CN109289487B - Method for treating chlorine and argon-containing tail gas of high-temperature furnace - Google Patents
Method for treating chlorine and argon-containing tail gas of high-temperature furnace Download PDFInfo
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- CN109289487B CN109289487B CN201811303382.XA CN201811303382A CN109289487B CN 109289487 B CN109289487 B CN 109289487B CN 201811303382 A CN201811303382 A CN 201811303382A CN 109289487 B CN109289487 B CN 109289487B
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B01D53/34—Chemical or biological purification of waste gases
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B01D2257/202—Single element halogens
- B01D2257/2025—Chlorine
Abstract
The invention discloses a method for treating chlorine and argon-containing tail gas of a high-temperature furnace, which comprises the following steps: a. introducing tail gas discharged by the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas; b. introducing the tail gas from which the impurity gas is removed into a chlorine purification system, and separating and recovering chlorine in the tail gas to obtain dechlorination tail gas; c. and introducing the dechlorination tail gas into an argon purification system, separating argon from other gases in the tail gas, and recovering to obtain the argon. The step b comprises the following steps: b1, enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain tail gas containing trace residual chlorine; b2, introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting the sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain the chlorine-removed tail gas.
Description
Technical Field
The invention relates to the field of environmental protection, in particular to a treatment system for chlorine and argon containing tail gas of a high-temperature furnace.
Background
At present, purification of raw material graphite of diamond synthesis enterprises at home and abroad is dry production, most of used equipment is a high-temperature furnace, the working temperature in the furnace is generally more than 2800 ℃, and the graphite has poor oxidation resistance, and is particularly easy to be oxidized into carbon dioxide at high temperature to volatilize, so that purification of the graphite at high temperature must be carried out in an oxygen-free environment with inert gas (most enterprises use argon), and a certain amount of chlorine is introduced into the furnace by many enterprises for improving the quality of the product graphite, so that the problem of the chlorine must be considered when treating tail gas; in addition, in actual production, due to the reasons of raw material change, process adjustment, poor sealing effect of each valve on the high-temperature furnace and the like, the components of the tail gas discharged by the high-temperature furnace are relatively complex, so that the problems of extremely small amount of oxygen and carbon oxide need to be considered in the tail gas treatment process besides chlorine and argon.
Therefore, the technical problem to be solved in the art is to provide a method for treating chlorine and argon containing tail gas of a high-temperature furnace, separate and recover chlorine and argon in the tail gas of the high-temperature furnace, and prevent the tail gas from being directly discharged into the air to pollute the environment.
Disclosure of Invention
In order to solve the technical problems, the invention provides a method for treating chlorine and argon-containing tail gas of a high-temperature furnace, which is used for separating and recovering chlorine and argon in the tail gas of the high-temperature furnace and preventing the tail gas from being directly discharged into the air to pollute the environment.
According to one aspect of the invention, a method for treating chlorine and argon containing tail gas of a high-temperature furnace is provided, which comprises the following steps: a. introducing tail gas discharged by the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas; b. introducing the tail gas from which the impurity gas is removed into a chlorine purification system, and separating and recovering chlorine in the tail gas to obtain dechlorination tail gas; c. and introducing the dechlorination tail gas into an argon purification system, separating argon from other gases in the tail gas, and recovering to obtain the argon.
Optionally, in the step b, the tail gas from which the impurity gas is removed is introduced into a chlorine purification system, and the specific steps of separating and recovering chlorine in the tail gas are as follows: b1, enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain tail gas containing trace residual chlorine; b2, introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting the sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain the chlorine-removed tail gas.
Wherein, step b1 further comprises the following steps: and when the chlorine adsorbed by the activated carbon adsorber is close to saturation, stopping supplying tail gas to the activated carbon adsorber, and reducing the pressure in the activated carbon adsorber to 0.1-0.3 standard atmospheric pressure to desorb the chlorine adsorbed on the activated carbon adsorber, thereby recovering the chlorine.
