Process and system for recovering acetic acid and synchronously refining hydrochloric acid from hydrogen chloride tail gas

Abstract

The invention provides a process and a system for recovering acetic acid and synchronously refining hydrochloric acid from hydrogen chloride tail gas, which are applied to the technical field of tail gas treatment and comprise the following steps: S1, mixing hydrogen chloride tail gas containing acetic acid with absorption liquid in an absorption device to obtain absorption rich liquid and hydrogen chloride gas; s2, mixing the hydrogen chloride gas absorbed by the absorption liquid with water in a hydrogen chloride absorption device to obtain hydrochloric acid; s3, the absorption rich solution is rectified to obtain regenerated absorption liquid, acetic acid liquid is obtained at the same time, the regenerated absorption liquid can flow back to the step S1 to be mixed with tail gas of hydrogen chloride containing acetic acid, and therefore separation of hydrogen chloride and acetic acid in the tail gas is achieved.

Description

Technical Field

[0001] This application relates to the field of tail gas recovery technology, specifically to a process and system for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid. Background Technology

[0002] Currently, the industrial production method of chloroacetic acid uses acetic anhydride or sulfur as a catalyst to react acetic acid with chlorine gas to produce chloroacetic acid. The resulting hydrogen chloride tail gas contains hydrogen chloride, acetic acid, chlorine gas, chloroacetic acid, acetyl chloride, disulfide dichloride, etc., of which hydrogen chloride accounts for about 95%, acetic acid accounts for about 4%, and other components account for relatively small proportions. This tail gas is then passed through an absorption tower where deionized water is used to countercurrently absorb the hydrogen chloride, producing 30%-35% industrial hydrochloric acid. The acetic acid content is about 1%, which reduces the quality of the hydrochloric acid, making it unsuitable for use or sale as a qualified product, and also wastes acetic acid.

[0003] Hydrogen chloride recovery typically involves passing the exhaust gas into a falling film absorber (or a packed absorber), where pure water is used to countercurrently absorb the hydrogen chloride, producing 30%-35% industrial hydrochloric acid. During this process, acetic acid dissolves, accounting for approximately 1% of the total volume, and mixes into the industrial hydrochloric acid, becoming an impurity.

[0004] Chinese invention patent application CN218130947U discloses a system for removing organic matter from the tail gas of chloroacetic acid production. Chloroacetic acid is a high-boiling-point acid with a low equilibrium partial pressure in hydrogen chloride. Based on the principle of "like dissolves like," organic compounds such as acetic acid have high solubility in chloroacetic acid. Using chloroacetic acid as the absorbent for gaseous organic matter, through multi-stage absorption, the organic matter in the gaseous phase is essentially dissolved in chloroacetic acid, leaving mainly chloroacetic acid as the remaining organic matter in the gaseous phase.

[0005] Chinese invention patent application CN219848913U discloses a recovery system for hydrogenation tail gas in the production process of chloroacetic acid. The system sequentially passes the hydrogenation tail gas in the production process through sodium hypochlorite solution, sodium hydroxide solution, and production water treatment to remove impurities such as aldehydes, acetic acid, and trace amounts of hydrogen chloride from the hydrogenation tail gas.

[0006] Chinese invention patent application CN105036080A discloses a method for preparing high-concentration refined hydrochloric acid using hydrogen chloride from the tail gas produced during chloroacetic acid production. The method involves treating the hydrogen chloride gas with dilute hydrochloric acid and then separating low-boiling-point entrainment by condensation.

[0007] Due to the equilibrium limitations of physical dissolution and the non-selectivity of chemical reactions, the application of the above absorbents has not completely solved the problem of acetic acid residue in hydrogen chloride gas. In actual industrial applications, even with the above technical means, the hydrogen chloride tail gas still contains 3-4% (by mass) acetic acid. After absorption by water, this tail gas forms a 30% hydrochloric acid solution, in which the acetic acid content is about 1%, which is still unusable and can only be treated as waste.

[0008] Therefore, a new technological solution is needed. Summary of the Invention

[0009] In view of this, the embodiments of this specification provide a process and system for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid, so as to realize the resource utilization of hydrogen chloride tail gas generated in the production process of hydrochloroacetic acid.

