WO2023279279A1 - 尾气处理方法 - Google Patents

尾气处理方法 Download PDF

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Publication number
WO2023279279A1
WO2023279279A1 PCT/CN2021/104940 CN2021104940W WO2023279279A1 WO 2023279279 A1 WO2023279279 A1 WO 2023279279A1 CN 2021104940 W CN2021104940 W CN 2021104940W WO 2023279279 A1 WO2023279279 A1 WO 2023279279A1
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tail gas
ionic liquid
tower
regeneration
hcl
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PCT/CN2021/104940
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English (en)
French (fr)
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杨志健
陈永乐
陈宇涵
刘建
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安徽金禾实业股份有限公司
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Priority to PCT/CN2021/104940 priority Critical patent/WO2023279279A1/zh
Priority to CN202180002105.9A priority patent/CN113646062B/zh
Publication of WO2023279279A1 publication Critical patent/WO2023279279A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • B01D53/002—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 condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • B01D53/14—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 absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • B01D53/14—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 absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—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
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor

Definitions

  • the invention belongs to the industrial technical field of separation and recovery of chemical tail gas, and in particular relates to a tail gas treatment method.
  • Sucralose-6-ester is one of the important intermediates in the preparation of sucralose.
  • Sucralose-6-ester can be obtained by esterification of sucrose and then chlorinated by chlorinated reagents.
  • industrial chlorinated reagents mainly include Vilsmeier (Vilsmeier) chlorinated reagents and phosgene products are used by fewer companies due to the high risk and high pollution of phosgene.
  • the Vilsmeier chlorination reagent is mainly prepared from DMF and dimethyl sulfoxide, which is relatively safe to use.
  • tail gas will be produced, including HCl, SO 2 , water, DMF and trichloroethane.
  • the traditional treatment of the above-mentioned tail gas usually adopts operations such as cooling and condensation, sulfuric acid dehydration, and activated carbon adsorption, but this is not enough to remove all organic matter and water in the tail gas. /Inorganic solids adhere to the surface of flow-through materials such as pipe walls and delivery pumps, causing serious equipment corrosion and blockage, which greatly limits the recovery of HCl and SO 2 ; on the other hand, HCl and SO 2 cannot be completely separated, such as The hydrochloric acid obtained by direct water adsorption of HCl contains a large amount of SO 2 gas, and the SO 2 gas will form H 2 SO 3 in water.
  • Chinese patent CN208511908 adopts low-temperature condensation to separate HCl and SO 2 mixed gas.
  • the method is to utilize the difference in boiling point between the two, and air is blown into the SO 2 product to take out HCl, thereby improving the purity of the SO 2 product.
  • This method simply separates the two gases with different boiling points, but the energy consumption is much higher than other methods, and the purity of the product obtained is not good; In the case of solvents, this process is not applicable.
  • Chinese patent CN108373139 also adopts cooling separation method to separate HCl and SO 2 on the basis of removing water and solvent from sucralose chlorination tail gas.
  • This method uses concentrated sulfuric acid to remove water, and the water removal effect is better, but the subsequent regeneration or treatment of waste acid is more troublesome; the organic matter is simply collected by condensation during the separation process, and the complete removal of the organic matter cannot be achieved, so the obtained HCl and The SO2 product is not very pure.
  • Chinese patent CN103466550 reports a D-esterification tail gas recovery system in the amoxicillin production process, and the tail gas system mainly contains HCl and SO 2 gases.
  • This method uses pressurized rectification to separate the two gases, and uses triple pressurized rectification towers to separate the gas and organic matter; however, the system does not contain water, so the requirements for system equipment are relatively low; however, the chlorination of sucrose More water will be produced in the process, which will have a great test on the separation method and equipment of the system.
  • This method is not suitable for the waste gas produced by the chlorination reaction of sucrose.
  • tail gas treatment method is proposed, which can overcome the above problems or at least partially solve the above problems.
  • a method for treating tail gas is provided, the tail gas is produced in the process of generating sucralose-6-ester through chlorination reaction of sucrose-6-ester, the method comprising:
  • Condensation step cooling and condensing the tail gas to remove part of the organic solvent and part of the water to obtain the first solution and the first tail gas;
  • Removal step using hydrophilic ionic liquid to adsorb and separate the first tail gas to remove most of the water and part of the organic solvent to obtain the second tail gas;
  • Separation step adsorb and filter the second tail gas with a solid adsorbent to obtain a gaseous mixture, and separate the gaseous mixture to obtain gaseous hydrogen chloride and liquid sulfur dioxide;
  • Phase inversion step pass gaseous hydrogen chloride into water to obtain hydrochloric acid.
  • the method also includes:
  • the first regeneration step included in the removal step regenerating the hydrophilic ionic liquid used in the removal step to obtain the regenerated hydrophilic ionic liquid and the first regeneration tail gas;
  • the regenerated hydrophilic ionic liquid is recovered for use in the removal step.
  • the regeneration temperature of the hydrophilic ionic liquid is 80-120° C.
  • the regeneration vacuum is -0.1 to -0.05 MPa.
  • the method also includes:
  • a recovery step after the first regeneration step using a lipophilic ionic liquid to adsorb the first regeneration tail gas to remove organic components to obtain a third tail gas;
  • the obtained saturated sodium chloride aqueous solution having adsorbed hydrogen chloride is subjected to hydrogen chloride regeneration treatment to obtain regenerated hydrogen chloride, and the regenerated hydrogen chloride is recovered to the hydrogen chloride to enter the phase inversion step; the saturated sodium chloride aqueous solution having released hydrogen chloride is recovered to saturated chlorinated in sodium solution.
  • the method also includes:
  • the second regeneration step after the recovery step regenerating the lipophilic ionic liquid used in the recovery step to obtain the regenerated lipophilic ionic liquid and the fifth tail gas;
  • the regeneration temperature of the lipophilic ionic liquid is 80-120° C.
  • the regeneration vacuum is -0.1 to -0.05 MPa.
  • the lipophilic ionic liquid is 1-ethyl-3-methylimidazole dibutyl phosphate and/or 1-butyl-3-methylimidazole dibutyl phosphate ;
  • Using lipophilic ionic liquids to adsorb the first regeneration tail gas includes:
  • the first regeneration tail gas is adsorbed by lipophilic ionic liquid.
  • the cooling temperature is set to 0-30°C.
  • the hydrophilic ionic liquid is one or more of pyridine hydrogen sulfate, methylimidazolium hydrogen sulfate and ethylimidazolium hydrogen sulfate.
  • using hydrophilic ionic liquid to adsorb the first tail gas includes:
  • a hydrophilic ionic liquid is used to adsorb the first tail gas.
  • the beneficial effects of the present application are that the use of ionic liquids to adsorb impurities in the chlorinated tail gas effectively solves the impact of water and organic matter on the separation of HCl and SO2 gases before the pressurized rectification, and solves the problem caused by the pressurized separation process.
  • This application is mainly based on ionic liquid adsorption, and organically combined with condensation, rectification and other means, it can effectively treat the chlorinated tail gas in the sucralose production process, realize the effective separation of HCl and SO2, and obtain high - quality Hydrochloric acid and liquid SO2 products, and the overall treatment process is simple, low cost, and has great economic and application value.
  • Fig. 1 shows a schematic flow chart of a tail gas treatment method according to an embodiment of the present application
  • Fig. 2 shows a schematic structural diagram of an exhaust gas treatment device according to an embodiment of the present application.
  • Ionic liquids also known as Room Temperature Ionic Liquids (RTILs for short)
  • RTILs Room Temperature Ionic Liquids
  • It is a liquid organic molten salt with a melting point below 100°C. Since it is completely composed of anions and cations, it has many properties different from conventional organic solvents, such as "zero" vapor pressure, high thermal stability, strong solubility and The structure and function can be designed, etc., and it has great application potential in the fields of organic reaction, liquid phase separation, gas absorption, and electrochemistry.
  • chlorination of sucrose using Vilsmeier chlorination reagent to generate the tail gas produced by the sucralose-6-ester process referred to as the treatment of chlorinated tail gas
  • the treatment of chlorinated tail gas has the disadvantages of poor separation effect, easy to cause serious equipment corrosion, and compressed gas
  • the formation of solid deposits leads to problems such as pipe blockage.
  • This application introduces ionic liquids into the treatment of chlorinated tail gas, absorbs moisture and organic impurities in the tail gas through ionic liquids, and combines condensation and pressurized rectification technologies to effectively overcome the shortcomings of the prior art.
  • Fig. 1 shows a schematic flow chart of an exhaust gas treatment method according to an embodiment of the present application. It can be seen from Fig. 1 that the present application includes at least steps S110 to S140:
  • Condensation step S110 cooling and condensing the tail gas to remove part of the organic solvent and water to obtain a first solution and a first tail gas.
  • the tail gas of the present application refers to sucrose-6 ester and chlorination reagent, such as Vilsmeier reagent etc., carry out chlorination reaction, produce in the chlorination process of sucralose-6-ester, mainly contain gaseous water, HCl, SO 2 , and organic solvents such as DMF and trichloroethane.
  • chlorination reagent such as Vilsmeier reagent etc.
  • carry out chlorination reaction produce in the chlorination process of sucralose-6-ester, mainly contain gaseous water, HCl, SO 2 , and organic solvents such as DMF and trichloroethane.
  • the mainstream technology for the treatment of the above-mentioned tail gas usually adopts the traditional process of cooling condensation-concentrated sulfuric acid dehydration-activated carbon desolventization-pressurized rectification and separation.
  • the equipment is corroded, and it is easy to carbonize the solvent, and the concentrated sulfuric acid is not easy to regenerate after absorbing water; the traditional condensation plus activated carbon adsorption cannot completely remove the high concentration of organic matter contained in the gas, which will lead to the enrichment of organic matter in the subsequent compression process. And in the presence of SO2 , it will adhere to the pipe wall or valve together with solid particles, blocking the pipeline, etc.