Optionally, in the step c, the chlorine-removed tail gas is introduced into an argon purification system, and the specific steps of separating and recovering argon from other gases in the tail gas are as follows: and enabling the chlorine-removed tail gas to penetrate through the molecular sieve membrane bed, adsorbing other gases except argon in the tail gas by the molecular sieve membrane bed, and recovering the gas penetrating through the molecular sieve membrane bed to obtain the argon.
Optionally, the method further comprises the step of stopping the supply of the tail gas to the molecular sieve membrane bed when the suction volume of the molecular sieve membrane bed is close to saturation, and reducing the pressure in the molecular sieve membrane bed to 0.1-0.3 standard atmosphere, so as to desorb the gas adsorbed on the molecular sieve membrane bed.
Optionally, the method for treating chlorine and argon-containing tail gas of the high-temperature furnace further comprises the following reaction liquid recovery steps: and introducing the reaction liquid of chlorine absorbed by the sodium hydroxide reactor into a ferrous sulfate reactor to perform the following reduction reaction to obtain a mixed liquid containing sodium chloride and ferric sulfate and a ferric hydroxide precipitate, and recovering the mixed liquid through a slag extractor to obtain the ferric hydroxide precipitate. And introducing the mixed solution containing sodium chloride and ferric sulfate in the ferrous sulfate reactor into a brine separation device, and separating to obtain sodium chloride and ferric sulfate mixed crystals and water.
Optionally, the reaction liquid recovery step further comprises: and (3) introducing the water separated by the brine separation device into a condensing device, cooling to 0-5 ℃, and pumping the water into a cooling device of the solid-gas separation device by a high-pressure water pump for recycling.
Optionally, after step a, before step b, the method further comprises passing the off-gas discharged from the solid-gas separation device through a filter to remove solid impurity gases which are not completely settled in the off-gas.
Alternatively, in step a, the solidified impurity gas is recovered by a discharger at the bottom of the solid-gas separation device.
As a preferable scheme of the invention, the method for treating the chlorine and argon containing tail gas of the high-temperature furnace comprises the following steps:
a. and introducing tail gas exhausted from the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas through a discharger at the bottom of the solid-gas separation device.
b. And (4) enabling the tail gas discharged from the solid-gas separation device to pass through a filter to remove solid impurity gases which are not completely settled in the tail gas.
c. And (3) enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine gas by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain the tail gas containing trace residual chlorine gas.
And when the chlorine adsorbed by the activated carbon adsorber is close to saturation, stopping supplying tail gas to the activated carbon adsorber, and reducing the pressure in the activated carbon adsorber to 0.1-0.3 standard atmospheric pressure, so that the chlorine adsorbed on the activated carbon adsorber is desorbed and recovered to obtain the chlorine.
d. And introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting the sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain the dechlorination tail gas.
e. And recovering the reaction liquid in the sodium hydroxide reactor.
e1, introducing the reaction solution of chlorine absorbed by the sodium hydroxide reactor into a ferrous sulfate reactor for reduction reaction to obtain a mixed solution containing sodium chloride and ferric sulfate and a ferric hydroxide precipitate, and recovering the mixed solution through a slag extractor to obtain the ferric hydroxide precipitate.
e2, introducing the mixed liquid containing sodium chloride and ferric sulfate in the ferrous sulfate reactor into a brine separation device, and separating to obtain sodium chloride, ferric sulfate mixed crystals and water.
e3, introducing the water separated by the brine separation device into a condensing device, cooling to 0-5 ℃, and pumping the water into a cooling device of the solid-gas separation device by a high-pressure water pump for recycling.
f. And enabling the chlorine-removed tail gas passing through the sodium hydroxide reactor to penetrate through the molecular sieve membrane bed, adsorbing other gases except argon in the tail gas by the molecular sieve membrane bed, and recovering the gas penetrating through the molecular sieve membrane bed to obtain the argon.
