pipeline 9, and the obtained hydrochloric acid with high purity is discharged through a hydrochloric acid discharge pipe 19; the residual waste gas is continuously introduced into a second-stage hydrogen chloride washing tower 6 for washing;
the obtained concentrated hydrochloric acid is adjusted to the concentration of 25 to 31 percent and then is continuously used as the absorption liquid of the two-stage hydrogen fluoride washing tower.
Claims (10)
1. The system for treating the waste gas in the lithium hexafluorophosphate preparation process is characterized in that a waste gas discharge pipeline is connected with a first heat exchanger (1);
the first heat exchanger (1) is connected with the first-stage hydrogen fluoride washing tower (2), the second-stage hydrogen fluoride washing tower (3), the second heat exchanger (4), the first-stage hydrogen chloride washing tower (5) and the second-stage hydrogen chloride washing tower (6) in series in sequence through gas pipelines.
2. The system for treating the waste gas generated in the lithium hexafluorophosphate preparation process as claimed in claim 1, wherein the lower part of the first-stage hydrogen fluoride washing tower (2) is connected in series with the first heat exchanger (1) and the first liquid storage tank (14) in sequence through an acid liquor pipeline;
the upper end of the first-stage hydrogen fluoride washing tower (2) is connected with the upper end of a third heat exchanger (11) through a first liquid pipeline (7);
the pipeline at the lower end of the third heat exchanger (11) is divided into a first branch pipeline (301) and a second branch pipeline (302), and the first branch pipeline (301) and the second branch pipeline (302) are respectively connected with the upper end and the lower end of the first liquid storage tank (14); the second branch pipeline (302) is connected with a mixed acid discharge pipe (18);
an air pressure balance pipeline is arranged between the upper part of the first liquid storage tank (14) and the lower part of the first-stage hydrogen fluoride washing tower (2).
3. The system for treating exhaust gas from a lithium hexafluorophosphate production process as set forth in claim 2, wherein the upper end of the second-stage hydrogen fluoride washing column (3) is connected to the upper end of the fourth heat exchanger (12) through a second liquid pipe (8);
the lower part of the second-stage hydrogen fluoride washing tower (3) is connected with the second liquid storage tank (15) through an acid liquor pipeline;
the pipeline at the lower end of the fourth heat exchanger (12) is divided into a third branch pipeline (303) and a fourth branch pipeline (304), and the third branch pipeline (303) and the fourth branch pipeline (304) are respectively connected with the upper end and the lower end of the second liquid storage tank (15); a pipeline for connecting the second liquid storage tank (15) with the first liquid storage tank (14) is arranged on the fourth branch pipeline (304);
a hydrochloric acid pipeline (20) is also arranged at the upper part of the second liquid storage tank (15), and an air pressure balancing pipeline is arranged between the upper part of the second liquid storage tank (15) and the lower part of the second-stage hydrogen fluoride washing tower (3).
4. The system for treating the waste gas generated in the lithium hexafluorophosphate preparation process as claimed in claim 3, wherein the lower part of the first-stage hydrogen chloride scrubber (5) is connected in series with the second heat exchanger (4) and the third liquid storage tank (16) in sequence through an acid liquor pipeline;
the upper end of the fifth heat exchanger (13) is connected with the upper end of the first-stage hydrogen chloride washing tower (5) through a third liquid pipeline (9);
the pipeline at the lower end of the fifth heat exchanger (13) is divided into a fifth branch pipeline (305) and a sixth branch pipeline (306), and the fifth branch pipeline (305) and the sixth branch pipeline (306) are respectively connected with the upper end and the lower end of the third liquid storage tank (16);
a hydrochloric acid discharge pipe (19) is arranged on the fifth branch pipeline (305), and an air pressure balance pipeline is arranged between the upper part of the third liquid storage tank (16) and the lower part of the third-stage hydrogen fluoride washing tower (5).
5. The system for treating waste gas in the process of producing lithium hexafluorophosphate according to claim 4, wherein the lower part of the second-stage hydrogen chloride scrubber (6) is connected to the fourth liquid storage tank (17) through an acid liquor pipe;
a fourth liquid pipeline (10) at the upper part of the second-stage hydrogen chloride washing tower (6) is divided into a seventh branch pipeline (307) and an eighth branch pipeline (308) which are respectively connected with the upper end and the lower end of a fourth liquid storage tank (17); a pipeline for connecting the fourth liquid storage tank (17) with the third liquid storage tank (16) is arranged on the eighth branch pipeline (308);
the upper part of the fourth liquid storage tank (17) and the lower part of the second-stage hydrogen chloride washing tower (6) are provided with air pressure balancing pipelines;
a gas pipeline connected with the upper part of the second-stage hydrogen chloride washing tower (6) is divided into two branch pipelines, one branch is connected with the third liquid storage tank (16), and the other branch is communicated with the first-stage alkaline washing tower; the first stage alkaline washing tower (41) is connected with the second stage alkaline washing tower (42) in series;
the upper part of the fourth liquid storage tank (17) is provided with a water inlet pipeline (21).