  • the above-mentioned tail gas is cooled and condensed.
  • gaseous organic solvents such as gaseous DMF and gaseous trichloroethane will be converted into liquids, which are recorded as the first
  • the solution is split with the gaseous mixture, and the gaseous mixture is recorded as the first tail gas.
  • the first solution mainly contains liquid water, DMF and trichloroethane, and the first solution can be used for solvent recovery treatment.
  • the first tail gas contains gaseous hydrogen chloride, SO 2 , and part of gaseous water, a small amount of gaseous DMF and gaseous trichloroethane.
  • the cooling and condensation temperature can be set at 0-30°C.
  • Removal step S120 Adsorbing the first tail gas with a hydrophilic ionic liquid to remove most of the water and organic solvent therein to obtain a second tail gas;
  • the condensation step the content of the organic solvent has been reduced to a very low level, the content is very small, and the water content is relatively high.
  • This step selects the hydrophilic ionic liquid to adsorb the first tail gas, which is due to the hydrophilic ionic liquid. Moisture has a strong adsorption effect, and also has a certain adsorption effect on organic solvents. After the first tail gas is adsorbed by hydrophilic ionic liquids, the water is basically eliminated, and the content of organic solvents is also very low.
  • Separation step S130 Adsorb and filter the second tail gas with a solid adsorbent to obtain a first gaseous mixture, and separate the first gaseous mixture to obtain gaseous hydrogen chloride and liquid sulfur dioxide.
  • a solid adsorbent such as activated carbon, etc.
  • the gaseous mixture mainly includes gaseous HCl and Gaseous SO 2 also includes extremely small amounts of water vapor and gaseous organic solvents.
  • the specific separation process can refer to the prior art, and the methods of pressurization, adsorption, filtration and pressurized rectification can also be used.
  • First Pressurize the first gaseous mixture then use solid adsorbent to adsorb the residual organic solvent again, and finally use the difference in volatility between gaseous HCl and gaseous SO2 to separate the gaseous mixture by using pressurized rectification technology, During pressurization, gaseous SO 2 is converted into liquid SO 2 , so that gaseous HCl and gaseous SO 2 are separated from each other, and after separation, gaseous HCl and liquid SO 2 are obtained.
  • phase inversion step S140 passing gaseous hydrogen chloride into water to obtain hydrochloric acid.
  • Gaseous hydrogen chloride is not easy to store, and in practical applications, hydrochloric acid is a more commonly used chemical reagent, therefore, for economic considerations, gaseous hydrogen chloride is converted into a liquid product, i.e. hydrochloric acid, specifically, gaseous hydrogen chloride is passed into water, i.e. Hydrochloric acid is available.
  • this application utilizes ionic liquids to adsorb impurities in the chlorinated tail gas, and before the pressurized rectification, effectively solves the impact of water and organic matter on the separation of HCl and SO 2 gases , which solves the serious corrosion and blockage problems caused by the organic/inorganic solids attached to the pipe wall and delivery pump during the pressure separation process, and can obtain high-purity liquid SO 2 products;
  • the ionic liquid is extremely low in corrosion, and adopts Ionic liquid replaces concentrated sulfuric acid, which can effectively overcome the equipment corrosion and subsequent treatment problems caused by the dehydration of concentrated sulfuric acid in the traditional technology; in addition, ionic liquid has high reproducibility, and the regeneration process is simple, which greatly reduces the cost of tail gas treatment .
  • This application is mainly based on ionic liquids, and organically combined with condensation, rectification and other means, which can effectively treat the chlorinated tail gas in the sucralose production process, realize the effective separation of HCl and SO2, and obtain high - quality hydrochloric acid And liquid SO 2 products, and the overall treatment process is simple, low cost, and has great economic and application value.
  • the above method further includes: a first regeneration step included in the removal step: performing regeneration treatment on the hydrophilic ionic liquid used in the removal step to obtain a regenerated hydrophilic ionic liquid and the first regeneration tail gas; and recycling the regeneration hydrophilic ionic liquid to the removal step.
  • the second tail gas and the hydrophilic ionic liquid with adsorbed impurities are obtained, that is, the hydrophilic ionic liquid after use.
  • the liquid has strong regeneration ability, simple regeneration process, and low regeneration cost. Therefore, the hydrophilic ionic liquid can be regenerated and recycled, which can greatly save the treatment cost of chlorinated tail gas.
  • the hydrophilic ionic liquid is sent into the ionic liquid regeneration tank for regeneration, and the regenerated hydrophilic ionic liquid is extracted from the bottom of the regeneration tank, and after being condensed by a condenser, After being filtered through a filter, it can be refluxed and used repeatedly.
  • the regeneration of the ionic liquid it is to make the ionic liquid release the gaseous substance that has been adsorbed.
  • the present application does not limit the regeneration conditions of the hydrophilic ionic liquid, any gaseous substance that can make the ionic liquid desorbed can be achieved, such as by stirring, heating and other means to achieve the above purpose; in other embodiments of the present application, the For economic considerations, the regeneration temperature of the hydrophilic ionic liquid is 80-120°C, and the regeneration vacuum is -0.1 to -0.05MPa. Under the above conditions, the hydrophilic ionic liquid can quickly remove the adsorbed gaseous substances.
  • the hydrophilic ionic liquid in the process of adsorbing the first tail gas, the hydrophilic ionic liquid will not only adsorb the moisture and organic solvent in the tail gas, but also a part of the target products HCl and SO It is taken out of the first tail gas, so when the hydrophilic ionic liquid is regenerated, the first regeneration tail gas produced will contain some target products HCl and SO in addition to organic solvents such as impurity water, DMF and trichloroethane . In order to further increase the yield of HCl and SO 2 , the first regeneration tail gas can be recovered and reprocessed so as to separate the HCl and SO 2 therein.
  • the above method further includes: a recovery step after the first regeneration step: using a lipophilic ionic liquid to adsorb the first regeneration tail gas to remove organic components to obtain a third tail gas ; Adsorb the third tail gas by using a saturated sodium chloride aqueous solution to absorb hydrogen chloride to obtain a fourth tail gas; recycle the fourth tail gas to the first tail gas to enter the removal step.
  • the obtained saturated sodium chloride aqueous solution having adsorbed hydrogen chloride is subjected to hydrogen chloride regeneration treatment to obtain regenerated hydrogen chloride, and the regenerated hydrogen chloride is recovered to the hydrogen chloride to enter the phase inversion step; the saturated sodium chloride aqueous solution having released hydrogen chloride is recovered to saturated chlorinated in sodium solution.
  • the moisture content is negligible, almost non-existent, and the content of organic components is relatively large, so when recovering the first regeneration tail gas, lipophilic ionic liquids, lipophilic ionic liquids are selected
  • the adsorption effect on organic components is stronger than that of hydrophilic ionic liquids.
  • the choice of lipophilic ionic liquids can better purify the first regeneration tail gas. After the first regeneration tail gas is adsorbed and separated by lipophilic ionic liquids, the adsorbed The lipophilic ionic liquid of impurities, and the third tail gas.
  • the third tail gas mainly contains HCl and SO 2 .
  • the third tail gas can be directly separated and treated in the same way as the second tail gas.
  • the third tail gas is adsorbed and filtered by a solid adsorbent to obtain a gaseous mixture.
  • the gaseous mixture is separated and treated, including but not limited to pressurization, adsorption, filtration and pressurized rectification, to obtain gaseous hydrogen chloride and liquid sulfur dioxide; further, gaseous hydrogen chloride is passed into water to obtain hydrochloric acid.
  • Also can adopt following recommended method to carry out separation treatment at first adopt saturated sodium chloride aqueous solution to adsorb the 3rd tail gas, absorb the hydrogen chloride in the 3rd tail gas, because SO 2 is insoluble in saturated sodium chloride aqueous solution, with this HCl and SO 2 is separated to obtain the saturated aqueous sodium chloride solution and the fourth tail gas that have adsorbed hydrogen chloride.
  • the fourth tail gas mainly contains SO 2 . Recycled to the first tail gas that will enter the removal step, and circulated to remove moisture.
  • the saturated sodium chloride aqueous solution that has adsorbed hydrogen chloride is carried out hydrogen chloride regeneration treatment to the saturated aqueous sodium chloride solution that has absorbed hydrogen chloride, promptly makes the saturated aqueous sodium chloride aqueous solution that has adsorbed hydrogen chloride release hydrogen chloride gas, as can make hydrogen chloride gas release by heating, the purity of the hydrogen chloride obtained by regeneration is Very high and can be recycled directly into the hydrogen chloride going to the phase inversion step. And the saturated aqueous sodium chloride solution that will release hydrogen chloride can be reused, promptly reclaimed in the saturated aqueous sodium chloride solution.
  • two types of ionic liquids with hydrophilic and hydrophobic properties are used to jointly treat water and organic matter in the chlorination tail gas, which can achieve a more significant separation effect, and the purity of the obtained HCl and SO Hydrophilic ionic liquids work better.
  • the lipophilic ionic liquid is sent to the ionic liquid regeneration kettle for regeneration, and the regenerated lipophilic ionic liquid is extracted from the bottom of the regeneration kettle, condensed by a condenser, filtered through a filter, and then can be refluxed for repeated use.
  • the lipophilic ionic liquid For the regeneration of the lipophilic ionic liquid, it is to make the lipophilic ionic liquid release the adsorbed gaseous substances.
  • the present application does not limit the regeneration conditions of the lipophilic ionic liquid, any gaseous substance that can make the lipophilic ionic liquid desorbed can be achieved, such as by stirring, heating and other means to achieve the above purpose; in other embodiments of the present application , out of economic considerations, the regeneration temperature of the hydrophilic ionic liquid is 80-120°C, and the regeneration vacuum is -0.1 to -0.05MPa. Under the above conditions, the ionic liquid can quickly remove the adsorbed gaseous substances.