When the air suction amount of the molecular sieve membrane bed is close to saturation, tail gas supply to the molecular sieve membrane bed is stopped, the pressure in the molecular sieve membrane bed is reduced to 0.1-0.3 standard atmospheric pressure, and gas adsorbed on the molecular sieve membrane bed is desorbed.
The invention has the beneficial effects that:
the method for treating the chlorine-and argon-containing tail gas of the high-temperature furnace separates and recycles the impurity gas, the argon gas and part of the chlorine gas by utilizing the difference of the phase change temperature, the adsorption property to the activated carbon and the passing property of the molecular sieve of the chlorine gas, the inert gas and the impurity gas in the tail gas of the high-temperature furnace, and prevents the tail gas from being directly discharged into the air to pollute the environment.
The method for treating the chlorine and argon-containing tail gas of the high-temperature furnace comprises the steps of introducing chlorine which is not completely adsorbed by the activated carbon adsorber into a sodium hydroxide reactor to react with a sodium hydroxide solution, and introducing a reaction solution into a ferrous sulfate reactor to react to obtain a mixed solution of ferric hydroxide precipitate and sodium chloride and ferric sulfate, wherein the mixed solution is harmless to the environment.
According to the method for treating the chlorine and argon-containing tail gas of the high-temperature furnace, the mixed solution of sodium chloride and ferric sulfate in the ferrous sulfate reactor is subjected to salt water separation, so that the mixed crystal of sodium chloride and ferric sulfate and water are finally obtained and respectively recovered, and the water is cooled and then conveyed back to the method for recycling, so that the resource waste can be reduced, the method is economical and environment-friendly, and has practical popularization value.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. It should be noted that, in the embodiments and examples of the present application, the feature vectors may be arbitrarily combined with each other without conflict.
A method for treating chlorine and argon-containing tail gas of a high-temperature furnace comprises the following steps:
a. and introducing tail gas exhausted from the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas through a discharger at the bottom of the solid-gas separation device.
b. And (4) enabling the tail gas discharged from the solid-gas separation device to pass through a filter to remove solid impurity gases which are not completely settled in the tail gas.
c. And (3) enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine gas by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain the tail gas containing trace residual chlorine gas.
And when the chlorine adsorbed by the activated carbon adsorber is close to saturation, stopping supplying tail gas to the activated carbon adsorber, and reducing the pressure in the activated carbon adsorber to 0.1-0.3 standard atmospheric pressure, so that the chlorine adsorbed on the activated carbon adsorber is desorbed and recovered to obtain the chlorine.
d. And introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting the sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain the dechlorination tail gas.
e. Recovering the reaction liquid in the sodium hydroxide reactor:
e1, introducing the reaction solution of chlorine absorbed by the sodium hydroxide reactor into a ferrous sulfate reactor for reduction reaction to obtain a mixed solution containing sodium chloride and ferric sulfate and a ferric hydroxide precipitate, and recovering the mixed solution through a slag extractor to obtain the ferric hydroxide precipitate.
e2, introducing the mixed liquid containing sodium chloride and ferric sulfate in the ferrous sulfate reactor into a brine separation device, and separating to obtain sodium chloride, ferric sulfate mixed crystals and water.
e3, introducing the water separated by the brine separation device into a condensing device, cooling to 0-5 ℃, and pumping the water into a cooling device of the solid-gas separation device by a high-pressure water pump for recycling.
f. And enabling the chlorine-removed tail gas passing through the sodium hydroxide reactor to penetrate through the molecular sieve membrane bed, adsorbing other gases except argon in the tail gas by the molecular sieve membrane bed, and recovering the gas penetrating through the molecular sieve membrane bed to obtain the argon.
When the air suction amount of the molecular sieve membrane bed is close to saturation, tail gas supply to the molecular sieve membrane bed is stopped, the pressure in the molecular sieve membrane bed is reduced to 0.1-0.3 standard atmospheric pressure, and gas adsorbed on the molecular sieve membrane bed is desorbed.