[0010] The embodiments of this specification provide the following technical solution: a process for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid, including S1, mixing the acetic acid-containing hydrogen chloride tail gas with the absorbent in an absorption device to obtain a rich absorbent liquid and hydrogen chloride gas.

[0011] The absorbent liquid includes a main absorbent, a first absorbent additive, and a second absorbent additive. The main absorbent is an organic acid ester or an inorganic acid ester, the first absorbent additive is a fatty acid compound, and the second absorbent additive is a perfluoroalkane compound.

[0012] S2. The hydrogen chloride gas absorbed by the absorbent is mixed with water in the hydrogen chloride absorption device to obtain hydrochloric acid.

[0013] S3. The rich absorbent solution is distilled to obtain a regenerated absorbent solution, and acetic acid liquid is obtained at the same time. The regenerated absorbent solution can be refluxed back to S1 and mixed with the tail gas containing acetic acid and hydrogen chloride.

[0014] Optionally, in S1, the acetic acid absorbent has a mass fraction of 100 parts, the first absorbent additive and the second absorbent additive have a total mass fraction of 1 to 25 parts, and the proportion of the first absorbent additive or the second absorbent additive in the mixture of the first absorbent additive and the second absorbent additive does not exceed 90%.

[0015] Optionally, in S1, the Hansen solubility parameter δD of the ester compound ranges from 15 to 19, δP ranges from 5 to 12, and δP ranges from 4 to 11. The ester compound specifically includes one or more of dimethyl oxalate, dimethyl succinate, diethyl succinate, ethyl 2-chloroacetate, ethyl 3-chloropropionate, methyl benzoate, ethyl benzoate, dibutyl phthalate, diethyl phthalate, dimethyl phthalate, tributyl phosphate, and triethyl phosphate.

[0016] The Hansen solubility parameters δD of the fatty acid compounds range from 15.5 to 16.5, δP range from 3 to 5.5, and dH range from 8 to 11.5, specifically including hexanoic acid, heptanoic acid, or octanoic acid;

[0017] The Hansen solubility parameters δD of the perfluoroalkane compounds range from 12 to 13, δP range from 0 to 1, and dH range from 0 to 1, specifically including perfluorododecane, perfluorotetradecane, or perfluorohexadecane.

[0018] Optionally, in S1, the operating pressure of the absorption device is atmospheric pressure, the temperature is 0~30℃, and the absorption water is deionized water.

[0019] Optionally, in S1, the mass ratio of the acetic acid-containing hydrogen chloride tail gas to the absorption liquid is 2:0.5~1.

[0020] Optionally, in S1, the tail gas containing acetic acid and hydrogen chloride is mixed with the absorbent in a multi-stage countercurrent manner in the absorption device, with the tail gas containing acetic acid and hydrogen chloride being mixed from bottom to top and the absorbent from top to bottom.

[0021] This application also provides a system for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid, including an acetic acid adsorption device and a hydrogen chloride adsorption device, wherein the acetic acid adsorption device and the hydrogen chloride adsorption device are connected in sequence, the acetic acid adsorption device is provided with an absorbent, and the hydrogen chloride adsorption device is provided with deionized water, and the tail gas in the tail gas storage device flows through the acetic acid adsorption device and the hydrogen chloride adsorption device in sequence to complete the separation of acetic acid and hydrogen chloride, and obtain a refined hydrochloric acid solution.

[0022] Optionally, the acetic acid adsorption device is connected to an acetic acid distillation device, and the adsorbent liquid containing acetic acid is separated from the adsorbent rich liquid by the acetic acid distillation device. The regenerated absorbent liquid in the acetic acid distillation device can be returned to the acetic acid adsorption device.

[0023] Optionally, the acetic acid adsorption device and the hydrogen chloride adsorption device mentioned in S1 and S2 are absorption vessels or absorption towers.