  • tail gas produced during the regeneration of lipophilic ionic liquids it is recorded as the fifth tail gas, and the content is small, which has no recovery value, and can be directly used for solvent recovery treatment.
  • the type of hydrophilic ionic liquid is not limited, and any ionic liquid with a better affinity for water can be used; in other embodiments, the hydrophilic ionic liquid is pyridine bisulfate, One or more of methylimidazole hydrogen sulfate and ethylimidazole hydrogen sulfate.
  • the conditions for the adsorption of the first tail gas by the hydrophilic ionic liquid are not limited, but it is necessary to keep the hydrophilic ionic liquid in the state of an ionic liquid without converting it into Solution state; because the force between the anions and cations of the ionic liquid is the Coulomb force, increasing the temperature will weaken the force between the anions and cations, and the excessively high temperature will easily convert the ionic liquid into a solution. Therefore, in another part of the application In some embodiments, when the hydrophilic ionic liquid is used to adsorb the first tail gas, the temperature may be set at 20-50°C.
  • the type of lipophilic ionic liquid is not limited, and any ionic liquid with good affinity to organic matter can be used; in other embodiments, the lipophilic ionic liquid is 1-ethyl- Dibutyl 3-methylimidazolium phosphate and/or dibutyl 1-butyl-3-methylimidazolium phosphate.
  • the adsorption conditions for the lipophilic ionic liquid to the first regeneration tail gas that is, the conditions for the action of the lipophilic ionic liquid are not limited, but it is necessary to keep the lipophilic ionic liquid in an ionic liquid state; in the present application
  • the temperature may be set at 20-40°C.
  • the present application has designed a tail gas treatment device for the above method, as shown in Figure 2, which shows a schematic structural view of a tail gas treatment device according to an embodiment of the application, as can be seen from Figure 2, the tail gas treatment device 200 mainly includes:
  • the outlet of the cooling tower R-1 is connected to the inlet of the adsorption tower R-2, and the gaseous substance outlet of the adsorption tower R-2 is connected to the filter tank T-1, and the filter tank T-1 is connected to the filter E-3 and the compressor T in turn. -2.
  • the liquid substance outlet of the adsorption tower R-2 is connected to the inlet of the ionic liquid regeneration kettle V-1, and the liquid substance outlet of the ionic liquid regeneration kettle V-1 is connected to the condenser C-1, the filter E-1 and the adsorption tower R-2 Ionic liquid inlet.
  • the outlet of the gaseous substance in the ionic liquid regeneration tank V-1 is connected to the inlet of the dehydration tower R-3.
  • the liquid substance outlet of the dehydration and desolventization tower R-3 is connected to the inlet of the ionic liquid regeneration kettle V-2, and the liquid substance outlet of the ionic liquid regeneration kettle V-2 is connected to the condenser C-2, the filter E-2, and the adsorption tower in turn Ionic liquid inlet for R-2.
  • the gaseous substance outlet of the dehydration and desolventization tower R-3 is connected to the HCl absorption tank V-3, the HCl regeneration tank V-4, and the adsorption tower R-5.
  • the gaseous substance outlet of the pressurized rectification tower R-4 is connected to the inlet of the adsorption tower R-5.
  • the above description is only the main connection relationship of the exhaust gas treatment device 200, the connection relationship of each tank or filter can be adjusted according to the needs, and the type of each tank can be selected according to the respective functional needs.
  • the application is not limited.
  • the desolventization kettle can be an evaporative reactor, and a vacuum pump can be installed if necessary.
  • various kettles or filters in the above-mentioned devices can also be added or deleted as needed.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1 to remove most of DMF, trichloroethane and water.
  • the aqueous solution at the bottom of the cooling tower R-1 is sent to the solvent recovery, and the top of the cooling tower R-1 gets the first
  • the first tail gas enters the dehydration and desolventization tower R-2 to continue processing.
  • the dehydration and desolventization tower R-2 is preset with a hydrophilic ionic liquid, which can basically completely remove the remaining water and most of the solvent in the tail gas. After dehydration and desolventization, the second tail gas is obtained, and the second tail gas enters the next step of solid Sorbent adsorption treatment.
  • the hydrophilic ionic liquid that absorbs water and organic solvents enters the ionic liquid regeneration tank V-1 for dehydration and desolvation regeneration, and the regenerated hydrophilic ionic liquid is cooled by the condenser E-1 and returned to the dehydration and desolventization tower R-2 for continued use , the mixed vapor formed by the released water, HCl, SO 2 and organic solvent enters the dehydration and desolventization tower R-3 for further processing.
  • Activated carbon tank T-1 can be selected for filter tank T-1, and activated carbon tank T-1 is used to absorb the residual solvent in the second tail gas extracted from the top of dehydration and desolventization tower R-2, and then pass through filter E-3, compressor T -2.
  • the filter E-4 After the filter E-4 is processed, it enters the pressurized rectification tower R-4 for separation and treatment, and obtains the high-purity liquid SO at the bottom of the pressurized rectification tower R- 4 product, and the pressurized rectification tower R-4
  • the HCl gas obtained at the top of the tower goes to the water adsorption tower R-5 for adsorption treatment to generate hydrochloric acid.
  • the dehydration and desolventization tower R-3 can basically completely remove the organic matter in the third tail gas evaporated from the regeneration tank V-1, and the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 passes through the regeneration tank V-2 After regeneration, it can be condensed by the condenser E-2, and then returned to the dehydration and desolventization tower R-3 for continued use; the organic matter evaporated from the regeneration kettle V-2 is desolvated and recovered.
  • the mixed steam formed by the water, HCl and SO2 produced from the top of the dehydration and desolventization tower R-3 enters the HCl absorption tank V- 3 containing saturated saline to absorb HCl, and the fourth tail gas containing SO2 and water returns to dehydration and desolventization Tower R-2 is recycled.
  • the saturated brine that has absorbed HCl in the HCl absorption tank V-3 enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the adsorption tower R- together with the HCl gas extracted from the top of the pressurized distillation tower R-4.
  • Adsorption, high-quality hydrochloric acid products can be obtained from the bottom of the adsorption tower R-5, and a small amount of tail gas at the top of the tower can be used for tail gas treatment. According to the comprehensive demand of economy and effect, the above steps need to be added or deleted to achieve the desired effect.
  • the chlorination tail gas is the sucrose-6-ester obtained by esterification of sucrose when the single-group protection method is used to prepare sucralose, and the chlorination reaction occurs with the chlorination reagent , to generate the tail gas produced by sucralose-6-ester, hereinafter referred to as the chlorinated tail gas.
  • the chlorinated tail gas is cooled and condensed by cooling tower R-1, and condensed to 0°C. After condensation, the bottom aqueous solution of cooling tower R-1 is sent to solvent recovery, and the top tail gas of cooling tower R-1, that is, the first tail gas enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 40 ° C, wherein the hydrophilic ionic liquid is 50wt% pyridine hydrogensulfate and 50wt% methylimidazole hydrogensulfate mixture.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 2MPa, the temperature at the bottom of the tower is 0°C, and the temperature at the top of the tower is 10°C. From the bottom of the pressurized rectification tower R-4, high-purity liquid SO 2 is obtained with a purity of 99.9%. ; The HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regeneration kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-ethyl-3-methylimidazole dibutyl phosphate, and the adsorption temperature is 25°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 85°C and the vacuum degree is -0.09MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 34.5%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 30°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 30 ° C, wherein the hydrophilic ionic liquid is 40wt% pyridine hydrogensulfate and 60wt% ethyl imidazole hydrogensulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 100°C and the vacuum degree is -0.07MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 30°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 2.5MPa, the temperature at the bottom of the tower is 5°C, and the temperature at the top of the tower is 15°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4 with a purity of 99.8 %;
  • the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regeneration kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 30°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 95°C and the vacuum degree is -0.07MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 35.8%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 10°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 40°C, wherein the hydrophilic ionic liquid is 20wt% pyridine hydrogensulfate, 30wt% methylimidazole hydrogensulfate and A mixture of 50 wt% ethyl imidazolium bisulfate.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 120°C and the vacuum degree is -0.05MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 20°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 1.5MPa, the temperature at the bottom of the tower is -5°C, and the temperature at the top of the tower is 5°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4. 99.7%; the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-ethyl-3-methylimidazole dibutyl phosphate, and the adsorption temperature is 35°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 80°C and the vacuum degree is -0.10MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO 2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 for further processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 35.6%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by cooling tower R-1, and condensed to 0°C. After condensation, the bottom aqueous solution of cooling tower R-1 is sent to solvent recovery, and the top tail gas of cooling tower R-1, that is, the first tail gas enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 40 ° C, wherein the hydrophilic ionic liquid is 50wt% pyridine hydrogensulfate and 50wt% methylimidazole hydrogensulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 80°C and the vacuum degree is -0.10MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from the The bottom of kettle V-1 is taken out, cooled to 40°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 2MPa, the temperature at the bottom of the tower is 0°C, and the temperature at the top of the tower is 10°C. From the bottom of the pressurized rectification tower R-4, high-purity liquid SO 2 is obtained with a purity of 99.9%. ; The produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-ethyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 20°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 90°C and the vacuum degree is -0.08MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 35.1%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 30°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 30 ° C, wherein the hydrophilic ionic liquid is 40wt% pyridine hydrogensulfate and 60wt% ethyl imidazole hydrogensulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 100°C and the vacuum degree is -0.07MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 30°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 2.5MPa, the temperature at the bottom of the tower is 5°C, and the temperature at the top of the tower is 15°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4 with a purity of 99.8 %;
  • the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 40°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 80°C and the vacuum degree is -0.10MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 37.0%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 10°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with a hydrophilic ionic liquid, and the adsorption temperature is set at 20°C, wherein the hydrophilic ionic liquid is 20wt% pyridine hydrogensulfate, 30wt% methylimidazole hydrogensulfate and A mixture of 50 wt% ethyl imidazolium bisulfate.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 120°C and the vacuum degree is -0.05MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 20°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 1.5MPa, the temperature at the bottom of the tower is -5°C, and the temperature at the top of the tower is 5°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4. 99.9%; the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein,
  • the lipophilic ionic liquid is a mixture of 50 wt% 1-ethyl-3-methylimidazole dibutyl phosphate and 50 wt% 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 30°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 110°C and the vacuum degree is -0.07MPa. It is cooled to 30°C by the condenser E-2, and then returned to the dehydration and desolventization tower R-3 for continued use.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 34.9%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 20°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with a hydrophilic ionic liquid, and the adsorption temperature is set at 50°C, wherein the hydrophilic ionic liquid is 75wt% methylimidazolium hydrogensulfate and 25wt% ethylimidazolium hydrogensulfate salt mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 110°C and the vacuum degree is -0.06MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of the still V-1 is taken out, cooled to 50°C by the condenser E-1, filtered by the filter E-1, and then returned to the dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 1.0MPa, the temperature at the bottom of the tower is -10°C, and the temperature at the top of the tower is 0°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein,
  • the lipophilic ionic liquid is a mixture of 85 wt% 1-ethyl-3-methylimidazole dibutyl phosphate and 15 wt% 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 35°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 110°C and the vacuum degree is -0.07MPa. It is cooled to 30°C by the condenser E-2, and then returned to the dehydration and desolventization tower R-3 for continued use.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 36.1%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 15°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with a hydrophilic ionic liquid, and the adsorption temperature is set at 25°C, wherein the hydrophilic ionic liquid is 15wt% methylimidazolium hydrogensulfate and 85wt% ethylimidazolium hydrogensulfate salt mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 100°C and the vacuum degree is -0.07MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 25°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 3.0MPa, the temperature at the bottom of the tower is 10°C, and the temperature at the top of the tower is 20°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4 with a purity of 99.7 %;
  • the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein,
  • the lipophilic ionic liquid is a mixture of 25 wt% 1-ethyl-3-methylimidazole dibutyl phosphate and 75 wt% 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 25°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 95°C and the vacuum degree is -0.08MPa. Cool down to 25°C through condenser E-2, and then return to dehydration and desolventization tower R-3 for continued use.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 35.5%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 5°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas enters the dehydration process.