Specifically, when the high-temperature furnace system is started to operate, the tail gas discharged from the furnace body is subjected to three steps, so that the solidification recovery of impurity gases, the recovery of chlorine and argon and the discharge of other gases and water can be completely realized.
The tail gas containing chlorine, argon and impurity gas, etc. discharged from high-temp. furnace is firstly fed into solid-gas separation device whose periphery is equipped with cooling circulating water to make cooling, the impurity gas (metal and metal oxide) volatilized from graphite can be quickly solidified and settled by means of quenching, and can be discharged from bottom closed discharger to recover (in which there is a small quantity of chloride produced by reaction with chlorine), and the chlorine and argon gas still existed in the form of gas can be fed into filter from top portion of solid-gas separation device to filter out the solid impurity which is not completely settled.
For the argon and chlorine-containing gas, firstly, the chlorine-containing gas is subjected to adsorption treatment by using an activated carbon adsorber (most of the chlorine is removed; and then the rest of the gas containing only a trace amount of chlorine is subjected to chemical treatment, namely, the gas is reacted with a sodium hydroxide solution (NaOH) in a sodium hydroxide reactor:
Cl2+2NaOH==NaCl+NaClO+H2O
the product of the reaction and the reaction liquid enter a ferrous sulfate reactor together to react with ferrous sulfate (FeSO)4) Carrying out reduction reaction:
6FeSO4+3NaClO+3H2O=2Fe2(SO4)3+2Fe(OH)3↓+3NaCl
finally generating the chlorine-containing salt (NaCl) and the ferric salt Fe2(SO4)3And iron hydroxides Fe (OH)3And (4) precipitating. Precipitation of Fe (OH)3Can be discharged and recycled through a slag extractor, and the mixed solution NaCl and Fe remained in the ferrous sulfate reactor2(SO4)3The solution is not harmful to environment, but needs further treatment, and the mixed solution can be introduced into a brine separator to recover NaCl and Fe2(SO4)3And mixing the crystals, cooling the separated water to 0-5 ℃ through a condensing device, and conveying the water to a cooling device of a solid-gas separation device through a high-pressure water pump for recycling.
The argon-containing gas discharged from the sodium hydroxide reactor is passed directly through a molecular sieve membrane bed, since the molecular sieve is a titanosilicate (ETS-3A), a material having an aperture 3A, allowing only argon to pass through, while other gas molecules such as oxygen, which are large in cross section, remain, thereby achieving separation of argon from other gases.
Example 1
The measured discharge capacity of the tail gas of the furnace body is 1100L/min, the chlorine content in the discharged gas is 5 percent (volume percentage) and the argon content is 90 percent through rapid measurement, at the moment, the gas containing argon, chlorine and impurities discharged by the furnace body is directly introduced into a solid-gas separation device which is cooled by cooling circulating water at the periphery, the impurities are solidified due to shock cooling, the impurities are settled in the solid-gas separation device (wherein metal oxides, partial metal chlorides and the like are contained), and then the impurities are discharged by a closed discharger at the bottom of the solid-gas separation device, and the quantity is about 0.045kg/min through recovery; and the chlorine and argon containing gas is discharged from the top of the solid-gas separation device and then enters a subsequent chlorine purification treatment system and an argon purification treatment system.
The gas containing argon and chlorine discharged from the top of the solid-gas separation device firstly enters an activated carbon adsorber, the chlorine in the gas is adsorbed (most of the chlorine is removed), and the quantity is 45L/min after recovery and determination; then the rest gas containing trace chlorine and a large amount of argon is chemically treated in a sodium hydroxide reactor, namely, chlorine reacts with sodium hydroxide solution (NaOH), and the solution after reaction is introduced into a ferrous sulfate reactor by the sodium hydroxide reactor and is mixed with ferrous sulfate (FeSO)4) And (4) reacting. Finally generating NaCl containing chloride salt and Fe containing iron salt2(SO4)3And iron hydroxides Fe (OH)3Precipitating, and obtaining the amount of about 0.033kg/min by recovering the precipitate; the mixed liquid left in the ferrous sulfate reactor is introduced into a brine separation device to recover NaCl and Fe2(SO4)3Mixing the crystals, and recycling the separated water.