[0024] Compared with the prior art, the beneficial effects that at least one technical solution adopted in the embodiments of this specification can achieve include at least:

[0025] The technical solution of this application uses perfluoroalkanes to adjust the dispersion force (δD) of the main absorbent and fatty acid compounds to adjust the polar force (δP) and hydrogen bonding force (δH) of the main absorbent. The prepared absorbent solution is a mixed solvent with intermolecular forces more similar to acetic acid. This mixed solvent has good solubility for acetic acid, thereby capturing acetic acid in the hydrogen chloride tail gas. Hydrogen chloride is incompatible with the absorbent due to its aprotic and low polarity, thus achieving the separation of hydrogen chloride and acetic acid in the tail gas.

[0026] The separated hydrogen chloride is mixed with water to directly obtain hydrochloric acid. The separated acetic acid is passed through the absorbent regeneration tower to obtain an acetic acid solution at the top of the tower. This solution is returned to the chloroacetic acid reaction unit as a raw material. The absorbent regenerated at the bottom of the tower is reused in step one, which can realize recycling, improve production efficiency, and avoid pollutant discharge. Attached Figure Description

[0027] To more clearly illustrate the technical solutions of the embodiments of this application, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0028] Figure 1 This is a schematic diagram of a system for simultaneously refining hydrochloric acid from hydrogen chloride tail gas, as described in this application.

[0029] In the diagram: 1. Gas cylinder; 2. Acetic acid absorption vessel; 3. Electronic scale; 4. Hydrogen chloride absorption vessel; 5. Pressure reducing valve; 6. Pressure gauge; 7. Flow meter; 8. Control valve. Detailed Implementation

[0030] The embodiments of this application will now be described in detail with reference to the accompanying drawings.

[0031] The following specific examples illustrate the implementation of this application. Those skilled in the art can easily understand other advantages and effects of this application from the content disclosed in this specification. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. This application can also be implemented or applied through other different specific embodiments, and the details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of this application. It should be noted that, in the absence of conflict, the following embodiments and features in the embodiments can be combined with each other. Based on the embodiments in this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0032] It should be noted that various aspects of embodiments within the scope of the appended claims are described below. It will be apparent that the aspects described herein can be embodied in a wide variety of forms, and any particular structure and / or function described herein is merely illustrative. Based on this application, those skilled in the art will understand that one aspect described herein can be implemented independently of any other aspect, and two or more of these aspects can be combined in various ways. For example, any number and aspects set forth herein can be used to implement the device and / or practice the method. Additionally, this device and / or method can be implemented using structures and / or functionalities other than one or more of the aspects set forth herein.

[0033] It should also be noted that the illustrations provided in the following embodiments are only schematic representations of the basic concept of this application. The drawings only show the components related to this application and are not drawn according to the actual number, shape and size of the components in the actual implementation. In the actual implementation, the form, quantity and proportion of each component can be arbitrarily changed, and the layout of the components may also be more complex.

[0034] Additionally, specific details are provided in the following description to facilitate a thorough understanding of the examples. However, those skilled in the art will understand that practice can be carried out without these specific details.

[0035] This specification provides an embodiment of a process for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid. The process includes S1, mixing the acetic acid-containing hydrogen chloride tail gas with an absorbent in an absorption device to obtain a rich absorbent and hydrogen chloride gas.

[0036] The absorbent liquid includes a main absorbent, a first absorbent additive, and a second absorbent additive. The main absorbent is an organic acid ester or an inorganic acid ester. The Hansen solubility parameter δD of the main absorbent is in the range of 15 to 19, δP is in the range of 5 to 12, and δP is in the range of 4 to 11. The first absorbent additive is a fatty acid compound, including hexanoic acid, heptanoic acid, or octanoic acid. The second absorbent additive is a perfluoroalkane compound, including perfluorododecane, perfluorotetradecane, or perfluorohexadecane.

[0037] S2. The hydrogen chloride gas absorbed by the absorbent is mixed with water in the hydrogen chloride absorption device to obtain hydrochloric acid.

[0038] S3. The rich absorbent solution is distilled to obtain a regenerated absorbent solution, and acetic acid liquid is obtained at the same time. The regenerated absorbent solution can be refluxed back to S1 and mixed with the tail gas containing acetic acid and hydrogen chloride.