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with a hydrophilic ionic liquid, and the adsorption temperature is set to 35 ° C, wherein the hydrophilic ionic liquid is 15wt% pyridine hydrogensulfate and 85wt% ethyl imidazole hydrogensulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 105°C and the vacuum degree is -0.07MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from the The bottom of kettle V-1 is taken out, cooled to 35°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 2.5MPa, the temperature at the bottom of the tower is 5°C, and the temperature at the top of the tower is 15°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4 with a purity of 99.9 %;
  • the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-ethyl-3-methylimidazole dibutyl phosphate, and the adsorption temperature is 35°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 85°C and the vacuum degree is -0.09MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 36.5%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by cooling tower R-1, and condensed to 25°C. After condensation, the aqueous solution at the bottom of cooling tower R-1 is sent to solvent recovery, and the top tail gas of cooling tower R-1, that is, the first tail gas enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 45°C, wherein the hydrophilic ionic liquid is 35wt% pyrolinate hydrogen salt and 65wt% methylimidazole hydrogen sulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 115°C and the vacuum degree is -0.06MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from The bottom of kettle V-1 is taken out, cooled to 45°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 1.5MPa, the temperature at the bottom of the tower is -5°C, and the temperature at the top of the tower is 5°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4. 99.7%; the produced HCl gas obtained from the top of the pressurized rectification tower R-4 enters the water adsorption tower R-5 for adsorption treatment.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-butyl-3-methylimidazolium dibutyl phosphate, and the adsorption temperature is 20°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 115°C and the vacuum degree is -0.06MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 35.5%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is cooled and condensed by the cooling tower R-1, and condensed to 35°C. After condensation, the aqueous solution at the bottom of the cooling tower R-1 is sent to solvent recovery, and the top tail gas of the cooling tower R-1, that is, the first tail gas, enters dehydration
  • the desolventization tower R-2 continues to process.
  • the first tail gas enters the dehydration and desolventization tower R-2 preset with hydrophilic ionic liquid, and the adsorption temperature is set to 35°C, wherein the hydrophilic ionic liquid is 75wt% pyrolinate hydrogen salt and 25wt% ethyl imidazole hydrogen sulfate mixture.
  • the used hydrophilic ionic liquid at the bottom of the dehydration and desolventization tower R-2 enters the ionic liquid regeneration tank V-1 for regeneration treatment.
  • the regeneration temperature is 85°C and the vacuum degree is -0.09MPa.
  • the regenerated hydrophilic ionic liquid is regenerated from the The bottom of kettle V-1 is taken out, cooled to 35°C by condenser E-1, filtered by filter E-1, and then returned to dehydration and desolventization tower R-2 for continued use.
  • the second tail gas extracted from the top of the dehydration and desolventization tower R-2 is absorbed by the activated carbon tank T-1 to absorb the residual organic gas, and then it is treated by the filter E-3, the compressor T-2, and the filter E-4, and then enters the Pressurized rectification tower R-4, the pressure of the pressurized rectification tower is 1.0MPa, the temperature at the bottom of the tower is -10°C, and the temperature at the top of the tower is 0°C.
  • High-purity liquid SO 2 is obtained from the bottom of the pressurized rectification tower R-4.
  • the water, organic solvent, and a small amount of HCl and SO evaporated from the top of the regenerative kettle V- 1 of the hydrophilic ionic liquid
  • the third tail gas formed enters the dehydration and desolventization tower R-3 preset with the lipophilic ionic liquid, wherein, The lipophilic ionic liquid is 1-ethyl-3-methylimidazole dibutyl phosphate, and the adsorption temperature is 25°C.
  • the lipophilic ionic liquid extracted from the bottom of the dehydration and desolventization tower R-3 enters the regeneration tank V-2 of the lipophilic ionic liquid for regeneration.
  • the regeneration temperature is 105°C and the vacuum degree is -0.07MPa.
  • the mixed gas formed by the water, HCl and SO2 produced at the top of the dehydration and desolventization tower R-3 is recorded as the fourth tail gas, and the fourth tail gas enters the HCl absorption tank V-3 containing saturated sodium chloride aqueous solution to absorb HCl gas, Normal temperature adsorption.
  • the mixed gas containing SO2 and water extracted from the top of the tank is recorded as the fifth tail gas, and the fifth tail gas is returned to the dehydration and desolventization tower R-2 to continue processing, and the saturated salt containing HCl extracted from the bottom of the absorption tank V-3
  • the water enters the HCl regeneration tank V-4, and the regenerated HCl water vapor enters the water adsorption tower R-5 for adsorption together with the HCl gas extracted from the top of the pressurized distillation tower R-4, and high-quality HCl gas can be obtained from the bottom of the tower.
  • Hydrochloric acid product with a purity of 36.5%, and a small amount of tail gas at the top of the tower for tail gas treatment.
  • the saturated brine produced by the regeneration tank V-4 is returned to the HCl absorption tank V-3 for continued use after adding some pure water.
  • the chlorinated tail gas is condensed by the condensation tower, the condensation temperature is 20°C, most of the organic solvents are removed, and then dehydrated by concentrated sulfuric acid, the water content is less than 0.01%, and then the gas is adsorbed by activated carbon, and the gas is compressed by the compressor before entering the processing Separation in a pressure rectification tower, the pressure of the pressure rectification tower is 1.0MPa, the temperature at the bottom of the tower is -10°C, and the temperature at the top of the tower is 0°C, and liquid SO 2 is obtained from the bottom of the pressure rectification tower R-4 with a purity of 98.5%.
  • the organic matter content is 1.3%; the HCl gas at the top of the tower enters the water adsorption tower for adsorption, and the hydrochloric acid product is obtained at the bottom of the tower with a purity of 35.1%, and the trace gas at the top of the tower is used for tail gas treatment.
  • this application utilizes ionic liquids to adsorb impurities in the chlorinated tail gas, and before the pressurized rectification, it effectively solves the impact of water and organic matter on the separation of HCl and SO 2 gases, and solves the problem of separation due to pressure.
  • This application is mainly based on ionic liquids, and organically combined with condensation, rectification and other means, which can effectively treat the chlorinated tail gas in the sucralose production process, realize the effective separation of HCl and SO2, and obtain high - quality hydrochloric acid And liquid SO 2 products, and the overall treatment process is simple, low cost, and has great economic and application value.
  • connection should be understood in a broad sense, for example, it can be a fixed connection or a detachable connection. Connected, or integrally connected; it can be mechanically connected or electrically connected; it can be directly connected or indirectly connected through an intermediary, and it can be the internal communication of two components. Those of ordinary skill in the art can understand the specific meanings of the above terms in this application in specific situations.