The argon-containing gas removed from the NaOH solution reactor was passed directly through the molecular sieve membrane bed, since the molecular sieve was a titanosilicate (ETS-3A) material, i.e. having a pore diameter of 3A, allowing only argon to pass through, while other gas molecules with large cross-sections were left to be removed, and the molecular sieve membrane bed was depressurized (to a relative pressure P/P0= 0.15) desorbing argon gas and recovering argon gas with a purity of 99.99% (amount 950L/min).
Example 2
Actually measuring the tail gas discharge capacity of a furnace body to be 1300L/min, quickly measuring the chlorine content in the discharged gas to be 6 percent (volume percentage) and the argon content to be 90 percent, directly introducing the gas containing argon, chlorine and impurities discharged by the furnace body into a solid-gas separation device with cooling circulating water at the periphery for cooling, solidifying the impurities due to shock cooling, settling in the solid-gas separation device (wherein metal oxides, partial metal chlorides and the like exist), discharging by a closed discharger at the bottom of the solid-gas separation device, and obtaining the quantity of about 0.053kg/min through recovery; and the chlorine and argon containing gas is discharged from the top of the solid-gas separation device and then enters a subsequent chlorine purification treatment system and an argon purification treatment system.
The gas containing argon and chlorine discharged from the top of the solid-gas separation device firstly enters an activated carbon adsorber, the chlorine in the gas is adsorbed (most of the chlorine is removed), and the quantity is 54L/min after recovery and determination; then the rest gas containing trace chlorine and a large amount of argon is chemically treated in a sodium hydroxide reactor, namely, chlorine reacts with sodium hydroxide solution (NaOH), and the solution after reaction is discharged from the sodium hydroxide reactor into a ferrous sulfate reactor and then reacts with ferrous sulfate (FeSO)4) Reaction to finally generate NaCl containing chloride salt and Fe containing iron salt2(SO4)3And iron hydroxides Fe (OH)3Precipitating by recovering the precipitateThe amount of the compound is about 0.039 kg/min; the mixed liquid left in the ferrous sulfate reactor is introduced into a brine separation device to recover NaCl and Fe2(SO4)3The crystals are mixed and the separated water can be recycled.
The argon-containing gas removed from the NaOH solution reactor was passed directly through the molecular sieve membrane bed, since the molecular sieve was a titanosilicate (ETS-3A) material, i.e. having a pore diameter of 3A, allowing only argon to pass through, while other gas molecules with large cross-sections were left to be removed, and the molecular sieve membrane bed was depressurized (to a relative pressure P/P0= 0.18) desorption of argon gas and recovery of argon gas with a purity of 99.99% (amount 1122L/min).
Example 3
Actually measuring the tail gas discharge capacity of a furnace body to be 900L/min, quickly measuring the chlorine content in the discharged gas to be 6 percent (volume percentage) and the argon content to be 88 percent, directly introducing the gas containing argon, chlorine and impurities discharged by the furnace body into a solid-gas separation device with cooling circulating water at the periphery for cooling, solidifying the impurity gas due to shock cooling, settling in the solid-gas separation device (wherein metal oxides, partial metal chlorides and the like exist), discharging by a closed discharger at the bottom of the solid-gas separation device, and obtaining the quantity of about 0.037kg/min through recovery; and the chlorine and argon containing gas is discharged from the top of the solid-gas separation device and then enters a subsequent chlorine purification treatment system and an argon purification treatment system.