[0039] In S1, the acetic acid absorbent has a mass fraction of 100 parts, the first absorbent additive and the second absorbent additive have a mass fraction of 1 to 25 parts, and in the mixture of the first absorbent additive and the second absorbent additive, the proportion of the first absorbent additive or the second absorbent additive does not exceed 90%.

[0040] In S1, the ester compounds specifically include one or more of the following: dimethyl oxalate, dimethyl succinate, diethyl succinate, ethyl 2-chloroacetate, ethyl 3-chloropropionate, methyl benzoate, ethyl benzoate, dibutyl phthalate, diethyl phthalate, dimethyl phthalate, tributyl phosphate, and triethyl phosphate.

[0041] The absorption device operates at atmospheric pressure and at a temperature of 0~30℃, and the water used for absorption is deionized water.

[0042] In S1, the mass ratio of the acetic acid-containing hydrogen chloride tail gas to the absorption liquid is 2:0.5~1.

[0043] In S1, the tail gas containing acetic acid and hydrogen chloride is mixed with the absorbent in a multi-stage countercurrent manner in the absorption device, with the tail gas containing acetic acid and hydrogen chloride being mixed from bottom to top and the absorbent from top to bottom.

[0044] This application also provides a system for recovering acetic acid from hydrogen chloride tail gas and simultaneously refining hydrochloric acid, including an acetic acid adsorption device and a hydrogen chloride adsorption device, wherein the acetic acid adsorption device and the hydrogen chloride adsorption device are connected in sequence, the acetic acid adsorption device is provided with an absorbent, and the hydrogen chloride adsorption device is provided with deionized water, and the tail gas in the tail gas storage device flows through the acetic acid adsorption device and the hydrogen chloride adsorption device in sequence to complete the separation of acetic acid and hydrogen chloride, and obtain a refined hydrochloric acid solution.

[0045] The acetic acid adsorption device is connected to an acetic acid distillation device. The adsorbent solution containing acetic acid is separated from the adsorbent rich solution by the acetic acid distillation device. The regenerated absorbent solution in the acetic acid distillation device can be returned to the acetic acid adsorption device.

[0046] The acetic acid adsorption device and hydrogen chloride adsorption device mentioned in S1 and S2 are absorption vessels or absorption towers.

[0047] Example

[0048] A gas cylinder (1) containing 1% acetic acid and high-pressure HCl flows into the acetic acid absorption device (2) at a flow rate of 200 ml per minute (7) after passing through a pressure reducing valve (5). The acetic acid absorption device (2) is pre-filled with a certain amount of absorbent liquid. The acetic acid in the HCl gas is absorbed in the acetic acid absorption device (2). The gas flowing out of the acetic acid absorption device (2) flows into the hydrogen chloride absorption device (4). The hydrogen chloride and unabsorbed acetic acid are absorbed in the hydrogen chloride absorption device (3). After 10 hours, the gas intake is stopped, and the weight of the electronic scale is recorded. The absorption amount of the acetic acid absorption device (2) and the hydrogen chloride absorption device (4) is measured by the electronic scale (3). The concentration of chloride ions and acetate ions in the two devices are measured by titration to determine the absorption selectivity and absorption rate of the composite solvent. The switch is controlled by the control valve (8), the system pressure is detected by the pressure gauge (6), and the system flow rate is detected by the flow meter (7).

[0049] Example 1

[0050] Prepare 500g of absorbent solution in the following proportions: main absorbent: 400g of dibutyl phthalate, 80g of hexanoic acid as the first absorbent additive, and 20g of perfluorododecane as the second absorbent additive. Mix them evenly and pour them into the acetic acid absorption vessel (2); put 500g of deionized water into the hydrogen chloride absorption vessel (4).

[0051] The measurement and calculation results after absorption are as follows: The net weight of the solution in the acetic acid absorption vessel (2) is 504.115g, of which the molar fraction of hydrogen chloride is 0.115% and the molar fraction of acetic acid is 0.188%, and the recovery of acetic acid by the solvent in the acetic acid absorption vessel is 99.56%; The net weight of the solution in the hydrogen chloride absorption vessel (4) is 680.13g, of which the concentration of hydrogen chloride is 15.1% and the concentration of acetic acid is 6.7ppm.