Abstract

本申请提供了一种尾气处理方法，所述尾气为蔗糖-6-酯经氯化反应生成三氯蔗糖-6-酯的过程中产生的，该方法包括：将尾气进行降温冷凝，以除去部分有机溶剂和水，得到第一溶液和第一尾气；采用亲水离子液体对第一尾气进行吸附、分离，以除去其中的大部分水和有机溶剂，得到第二尾气；将第二尾气采用固体吸附剂进行吸附、过滤，得到气态混合物，对气态混合物进行分离处理，得到气态氯化氢和液态二氧化硫；和将气态氯化氢通入水中，得到盐酸。本申请以离子液体吸附为主，与冷凝、精馏等手段有机结合，能够有效处理三氯蔗糖生产工艺中的氯化尾气，实现HCl和SO 2两种气体的有效分离，获得高品质的盐酸和液态SO 2产品，工艺简单、成本低。

Description

尾气处理方法 技术领域
本发明属于化工尾气分离回收工业技术领域，具体涉及一种尾气处理方法。
发明背景
三氯蔗糖-6-酯是制备三氯蔗糖中重要的中间体之一，蔗糖-6-酯可由蔗糖经酯化，然后经氯代试剂氯化得来，目前，工业化的氯化试剂主要有维尔斯迈尔(Vilsmeier)氯代试剂及光气类产品，由于光气的高风险，高污染性，使用的企业较少。而Vilsmeier氯代试剂主要由DMF，二甲基亚砜制备而来，使用时较为安全。然而在氯化过程中，会产生大量尾气，其中包含HCl、SO 2、水、DMF及三氯乙烷等。
传统的对上述尾气的处理通常采用降温冷凝、硫酸脱水、活性炭吸附等操作，但是这不足以去除尾气中的全部有机物及水，一方面导致在后续加压精馏过程中，会产生大量的有机/无机固体附着在管壁、输送泵等过流材质表面，造成严重的设备腐蚀及堵塞，极大地限制了HCl和SO 2的回收；另一方面HCl和SO 2得不到彻底的分离，如采用直接水吸附HCl得到的盐酸中含有大量SO 2气体，SO 2气体在水中会形成H 2SO 3，由于H 2SO 3受热易分解，产生大量SO 2气体，导致回收的盐酸产品在使用过程中与碱接触会产生气体乳化现象，严重影响盐酸产品的品质。
目前也有一些区别于传统技术的关于含有HCl和SO 2混合气体的尾气处理的报道，如中国专利CN103113197报道了一种以氯化尾气为原料，与醇、乙腈反应制备原乙酸三甲酯的方法，该法虽解决了HCl的处理问题，并为蔗糖酯化提供了原料；但原乙酸三甲酯酯化工艺目前已很少采用，且该工艺容易产生大量废盐、废水，因此该方法不具有很大的实用价值。
中国专利CN208511908采用低温冷凝的方式分离HCl和SO 2混合气体，其方法是利用两者沸点不同，且在SO 2产品中鼓入空气，带出HCl，从而提高SO 2产品纯度。该法单纯以两种气体的沸点不同，进行分离，但在能耗上较其他方法高很多，且得到的产品纯度不佳；此外，对于三氯蔗糖工艺中产生的氯化尾气在含水、含溶剂的情况下，该工艺并不适用。
中国专利CN108373139在针对三氯蔗糖氯化尾气除水、除溶剂的基础上，同样采用了冷却分离的方法分离HCl和SO 2。该方法使用了浓硫酸除水，除水效果较佳，但后续废酸再生或处理较为麻烦；有机物分离过程中单纯以冷凝的方式收集， 无法实现为其中有机物的完全去除，因此得到的HCl及SO 2产品纯度不高。
又如中国专利CN103466550报道了一种阿莫西林生产工艺中D-酸酯化尾气回收系统，尾气系统中主要为HCl及SO 2气体。该法采用加压精馏的方式分离两种气体，并采用三联加压精馏塔分离气体及有机物；然而该体系中不含水分，因此对于系统设备的要求相对不高；但蔗糖氯化反应中会产生较多的水分，对系统的分离方法及设备具有极大的考验，该方法不适宜用于对蔗糖氯化反应产生的废气中。
发明内容
鉴于目前蔗糖采用Vilsmeier氯代试剂氯化生成三氯蔗糖-6-酯工艺产生的尾气的处理现状，存在着分离效果差、后处理困难、容易造成严重的设备腐蚀，以及压缩气体形成固体附着物导致管路堵塞等问题，提出了一种尾气处理方法，可克服上述问题或者至少部分地解决上述问题。
根据本申请的第一方面，提供了一种尾气处理方法，该尾气为蔗糖-6-酯经氯化反应生成三氯蔗糖-6-酯的过程中产生的，该方法包括：
冷凝步骤：将尾气进行降温冷凝，以除去部分有机溶剂和部分水，得到第一溶液和第一尾气；
脱除步骤：采用亲水离子液体对第一尾气进行吸附、分离，以除去其中的大部分水和部分有机溶剂，得到第二尾气；
分离步骤：将第二尾气采用固体吸附剂进行吸附、过滤，得到气态混合物，对气态混合物进行分离处理，得到气态氯化氢和液态二氧化硫；和
相转化步骤：将气态氯化氢通入水中，得到盐酸。
可选的，该方法还包括：
在所述脱除步骤内包括的第一再生步骤：将脱除步骤中使用后的亲水离子液体进行再生处理，得到再生亲水离子液体和第一再生尾气；以及
将再生亲水离子液体回收，以供脱除步骤使用。
可选的，在上述方法中，亲水离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa。
可选的，该方法还包括：
在所述第一再生步骤后的回收步骤：采用亲油离子液体对第一再生尾气进行吸附，以脱除有机组分，得到第三尾气；
采用饱和氯化钠水溶液对第三尾气进行吸附，以吸收氯化氢，得到第四尾气；
将第四尾气回收至要进入脱除步骤的第一尾气中；
对得到的吸附了氯化氢的饱和氯化钠水溶液进行氯化氢再生处理，得到再生氯化氢，将再生氯化氢回收至要进入相转化步骤的氯化氢中；将释放了氯化氢的饱和氯化钠水溶液回收至饱和氯化钠水溶液中。
可选的，该方法还包括：
在所述回收步骤后的第二再生步骤：将回收步骤中使用后的亲油离子液体进行再生处理，得到再生亲油离子液体和第五尾气；
将再生亲油离子液体回收，以供回收步骤使用；
对第五尾气进行溶剂回收处理。
可选的，在上述方法中，亲油离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa。
可选的，在上述方法中，在回收步骤中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯和/或1-丁基-3-甲基咪唑磷酸二丁酯；
采用亲油离子液体对第一再生尾气进行吸附包括：
在温度为20～40℃，采用亲油离子液体对第一再生尾气进行吸附。
可选的，在上述方法中，在冷凝步骤中，降温冷凝的温度设为0～30℃。
可选的，在上述方法中，亲水离子液体为吡啶硫酸氢盐、甲基咪唑硫酸氢盐和乙基咪唑硫酸氢盐中的一种或几种。
可选的，在上述方法中，采用亲水离子液体对第一尾气进行吸附包括：
在温度为20～50℃，采用亲水离子液体对第一尾气进行吸附。
本申请的有益效果在于，利用离子液体吸附氯化尾气中的杂质，在加压精馏前，有效解决了水及有机物对HCl和SO 2两种气体分离的影响，解决了因加压分离过程中产生的有机/无机固体附着在管壁及输送泵造成的严重腐蚀及堵塞问题，且可获得高纯度的液体SO 2产品；离子液体的腐蚀性极低，采用离子液体代替浓硫酸，可有效克服传统技术中浓硫酸脱水带来的设备腐蚀及后续处理问题；此外，离子液体具有高度可再生性，且再生工艺简单，极大程度上降低了尾气处理的成本。本申请以离子液体吸附为主，并且与冷凝、精馏等手段有机结合，能够有效处理三氯蔗糖生产工艺中的氯化尾气，实现HCl和SO 2两种气体的有效分离，获得高品质的盐酸和液态SO 2产品，且整体处理工艺简单、成本低、具有极大的经济和应用价值。
上述说明仅是本申请技术方案的概述，为了能够更清楚了解本申请的技术手段，而可依照说明书的内容予以实施，并且为了让本申请的上述和其它目的、特征 和优点能够更明显易懂，以下特举本申请的具体实施方式。
附图简要说明
通过阅读下文优选实施方式的详细描述，各种其他的优点和益处对于本领域普通技术人员将变得清楚明了。附图仅用于示出优选实施方式的目的，而并不认为是对本申请的限制。而且在整个附图中，用相同的参考符号表示相同的部件。在附图中：
图1示出了根据本申请的一个实施例的尾气处理方法的流程示意图；
图2示出了根据本申请的一个实施例的尾气处理装置的结构示意图。
实施本发明的方式
下面将更详细地描述本申请的示例性实施例。虽然显示了本申请的示例性实施例，然而应当理解，可以以各种形式实现本申请而不应被这里阐述的实施例所限制。相反，提供这些实施例是为了能够更透彻地理解本申请，并且能够将本申请的范围完整地传达给本领域的技术人员。
离子液体又称室温离子液体(Room Temperature Ionic Liquids，简称RTILs)，是一种备受关注的绿色溶剂和催化剂。它是一种熔点低于100℃的液态有机熔融盐，由于其完全由阴阳离子组成，因此具有许多不同于常规有机溶剂的性质，如“零”蒸汽压、热稳定性高，溶解能力强及结构与功能可设计等，在有机反应、液相分离、气体吸收、电化学等领域具有极大的应用潜力。
现有技术中，对蔗糖采用Vilsmeier氯代试剂氯化生成三氯蔗糖-6-酯工艺产生的尾气，简称氯化尾气的处理，存在着分离效果差、容易造成严重的设备腐蚀，以及压缩气体形成固体附着物导致管路堵塞等问题。
本申请将离子液体引入至氯化尾气的处理中，通过离子液体吸附尾气中的水分和有机杂质，并结合冷凝和加压精馏等技术，有效克服了现有技术的不足。
图1示出了根据本申请的一个实施例的尾气处理方法的流程示意图，从图1可以看出，本申请至少包括步骤S110～步骤S140：
冷凝步骤S110：将尾气进行降温冷凝，以除去部分有机溶剂和水，得到第一溶液和第一尾气。
本申请的尾气指的是蔗糖-6酯与氯代试剂，如Vilsmeier试剂等，进行氯化反应，生成三氯蔗糖-6-酯的氯化工艺中产生的，主要含有气态水、HCl、SO 2、以及 DMF和三氯乙烷等有机溶剂。目前对上述尾气的处理，主流技术通常采用降温冷凝-浓硫酸脱水-活性炭脱溶-加压精馏分离的传统工艺，这种工艺存在着如下的技术缺陷：采用浓硫酸脱水的方式容易导致严重的设备腐蚀，且容易使溶剂碳化，浓硫酸吸水后不易再生；传统的冷凝加活性炭吸附，无法对气体中含有的较高浓度有机物完全去除，这会导致后续压缩过程中有机物富集，在HCl及SO 2存在的情况下与固体微颗粒一起附着在管壁或阀门处，堵塞管路等。
在本申请中，首先，将上述尾气进行降温冷凝，在这个过程中，大部分气态水会转化为液态水、气态DMF和气态三氯乙烷等气态有机溶剂会转化为液态，记为第一溶液，与气态混合物分流，气态混合物记为第一尾气。
在降温冷凝后，第一溶液中主要包含液态的水、DMF和三氯乙烷，第一溶液可做溶剂回收处理。第一尾气包含气态氯化氢、SO 2、以及部分气态水、少量的气态DMF和气态三氯乙烷。
在本申请的一些实施例中，在冷凝步骤中，对降温冷凝降至的温度不作限定，低于蔗糖-6酯与氯代试剂的氯代反应的温度即可；在另一些实施例中，出于经济和效果的综合考虑，可将降温冷凝的温度设为0～30℃。
脱除步骤S120：采用亲水离子液体对第一尾气进行吸附，以除去其中的大部分水和有机溶剂，得到第二尾气；
在冷凝步骤中，有机溶剂的含量已经被降至很低，含量是非常少的，水分含量相对较多，该步骤选择亲水离子液体对第一尾气进行吸附，这是由于亲水离子液体对水分有很强的吸附作用，同时对有机溶剂也有一定的吸附效果，在采用亲水离子液体对第一尾气进行吸附后，水分基本被消除殆尽，且有机溶剂的含量也是非常低的。
气态HCl和气态SO 2在离子液体中的溶解度是很低的，因此，采用离子液体对尾气进行吸附，可有效分离水、有机溶剂和HCl、SO 2。
分离步骤S130：将第二尾气采用固体吸附剂进行吸附、过滤，得到第一气态混合物，对第一气态混合物进行分离处理，得到气态氯化氢和液态二氧化硫。
为了进一步除去尾气中的有机溶剂，可以采用固体吸附剂，如活性炭等，吸附第二尾气中的残余溶剂，然后过滤掉固体吸附剂，得到了气态混合物，这时的气态混合物主要包括气态HCl和气态SO 2，还包括极其微量的水蒸气和气态有机溶剂。