The gas containing argon and chlorine discharged from the top of the solid-gas separation device firstly enters an activated carbon adsorber, the chlorine in the gas is adsorbed (most of the chlorine is removed), and the quantity is 44L/min after recovery and determination; then the rest gas containing trace chlorine and a large amount of argon is chemically treated in a sodium hydroxide reactor, namely, chlorine reacts with sodium hydroxide solution (NaOH), and the solution after reaction is discharged from the sodium hydroxide reactor into a ferrous sulfate reactor and then reacts with ferrous sulfate (FeSO)4) Reaction to finally generate NaCl containing chloride salt and Fe containing iron salt2(SO4)3And iron hydroxides Fe (OH)3Precipitating, wherein the amount of the precipitate is about 0.027kg/min by recovering the precipitate; and the mixed liquor remained in the ferrous sulfate reactor is introduced into a brine separation device,recovering NaCl and Fe2(SO4)3The crystals are mixed and the separated water can be recycled.
The argon-containing gas removed from the NaOH solution reactor was passed directly through the molecular sieve membrane bed, since the molecular sieve was a titanosilicate (ETS-3A) material, i.e. having a pore diameter of 3A, allowing only argon to pass through, while other gas molecules with large cross-sections were left to be removed, and the molecular sieve membrane bed was depressurized (to a relative pressure P/P0= 0.21) desorption of argon gas, and recovery of argon gas having a purity of 99.99% (amount of 761L/min).
It is to be noted that, in this document, the terms "comprises", "comprising" or any other variation thereof are intended to cover a non-exclusive inclusion, so that an article or apparatus including a series of elements includes not only those elements but also other elements not explicitly listed or inherent to such article or apparatus. Without further limitation, an element defined by the phrase "comprising … …" does not exclude the presence of additional like elements in the article or device comprising the element.
The above embodiments are merely to illustrate the technical solutions of the present invention and not to limit the present invention, and the present invention has been described in detail with reference to the preferred embodiments. It will be understood by those skilled in the art that various modifications and equivalent arrangements may be made without departing from the spirit and scope of the present invention and it should be understood that the present invention is to be covered by the appended claims.
Claims (6)
1. A method for treating chlorine and argon-containing tail gas of a high-temperature furnace is characterized by comprising the following steps:
a. introducing tail gas discharged by the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas;
b. introducing the tail gas from which the impurity gas is removed into a chlorine purification system, and separating and recovering chlorine in the tail gas to obtain dechlorination tail gas;
c. introducing the dechlorination tail gas into an argon purification system, separating argon from other gases in the tail gas, and recovering to obtain argon;
in the step c, the chlorine-removal tail gas is introduced into an argon purification system, and argon is separated from other gases in the tail gas and is recovered, and the method specifically comprises the following steps: enabling the chlorine-removed tail gas to penetrate through a molecular sieve membrane bed, adsorbing other gases except argon in the tail gas by the molecular sieve membrane bed, and recovering the gas penetrating through the molecular sieve membrane bed to obtain argon;
the molecular sieve film bed is a titanium silicate 3A molecular sieve;
and b, introducing the tail gas from which the impurity gas is removed into a chlorine purification system, and separating and recovering chlorine in the tail gas comprises the following specific steps:
b1, enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain tail gas containing trace residual chlorine;
b2, introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting the sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain chlorine-removed tail gas;
further comprises a reaction liquid recovery step:
introducing a reaction solution of chlorine absorbed by a sodium hydroxide reactor into a ferrous sulfate reactor for reduction reaction to obtain a mixed solution containing sodium chloride and ferric sulfate and a ferric hydroxide precipitate, and recovering the mixed solution through a slag extractor to obtain the ferric hydroxide precipitate;
introducing mixed liquid containing sodium chloride and ferric sulfate in the ferrous sulfate reactor into a brine separation device, and separating to obtain sodium chloride and ferric sulfate mixed crystals and water;
the reaction liquid recovery step further comprises: and introducing the water separated by the brine separation device into a condensing device, cooling to 0-5 ℃, and pumping the water into a cooling device of the solid-gas separation device by a high-pressure water pump for recycling.