[0052] Example 2

[0053] Prepare 500g of absorbent solution in the following proportions: main absorbent: 450g of diethyl succinate, 45g of octanoic acid as the first absorbent additive, and 5g of perfluorotetradecane as the second absorbent additive. Mix them evenly and pour them into the acetic acid absorption vessel (2); put 500g of deionized water into the hydrogen chloride absorption vessel (4).

[0054] The measurement and calculation results after absorption are as follows: The net weight of the solution in the acetic acid absorption vessel (2) is 504.92g, of which the molar fraction of hydrogen chloride is 0.273% and the molar fraction of acetic acid is 0.219%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 92.92%; The net weight of the solution in the hydrogen chloride absorption vessel (4) is 679.21g, of which the concentration of hydrogen chloride is 15.02% and the concentration of acetic acid is 108ppm.

[0055] Example 3

[0056] Prepare 500g of absorbent solution in the following proportions: main absorbent: 470g of tributyl phosphate, 10g of octanoic acid as the first absorbent additive, and 20g of perfluorohexadecane as the second absorbent additive. Mix them evenly and pour them into the acetic acid absorption vessel (2); put 500g of deionized water into the hydrogen chloride absorption vessel (4).

[0057] The measurement and calculation results after absorption are as follows: The net weight of the acetic acid absorption vessel (2) solution is 505.17g, of which the molar fraction of hydrogen chloride is 0.35% and the molar fraction of acetic acid is 0.4%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 97.04%; The net weight of the hydrogen chloride absorption vessel (4) solution is 691.25g, of which the concentration of hydrogen chloride is 27.64% and the concentration of acetic acid is 138ppm.

[0058] Comparative Example 1

[0059] The difference from Example 1 is that the first and second absorbent additives are not added, and the main absorbent is 500g of dibutyl phthalate.

[0060] The measurement and calculation results after absorption are as follows: The net weight of the acetic acid absorption vessel (2) solution is 503.15g, of which the molar fraction of hydrogen chloride is 0.19% and the molar fraction of acetic acid is 0.49%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 77.04%; The net weight of the hydrogen chloride absorption vessel (4) solution is 693.31g, of which the concentration of hydrogen chloride is 27.72% and the concentration of acetic acid is 715ppm.

[0061] Comparative Example 2

[0062] The difference from Example 1 is that the first absorbent additive is not added, and the main absorbent is 480g of dibutyl phthalate.

[0063] The measurement and calculation results after absorption are as follows: The net weight of the acetic acid absorption vessel (2) solution is 502.45g, of which the molar fraction of hydrogen chloride is 0.16% and the molar fraction of acetic acid is 0.39%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 62.2%; The net weight of the hydrogen chloride absorption vessel (4) solution is 694g, of which the concentration of hydrogen chloride is 27.8% and the concentration of acetic acid is 1215ppm.

[0064] Comparative Example 3

[0065] The difference from Example 1 is that no second absorbent additive is added, and the main absorbent is 420g of dibutyl phthalate.

[0066] The measurement and calculation results after absorption are as follows: The net weight of the acetic acid absorption vessel (2) solution is 502.95g, of which the molar fraction of hydrogen chloride is 0.18% and the molar fraction of acetic acid is 0.47%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 74.6%; The net weight of the hydrogen chloride absorption vessel (4) solution is 693.52g, of which the concentration of hydrogen chloride is 27.6% and the concentration of acetic acid is 815ppm.

[0067] Comparative Example 4

[0068] Prepare 500g of absorbent solution in the following proportions: main absorbent: 470g of tributyl phosphate, 20g of sebacic acid as the first absorbent additive (whose Hansen solubility parameters are δD, δP and dH are 17.7, 7.1 and 11.7 respectively), and 10g of dodecane as the second absorbent additive (whose Hansen solubility parameters are δD, δP and dH are 16, 0 and 0 respectively). Mix well and pour into the acetic acid absorption vessel (2); fill the hydrogen chloride absorption vessel (4) with 500g of deionized water.