然后对第一气态混合物进行分离，即可得到分离后的气态HCl和液态SO 2，具体的分离过程可参考现有技术，也可以采用加压、吸附、过滤和加压精馏的方法， 首先对第一气态混合物进行加压，然后再次采用固体吸附剂再次对残余有机溶剂进行吸附，最后利用气态HCl和气态SO 2在挥发度的差异，采用加压精馏技术对气态混合物进行分离处理，在加压的过程中，气态SO 2转化为液态SO 2，从而使得气态HCl和气态SO 2互相分离，在分离后，获得气态HCl和液态SO 2。
和相转化步骤S140：将气态氯化氢通入水中，得到盐酸。
气态氯化氢不容易存储，且在实际应用中，盐酸是比较常用的化学试剂，因此，出于经济的考虑，将气态氯化氢转化为液态产物，即盐酸，具体地，将气态氯化氢通入水中，即可得到盐酸。
从图1所示的方法中，可以看出，本申请利用离子液体吸附氯化尾气中的杂质，在加压精馏前，有效解决了水及有机物对HCl和SO 2两种气体分离的影响，解决了因加压分离过程中产生的有机/无机固体附着在管壁及输送泵造成的严重腐蚀及堵塞问题，且可获得高纯度的液体SO 2产品；离子液体的腐蚀性极低，采用离子液体代替浓硫酸，可有效克服传统技术中浓硫酸脱水带来的设备腐蚀及后续处理问题；此外，离子液体具有可高再生性，且再生工艺简单，极大程度上降低了尾气处理的成本。本申请以离子液体为主，并且与冷凝、精馏等手段有机结合，能够有效处理三氯蔗糖生产工艺中的氯化尾气，实现HCl和SO 2两种气体的有效分离，获得高品质的盐酸和液态SO 2产品，且整体处理工艺简单、成本低、具有极大的经济和应用价值。
在本申请的一些实施例中，上述方法还包括：在所述脱除步骤内包括的第一再生步骤：将脱除步骤中使用后的亲水离子液体进行再生处理，得到再生亲水离子液体和第一再生尾气；以及将再生亲水离子液体回收至脱除步骤中。
在脱除步骤中，采用亲水离子液体对第一尾气进行吸附后并分离后，得到第二尾气，以及吸附了杂质的亲水离子液体，即使用后的亲水离子液体，由于亲水离子液体再生能力强、再生工艺简单、再生成本低，因此可将亲水离子液体进行再生处理，循环利用，这能够极大程度节约氯化尾气的处理成本。
对于亲水离子液体的再生可采用下述方法：将亲水离子液体送入离子液体再生釜进行再生，再生后的亲水离子液体从再生釜的釜底采出，经冷凝器冷凝后、在经过过滤器过滤，然后就能够回流反复使用。
对于离子液体的再生，就是使得离子液体释放出已经吸附的气态物质。本申请对亲水离子液体的再生条件不做限制，凡是能够使得离子液体脱除吸附的气态物质即可，如通过搅拌、加热等手段实现上述目的；在本申请的另一些实施例中，出于 经济的考虑，亲水离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa，在上述条件下，亲水离子液体能够迅速脱除吸附的气态物质。
需要说明的是，亲水离子液体在对第一尾气进行吸附的过程中，不仅会吸附尾气中的水分、有机溶剂，一部分目标产物HCl和SO 2两种气体也会随着亲水离子液体一起被带出第一尾气，因此在亲水离子液体进行再生时，产生的第一再生尾气中，除了包含杂质水分、DMF和三氯乙烷等有机溶剂，还会包含一些目标产物HCl和SO 2。为了进一步提高HCl和SO 2的产率，可对第一再生尾气进行回收再处理，以便分离出其中的HCl和SO 2。
在本申请的一些实施例中，上述方法还包括：在所述第一再生步骤后的回收步骤：采用亲油离子液体对第一再生尾气进行吸附，以脱除有机组分，得到第三尾气；采用饱和氯化钠水溶液对第三尾气进行吸附，以吸收氯化氢，得到第四尾气；将第四尾气回收至要进入脱除步骤的第一尾气中。对得到的吸附了氯化氢的饱和氯化钠水溶液进行氯化氢再生处理，得到再生氯化氢，将再生氯化氢回收至要进入相转化步骤的氯化氢中；将释放了氯化氢的饱和氯化钠水溶液回收至饱和氯化钠水溶液中。
在第一再生尾气中，水分的含量是微乎其微的，几乎没有，而有机组分的含量相对较多，因此在对第一再生尾气进行回收时，选择了亲油性的离子液体，亲油离子液体对于有机组分的吸附效果强于亲水离子液体，这里选择亲油离子液体能够更好地纯化第一再生尾气，在采用亲油离子液体对第一再生尾气进行吸附、分离后，得到吸附了杂质的亲油离子液体，以及第三尾气。
在第三尾气中主要包含HCl和SO 2，对于第三尾气可以同对第二尾气的处理方法一致，直接进行分离处理，如将第三尾气采用固体吸附剂进行吸附、过滤，得到气态混合物，对气态混合物进行分离处理，包括但不限于加压、吸附、过滤以及加压精馏，即可得到气态氯化氢和液态二氧化硫；进一步的，将气态氯化氢通入水中，得到盐酸。
也可以采用下述推荐的方法进行分离处理，首先采用饱和氯化钠水溶液对第三尾气进行吸附，吸收第三尾气中的氯化氢，由于SO 2不溶于饱和氯化钠水溶液，以此HCl和SO 2得以分离，得到吸附了氯化氢的饱和氯化钠水溶液和第四尾气，第四尾气主要包含SO 2，由于SO 2从饱和氯化钠水溶液中析出，会带上水分，因此可将第四尾气回收至要进入脱除步骤的第一尾气中，循环处理，以脱除水分。对得到的吸附了氯化氢的饱和氯化钠水溶液进行氯化氢再生处理，即使得吸附了氯化氢的饱 和氯化钠水溶液释放出氯化氢气体，如可通过加热使得氯化氢气体释放，将再生得到的氯化氢的纯度是非常高的，可直接回收至要进入相转化步骤的氯化氢中。而对于将释放了氯化氢的饱和氯化钠水溶液可以重复利用，即回收至饱和氯化钠水溶液中。
在本实施例中，利用了具有亲水与疏水性的两类离子液体配合处理氯化尾气中的水及有机物，能够达到更加显著的分离效果，在得到的HCl和SO 2的纯度较单纯使用亲水离子液体效果更好。
同亲水离子液体一样，在本申请的一些实施例中，也可以对回收步骤中，使用后的亲油离子液体进行再生处理，以循环使用，具体的，同亲水离子液体，将亲油离子液体送入离子液体再生釜进行再生，再生后的亲油离子液体从再生釜的釜底采出，经冷凝器冷凝后、在经过过滤器过滤，然后就能够回流反复使用。
对于亲油离子液体的再生，就是使得亲油离子液体释放出已经吸附的气态物质。本申请对亲油离子液体的再生条件不做限制，凡是能够使得亲油离子液体脱除吸附的气态物质即可，如通过搅拌、加热等手段实现上述目；在本申请的另一些实施例中，出于经济的考虑，亲水离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa，在上述条件下，离子液体能够迅速脱除吸附的气态物质。
对于亲油离子液体再生过程中，产生的少量尾气，记为第五尾气，含量较少，已经没有回收价值，可直接做溶剂回收处理。
亲水液体离子的种类
在本申请的一些实施例中，对亲水离子液体的种类不作限制，对水有较好亲和性的离子液体均可；在另一些实施例中，亲水离子液体为吡啶硫酸氢盐、甲基咪唑硫酸氢盐和乙基咪唑硫酸氢盐中的一种和几种。
亲水液体离子作用条件
在本申请的一些实施例中，对于亲水离子液体对第一尾气进行吸附条件，即亲水离子液体的作用条件不作限制，但需要保持亲水离子液体为离子液体状态，而不会转化为溶液状态；由于离子液体的阴阳离子之间的力为库伦作用力，升高温度会使得阴阳离子之间的作用力减弱，过高温度容易使得离子液体转化为溶液，因此，在本申请的另一些实施例中，在采用亲水离子液体在对第一尾气进行吸附时，温度可设为20～50℃。
亲油液体离子的种类
在本申请的一些实施例中，对亲油离子液体的种类不作限制，对有机物有较好 亲和性的离子液体均可；在另一些实施例中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯和/或1-丁基-3-甲基咪唑磷酸二丁酯。
亲油液体离子作用条件
在本申请的一些实施例中，对于亲油离子液体对第一再生尾气进行吸附条件，即亲油离子液体的作用条件不作限制，但需要保持亲油离子液体为离子液体状态；在本申请的另一些实施例中，在采用亲油离子液体在对第一再生尾气进行吸附时，温度可设为20～40℃。
本申请针对上述方法，设计了尾气处理装置，如图2所示，图2示出了根据本申请的一个实施例的尾气处理装置的结构示意图，从图2可以看出，该尾气处理装置200主要包括：
冷却塔R-1、吸附塔R-2、脱水脱溶塔R-3、加压精馏塔R-4、吸附塔R-5、过滤器(E-1，E-2，E-3，E-4)、离子液体再生釜V-1、离子液体再生釜V-2、HCl吸收釜V-3、HCl再生釜V-4、过滤罐T-1、压缩机T-2、以及冷凝器(C-1，C-2，C-3)。
其中，冷却塔R-1的出口连接吸附塔R-2的入口，吸附塔R-2的气态物质出口连接过滤罐T-1、过滤罐T-1依次连接过滤器E-3、压缩机T-2、过滤器E-4和加压精馏塔R-4。吸附塔R-2的液态物质出口连接离子液体再生釜V-1的入口，离子液体再生釜V-1的液体物质出口连接冷凝器C-1、过滤器E-1和吸附塔R-2的离子液体入口。离子液体再生釜V-1的气态物质的出口连接脱水脱溶塔R-3的入口。脱水脱溶塔R-3的液态物质出口连接离子液体再生釜V-2的入口，离子液体再生釜V-2的液态物质出口依次连接冷凝器C-2、过滤器E-2、以及吸附塔R-2的离子液体入口。脱水脱溶塔R-3的气态物质出口连接HCl吸收釜V-3、HCl再生釜V-4、以及吸附塔R-5。加压精馏塔R-4的气态物质出口连接吸附塔R-5的入口。
需要说明的是，上述描述仅是尾气处理装置200的主要连接关系，各个釜或者过滤器等的连接关系可以根据需要进行适应性调整，且各个釜的类型可以根据各自的功能需要进行选择，本申请不作限制，如脱溶釜可以选择蒸发型的反应釜，必要时可以设置真空泵；另外，也可以根据需要对上述装置中的各个釜或者过滤器等根据需要进行增加或删减。
采用上述尾气处理装置200实施尾气处理方法的过程可简述如下：
氯化尾气经冷却塔R-1降温冷凝，去除大部分DMF、三氯乙烷和水，此时冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶得到第一尾气，第一尾气进入脱水脱溶塔R-2继续处理。
脱水脱溶塔R-2中预置有亲水离子液体，可基本完全脱除尾气中剩余的水分，以及大部分溶剂，经脱水脱溶后，得到第二尾气，第二尾气进入下一步固体吸附剂吸附处理。而吸附水分和有机溶剂的亲水离子液体进入离子液体再生釜V-1脱水脱溶再生，再生后的亲水离子液体经冷凝器E-1冷却后，返回脱水脱溶塔R-2继续使用，脱出的水、HCl、SO 2及有机溶剂形成的混合蒸气进入脱水脱溶塔R-3继续处理。
过滤罐T-1可选用活性炭罐T-1，采用活性炭罐T-1吸附脱水脱溶塔R-2塔顶采出的第二尾气中的残余溶剂，再经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4分离处理，得到加压精馏塔R-4的塔底高纯液体SO 2产品，加压精馏塔R-4的塔顶得到的HCl气体去水吸附塔R-5吸附处理，生成盐酸。
脱水脱溶塔R-3可基本完全脱除再生釜V-1蒸发出的第三尾气中的有机物，脱水脱溶塔R-3的塔底采出的亲油离子液体经再生釜V-2再生后，再经冷凝器E-2冷凝，即可返回脱水脱溶塔R-3继续使用；再生釜V-2蒸出的有机物去溶剂回收。
脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合蒸气进入含有饱和食盐水的HCl吸收釜V-3吸收HCl，含有SO 2和水的第四尾气返回脱水脱溶塔R-2循环处理。
HCl吸收釜V-3的吸附了HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入吸附塔R-5吸附，即可从吸附塔R-5的塔底获得品质较高的盐酸产品，塔顶微量尾气去做尾气处理。可根据经济和效果的综合需求，需要对上述步骤进行增加或删减，以达到预期效果。
氯化尾气的来源
在本申请的下述各实施例和对比例中，氯化尾气是采用单基团保护法制备三氯蔗糖时，蔗糖经过酯化得到的蔗糖-6-酯，与氯代试剂发生氯化反应，生成三氯蔗糖-6-酯产的尾气，下称氯化尾气。
实施例1