2. The method for treating chlorine and argon-containing tail gas of a high-temperature furnace according to claim 1, wherein the step b1 further comprises the following steps: and when the chlorine adsorbed by the activated carbon adsorber is close to saturation, stopping supplying tail gas to the activated carbon adsorber, and reducing the pressure in the activated carbon adsorber to 0.1-0.3 standard atmospheric pressure to desorb the chlorine adsorbed on the activated carbon adsorber, thereby recovering the chlorine.
3. The method according to claim 1, further comprising the step of, when the amount of gas sucked into the molecular sieve membrane bed approaches saturation, stopping the supply of the tail gas to the molecular sieve membrane bed and reducing the pressure in the molecular sieve membrane bed to 0.1 to 0.3 atm to desorb the gas adsorbed on the molecular sieve membrane bed.
4. The method for treating chlorine and argon containing tail gas of a high temperature furnace according to claim 1, wherein after the step a and before the step b, the method further comprises the step of passing the tail gas discharged from the solid-gas separation device through a filter to remove solid impurity gases which are not completely settled in the tail gas.
5. The method for treating chlorine and argon-containing tail gas of a high-temperature furnace according to claim 4, wherein in the step a, the solidified impurity gas is recycled through a discharger at the bottom of the solid-gas separation device.
6. The method for treating chlorine and argon-containing tail gas of the high-temperature furnace according to any one of claims 1 to 5, characterized by comprising the following steps:
a. introducing tail gas discharged by the high-temperature furnace into a solid-gas separation device with a cooling device arranged on the periphery, removing impurity gas in the tail gas due to quenching solidification, and recovering the solidified impurity gas through a discharger at the bottom of the solid-gas separation device;
b. enabling tail gas discharged by the solid-gas separation device to pass through a filter to remove incompletely-settled solid impurity gas in the tail gas;
c. enabling the tail gas from which the impurity gas is removed to pass through an activated carbon adsorber, adsorbing chlorine gas by the activated carbon adsorber, and enabling the rest gas to pass through the activated carbon adsorber to obtain tail gas containing trace residual chlorine gas;
when the chlorine adsorbed by the activated carbon adsorber is close to saturation, stopping supplying tail gas to the activated carbon adsorber, and reducing the pressure in the activated carbon adsorber to 0.1-0.3 standard atmospheric pressure, so that the chlorine adsorbed on the activated carbon adsorber is desorbed and recovered to obtain chlorine;
d. introducing the rest gas penetrating through the activated carbon adsorber into a sodium hydroxide reactor, and reacting a sodium hydroxide solution with trace chlorine in the tail gas to remove residual chlorine in the tail gas to obtain dechlorinated tail gas;
e. recovering the reaction liquid in the sodium hydroxide reactor:
e1, introducing the reaction solution of chlorine absorbed by the sodium hydroxide reactor into a ferrous sulfate reactor for reduction reaction to obtain a mixed solution containing sodium chloride and ferric sulfate and a ferric hydroxide precipitate, and recovering the mixed solution through a slag extractor to obtain the ferric hydroxide precipitate;
e2, introducing the mixed solution containing sodium chloride and ferric sulfate in the ferrous sulfate reactor into a brine separation device, and separating to obtain sodium chloride and ferric sulfate mixed crystals and water;
e3, introducing the water separated by the brine separation device into a condensing device, cooling to 0-5 ℃, and pumping the water into a cooling device of the solid-gas separation device by a high-pressure water pump for recycling;
f. enabling the chlorine-removed tail gas passing through the sodium hydroxide reactor to penetrate through a molecular sieve membrane bed, adsorbing other gases except argon in the tail gas by the molecular sieve membrane bed, and recovering the gas penetrating through the molecular sieve membrane bed to obtain argon;
when the air suction amount of the molecular sieve membrane bed is close to saturation, tail gas supply to the molecular sieve membrane bed is stopped, the pressure in the molecular sieve membrane bed is reduced to 0.1-0.3 standard atmospheric pressure, and gas adsorbed on the molecular sieve membrane bed is desorbed.
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