6. The system for treating waste gas generated in the process of preparing lithium hexafluorophosphate according to claim 5, wherein the second branch pipe (302), the fourth branch pipe (304), the sixth branch pipe (306) and the eighth branch pipe (308) are respectively provided with a pump; the pipelines in the system are all provided with valves.
7. The system for treating the waste gas generated in the lithium hexafluorophosphate preparation process as claimed in claim 6, wherein the first heat exchanger (1), the second heat exchanger (4), the third heat exchanger (11), the fourth heat exchanger (12) and the fifth heat exchanger (13) are all provided with water inlet pipelines at the lower parts, water outlet pipelines at the upper parts, and valves are respectively arranged on the water inlet pipelines and the water outlet pipelines.
8. The method for treating the waste gas in the preparation process of the lithium hexafluorophosphate comprises the following steps:
lithium hexafluorophosphate waste gas enters a first heat exchanger (1) through a waste gas discharge pipeline for heat exchange treatment, is absorbed by concentrated hydrochloric acid in a first-stage hydrogen fluoride washing tower (2), and the residual gas after absorption enters a second-stage hydrogen fluoride washing tower (3) for absorption again by the concentrated hydrochloric acid; the residual gas containing hydrogen chloride enters a second heat exchanger (4) for heat exchange, then enters a first-stage hydrogen chloride washing tower (5) to be absorbed by water, and the gas which is not absorbed enters a second-stage hydrogen chloride washing tower (6) to be continuously absorbed by the water.
9. The method for treating exhaust gas from a lithium hexafluorophosphate production process according to claim 8, comprising the steps of: the residual gas absorbed by the second-stage hydrogen chloride scrubber (6) is continuously absorbed by the first-stage alkaline scrubber (22) and the second-stage alkaline scrubber (23).
10. The method for treating exhaust gas from a lithium hexafluorophosphate production process according to claim 9, comprising the steps of:
s1: introducing lithium hexafluorophosphate waste gas into a first heat exchanger (1) through a waste gas discharge pipeline, carrying out heat exchange treatment, then conveying the lithium hexafluorophosphate waste gas into a first-stage hydrogen fluoride washing tower (2) to be absorbed by an absorption liquid, wherein the absorption liquid is 25-31% concentrated hydrochloric acid, most of hydrogen fluoride in the lithium hexafluorophosphate waste gas is absorbed by the concentrated hydrochloric acid, and at the moment, the absorption liquid is converted into a mixed acid of hydrofluoric acid and hydrochloric acid with the concentration of 30%;
the mixed acid is discharged through a mixed acid discharge pipe (18); or the waste water enters a first-stage hydrogen fluoride washing tower (2) for recycling after heat exchange through a first heat exchanger (1); or the waste heat enters the first heat exchanger (1) for heat exchange and then flows back to the first liquid storage tank (14) through the first branch pipeline (301);
s2: the gas absorbed by the first-stage hydrogen fluoride washing tower (2) enters a second-stage hydrogen fluoride washing tower (3) through a gas pipeline at the upper part of the first-stage hydrogen fluoride washing tower (2), and is continuously absorbed by concentrated hydrochloric acid with the concentration of 25% -31%;
the mixed acid after absorbing the hydrogen fluoride in the second-stage hydrogen fluoride washing tower (3) enters a second liquid storage tank (15), and the mixed acid enters a first liquid storage tank (14) or is discharged or reused; or the mixed acid enters a second-stage hydrogen fluoride washing tower (3) to continuously absorb the waste gas hydrogen fluoride after heat exchange in a fourth heat exchanger (12) or flows back to a second liquid storage tank (15);
s3: the gas absorbed by the second-stage hydrogen fluoride washing tower (3) enters a second heat exchanger (4) for heat exchange, and then enters a first-stage hydrogen chloride washing tower (5) to be absorbed by water;
the absorption liquid in the first-stage hydrogen chloride washing tower (5) absorbs hydrogen chloride and is converted into concentrated hydrochloric acid, the concentrated hydrochloric acid enters a third liquid storage tank (16) after heat exchange through a second heat exchanger (4), or is collected (19) through a hydrochloric acid discharge pipe or enters the first-stage hydrogen chloride washing tower (5) after heat exchange through a fifth heat exchanger (13) for cyclic utilization, or flows back to the third liquid storage tank (16) after heat exchange through the fifth heat exchanger (13);
s4: the gas absorbed by the first-stage hydrogen chloride washing tower (5) enters a second-stage hydrogen chloride washing tower (6) to be continuously absorbed, and concentrated hydrochloric acid in the first-stage hydrogen chloride washing tower (5) enters a fourth liquid storage tank (17), or is conveyed to a third liquid storage tank (16) to be recycled, or enters the second-stage hydrogen chloride washing tower (6) to be recycled;
s5: the gas remained in the third liquid storage tank (16) is conveyed to the first-stage alkaline tower (22) and the second-stage alkaline tower (23) through a gas pipeline at the upper part of the second-stage hydrogen chloride washing tower (6) to be continuously absorbed.
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| JP2000061261A (en) * | 1998-08-25 | 2000-02-29 | Chiyoda Engineering Kk | Method for recovering hydrogen chloride in high temperature gas |
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