氯化尾气经冷却塔R-1降温冷凝，冷凝至0℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为40℃，其中，亲水离子液体为50wt％吡啶硫酸氢盐和50wt％甲基咪唑硫酸氢盐的混合物。脱水脱 溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为2MPa，塔底温度0℃，塔顶温度10℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.9％；从加压精馏塔R-4的塔顶得到的HCl气体进入水吸附塔R-5吸附。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl、SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯，吸附温度为25℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为85℃，真空度-0.09MPa，再经冷凝器E-2冷却至25℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度34.5％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例2
氯化尾气经冷却塔R-1降温冷凝，冷凝至30℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为30℃，其中，亲水离子液体为40wt％吡啶硫酸氢盐和60wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为100℃，真空度-0.07MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至30℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为2.5MPa，塔底温度5℃，塔顶温度15℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.8％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl、SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-丁基-3-甲基咪唑磷酸二丁酯，吸附温度为30℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为95℃，真空度-0.07MPa，再经冷凝器E-2冷却至30℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度35.8％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例3
氯化尾气经冷却塔R-1降温冷凝，冷凝至10℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为40℃，其中，亲水离子液体为20wt％吡啶硫酸氢盐、30wt％甲基咪唑硫酸氢盐和50wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为120℃，真空度-0.05MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至20℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为1.5MPa，塔底温度-5℃，塔顶温度5℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.7％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯，吸附温度为35℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为80℃，真空度-0.10MPa，再经冷凝器E-2冷却至25℃，然后返回脱水脱溶塔R-3继续使用。 脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2、水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度35.6％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例4
氯化尾气经冷却塔R-1降温冷凝，冷凝至0℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为40℃，其中，亲水离子液体为50wt％吡啶硫酸氢盐和50wt％甲基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为80℃，真空度-0.10MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至40℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为2MPa，塔底温度0℃，塔顶温度10℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.9％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯，吸附温度为20℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为90℃，真空度-0.08MPa，再经冷凝器E-2冷却至20℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入 水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度35.1％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例5
氯化尾气经冷却塔R-1降温冷凝，冷凝至30℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为30℃，其中，亲水离子液体为40wt％吡啶硫酸氢盐和60wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为100℃，真空度-0.07MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至30℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为2.5MPa，塔底温度5℃，塔顶温度15℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.8％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-丁基-3-甲基咪唑磷酸二丁酯，吸附温度为40℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为80℃，真空度-0.10MPa，再经冷凝器E-2冷却至40℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度37.0％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例6
氯化尾气经冷却塔R-1降温冷凝，冷凝至10℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为20℃，其中，亲水离子液体为20wt％吡啶硫酸氢盐、30wt％甲基咪唑硫酸氢盐和50wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为120℃，真空度-0.05MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至20℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为1.5MPa，塔底温度-5℃，塔顶温度5℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.9％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为50wt％1-乙基-3-甲基咪唑磷酸二丁酯和50wt％1-丁基-3-甲基咪唑磷酸二丁酯的混合物，吸附温度为30℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为110℃，真空度-0.07MPa，再经冷凝器E-2冷却至30℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度34.9％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例7
氯化尾气经冷却塔R-1降温冷凝，冷凝至20℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继 续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为50℃，其中，亲水离子液体为75wt％甲基咪唑硫酸氢盐和25wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为110℃，真空度-0.06MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至50℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为1.0MPa，塔底温度-10℃，塔顶温度0℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.8％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为85wt％1-乙基-3-甲基咪唑磷酸二丁酯和15wt％1-丁基-3-甲基咪唑磷酸二丁酯的混合物，吸附温度为35℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为110℃，真空度-0.07MPa，再经冷凝器E-2冷却至30℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度36.1％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例8
氯化尾气经冷却塔R-1降温冷凝，冷凝至15℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为25℃，其中，亲水离子液体为15wt％甲基咪唑硫酸氢盐和85wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行 再生处理，再生温度为100℃，真空度-0.07MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至25℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为3.0MPa，塔底温度10℃，塔顶温度20℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.7％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为25wt％1-乙基-3-甲基咪唑磷酸二丁酯和75wt％1-丁基-3-甲基咪唑磷酸二丁酯的混合物，吸附温度为25℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为95℃，真空度-0.08MPa，再经冷凝器E-2冷却至25℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度35.5％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例9
氯化尾气经冷却塔R-1降温冷凝，冷凝至5℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为35℃，其中，亲水离子液体为15wt％吡啶硫酸氢盐和85wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为105℃，真空度-0.07MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至35℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏 塔R-4，加压精馏塔压力为2.5MPa，塔底温度5℃，塔顶温度15℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.9％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯，吸附温度为35℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为85℃，真空度-0.09MPa，再经冷凝器E-2冷却至35℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度36.5％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例10
氯化尾气经冷却塔R-1降温冷凝，冷凝至25℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为45℃，其中，亲水离子液体为35wt％吡啶酸氢盐和65wt％甲基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为115℃，真空度-0.06MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至45℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为1.5MPa，塔底温度-5℃，塔顶温度5℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.7％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1- 丁基-3-甲基咪唑磷酸二丁酯，吸附温度为20℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为115℃，真空度-0.06MPa，再经冷凝器E-2冷却至20℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度35.5％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
实施例11
氯化尾气经冷却塔R-1降温冷凝，冷凝至35℃，冷凝后，冷却塔R-1的塔底水溶液送去溶剂回收，冷却塔R-1的塔顶尾气，即第一尾气进入脱水脱溶塔R-2继续处理。第一尾气进入预置有亲水离子液体的脱水脱溶塔R-2，吸附温度设为35℃，其中，亲水离子液体为75wt％吡啶酸氢盐和25wt％乙基咪唑硫酸氢盐的混合物。脱水脱溶塔R-2的塔底使用后的亲水离子液体进入离子液体再生釜V-1进行再生处理，再生温度为85℃，真空度-0.09MPa，再生后的亲水离子液体从再生釜V-1的釜底采出，经冷凝器E-1冷却至35℃后，并经过过滤器E-1过滤后，返回脱水脱溶塔R-2继续使用。脱水脱溶塔R-2塔顶采出的第二尾气经活性炭罐T-1吸附残余的有机气体，然后经过滤器E-3、压缩机T-2、过滤器E-4处理后，进入加压精馏塔R-4，加压精馏塔压力为1.0MPa，塔底温度-10℃，塔顶温度0℃，从压精馏塔R-4的塔底得到高纯液体SO 2，纯度99.9％；从加压精馏塔R-4的塔顶得到的采出的HCl气体进入水吸附塔R-5吸附处理。
亲水离子液体的再生釜V-1的釜顶蒸发出的水、有机溶剂及少量HCl和SO 2形成的第三尾气进入预置有亲油离子液体的脱水脱溶塔R-3，其中，亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯，吸附温度为25℃。脱除有机组分后，脱水脱溶塔R-3的塔底采出的亲油离子液体进入亲油离子液体的再生釜V-2再生，再生温度为105℃，真空度-0.07MPa，再经冷凝器E-2冷却至25℃，然后返回脱水脱溶塔R-3继续使用。脱水脱溶塔R-3塔顶采出的水、HCl和SO 2形成的混合气体，记为第四尾气，第四尾气进入含有饱和氯化钠水溶液的HCl吸收釜V-3吸附HCl气体，常温吸附。釜 顶采出的含有SO 2和水的混合气体，记为第五尾气，第五尾气返回脱水脱溶塔R-2继续处理，吸收釜V-3的釜底采出的含有HCl的饱和食盐水进入HCl再生釜V-4，再生出的HCl水蒸气与加压精馏塔R-4塔顶采出的HCl气体一同进入水吸附塔R-5吸附，即可从塔底获得品质较高的盐酸产品，纯度36.5％，塔顶微量尾气去做尾气处理。再生釜V-4产生的饱和食盐水，补加部分纯水后返回HCl吸收釜V-3继续使用。
对比例1
氯化尾气经冷凝塔冷凝，冷凝温度为20℃，除去大部分有机溶剂，然后经浓硫酸脱水，水含量低于0.01％，然后将气体经活性炭吸附处理，气体经压缩机压缩后再进入加压精馏塔分离，加压精馏塔压力为1.0MPa，塔底温度-10℃，塔顶温度0℃，从压精馏塔R-4的塔底得到液体SO 2，纯度98.5％，其中有机物含量1.3％；塔顶HCl气体进入水吸附塔吸附，塔底得到盐酸产品，纯度35.1％，塔顶微量气体去做尾气处理。
综上所述，本申请利用离子液体吸附氯化尾气中的杂质，在加压精馏前，有效解决了水及有机物对HCl和SO 2两种气体分离的影响，解决了因加压分离过程中产生的有机/无机固体附着在管壁及输送泵造成的严重腐蚀及堵塞问题，且可获得高纯度的液体SO 2产品；离子液体的腐蚀性极低，采用离子液体代替浓硫酸，可有效克服传统技术中浓硫酸脱水带来的设备腐蚀及后续处理问题；此外，离子液体具有可高再生性，且再生工艺简单，极大程度上降低了尾气处理的成本。本申请以离子液体为主，并且与冷凝、精馏等手段有机结合，能够有效处理三氯蔗糖生产工艺中的氯化尾气，实现HCl和SO 2两种气体的有效分离，获得高品质的盐酸和液态SO 2产品，且整体处理工艺简单、成本低、具有极大的经济和应用价值。
在本申请的描述中，需要说明的是，术语“中心”、“上”、“下”、“左”、“右”、“竖直”、“水平”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本申请和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本申请的限制。此外，术语“第一”、“第二”、“第三”等仅用于描述目的，而不能理解为指示或暗示相对重要性。
在本申请的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或 一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本申请中的具体含义。
以上所述，仅为本申请的具体实施方式，在本申请的上述教导下，本领域技术人员可以在上述实施例的基础上进行其他的改进或变形。本领域技术人员应该明白，上述的具体描述只是更好的解释本申请的目的，本申请的保护范围应以权利要求的保护范围为准。
此外，本领域的技术人员能够理解，尽管在此所述的一些实施例包括其它实施例中所包括的某些特征而不是其它特征，但是不同实施例的特征的组合意味着处于本申请的范围之内并且形成不同的实施例。例如，在下面的权利要求书中，所要求保护的实施例的任意之一都可以以任意的组合方式来使用。

Claims (10)

  1. 一种尾气处理方法，所述尾气为蔗糖-6-酯经氯化反应生成三氯蔗糖-6-酯的过程中产生的，其特征在于，所述方法包括：
    冷凝步骤：将所述尾气进行降温冷凝，以除去部分有机溶剂和部分水，得到第一溶液和第一尾气；
    脱除步骤：采用亲水离子液体对所述第一尾气进行吸附、分离，以除去其中的大部分水和部分有机溶剂，得到第二尾气；
    分离步骤：将所述第二尾气采用固体吸附剂进行吸附、过滤，得到气态混合物，对所述气态混合物进行分离处理，得到气态氯化氢和液态二氧化硫；和
    相转化步骤：将所述气态氯化氢通入水中，得到盐酸。
  2. 根据权利要求1所述的方法，其特征在于，所述方法还包括：
    在所述脱除步骤内包括的第一再生步骤：将所述脱除步骤中使用后的亲水离子液体进行再生处理，得到再生亲水离子液体和第一再生尾气；以及
    将所述再生亲水离子液体回收，以供所述脱除步骤使用。
  3. 根据权利要求2所述的方法，其特征在于，所述亲水离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa。
  4. 根据权利要求2所述的方法，其特征在于，所述方法还包括：
    在所述第一再生步骤后的回收步骤：采用亲油离子液体对所述第一再生尾气进行吸附，以脱除有机组分，得到第三尾气；
    采用饱和氯化钠水溶液对所述第三尾气进行吸附，以吸收氯化氢，得到第四尾气；
    将所述第四尾气回收至要进入所述脱除步骤的第一尾气中；
    对得到的吸附了氯化氢的饱和氯化钠水溶液进行氯化氢再生处理，得到再生氯化氢，将所述再生氯化氢回收至要进入所述相转化步骤的氯化氢中；将释放了氯化氢的饱和氯化钠水溶液回收至所述饱和氯化钠水溶液中。
  5. 根据权利要求4所述的方法，其特征在于，所述方法还包括：
    在所述回收步骤后的第二再生步骤：将所述回收步骤中使用后的亲油离子液体进行再生处理，得到再生亲油离子液体和第五尾气；
    将所述再生亲油离子液体回收，以供所述回收步骤使用；
    对所述第五尾气进行溶剂回收处理。
  6. 根据权利要求5所述的方法，其特征在于，所述亲油离子液体的再生温度为80～120℃，再生真空度为-0.1至-0.05MPa。
  7. 根据权利要求4所述的方法，其特征在于，在所述回收步骤中，所述亲油离子液体为1-乙基-3-甲基咪唑磷酸二丁酯和/或1-丁基-3-甲基咪唑磷酸二丁酯；
    所述采用亲油离子液体对所述第一再生尾气进行吸附包括：
    在温度为20～40℃，采用亲油离子液体对所述第一再生尾气进行吸附。
  8. 根据权利要求1所述的方法，其特征在于，在所述冷凝步骤中，所述降温冷凝的温度设为0～30℃。
  9. 根据权利要求1所述的方法，其特征在于，所述亲水离子液体为吡啶硫酸氢盐、甲基咪唑硫酸氢盐和乙基咪唑硫酸氢盐中的一种或几种。
  10. 根据权利要求1所述的方法，其特征在于，所述采用亲水离子液体对所述第一尾气进行吸附包括：
    在温度为20～50℃，采用亲水离子液体对所述第一尾气进行吸附。
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