[0069] The measurement and calculation results after absorption are as follows: The net weight of the acetic acid absorption vessel (2) solution is 502.16g, of which the molar fraction of hydrogen chloride is 0.2% and the molar fraction of acetic acid is 0.3%, and the recovery rate of acetic acid by the solvent in the acetic acid absorption vessel is 46.65%; The net weight of the hydrogen chloride absorption vessel (4) solution is 694.31g, of which the concentration of hydrogen chloride is 27.69% and the concentration of acetic acid is 2470ppm.

[0070] A comparison of Example 1 with Comparative Examples 1, 2 and 3 shows that, by omitting the addition of the first and second absorbent additives, the recovery rate of acetic acid decreased compared to Example 1.

[0071] A comparison between Example 3 and Comparative Example 4 shows that, by changing the first and second absorbent additives, the recovery rate of acetic acid in Comparative Example 4 is much lower than that in Example 3, due to limitations imposed by the Hansen solubility parameter.

[0072] In this specification, the same or similar parts between the various embodiments can be referred to mutually. Each embodiment focuses on describing the differences from other embodiments. In particular, the descriptions of the embodiments described later are relatively simple, and relevant parts can be referred to the descriptions of the foregoing embodiments.

[0073] The above description is merely a specific embodiment of this application, but the scope of protection of this application is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in this application should be included within the scope of protection of this application. Therefore, the scope of protection of this application should be determined by the scope of the claims.

Claims

1. A process for simultaneously refining hydrochloric acid from hydrogen chloride tail gas by recovering acetic acid, characterized in that: Including S1, mixing the hydrogen chloride tail gas containing acetic acid with the absorbent in the absorption device to obtain a rich absorbent liquid and hydrogen chloride gas; The absorbent liquid includes a main absorbent, a first absorbent additive, and a second absorbent additive. The main absorbent is an organic acid ester or an inorganic acid ester, the first absorbent additive is a fatty acid compound, and the second absorbent additive is a perfluoroalkane compound. S2. The hydrogen chloride gas absorbed by the absorbent is mixed with water in the hydrogen chloride absorption device to obtain hydrochloric acid. S3. The rich absorbent solution is distilled to obtain a regenerated absorbent solution, and acetic acid liquid is obtained at the same time. The regenerated absorbent solution can be refluxed back to S1 and mixed with the tail gas containing acetic acid and hydrogen chloride.

2. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: In S1, the main absorbent has a mass fraction of 100 parts, the first absorbent additive and the second absorbent additive have a mass fraction of 1 to 25 parts, and the proportion of the first absorbent additive or the second absorbent additive in the mixture of the first absorbent additive and the second absorbent additive does not exceed 90%.

3. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: In S1, the Hansen solubility parameter δD of the ester compound ranges from 15 to 19, δP ranges from 5 to 12, and δP ranges from 4 to 11. The ester compound specifically includes one or more of the following: dimethyl oxalate, dimethyl succinate, diethyl succinate, ethyl 2-chloroacetate, ethyl 3-chloropropionate, methyl benzoate, ethyl benzoate, dibutyl phthalate, diethyl phthalate, tributyl phosphate, and triethyl phosphate. The Hansen solubility parameters δD of the fatty acid compounds range from 15.5 to 16.5, δP range from 3 to 5.5, and dH range from 8 to 11.5, specifically including hexanoic acid, heptanoic acid, or octanoic acid; The Hansen solubility parameters δD of the perfluoroalkane compounds range from 12 to 13, δP range from 0 to 1, and dH range from 0 to 1, specifically including perfluorododecane, perfluorotetradecane, or perfluorohexadecane.

4. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: The absorption device operates at atmospheric pressure and at a temperature of 0~30℃, and the water used for absorption is deionized water.

5. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: In S1, the mass ratio of the acetic acid-containing hydrogen chloride tail gas to the absorption liquid is 2:0.5~1.

6. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: In S1, the tail gas containing acetic acid and hydrogen chloride is mixed with the absorbent in a multi-stage countercurrent manner in the absorption device, with the tail gas containing acetic acid and hydrogen chloride being mixed from bottom to top and the absorbent from top to bottom.

7. The process for recovering acetic acid and simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 1, characterized in that: In S2, deionized water is used to absorb hydrogen chloride in a countercurrent mixing process to obtain hydrochloric acid.

8. A system for simultaneously refining hydrochloric acid from hydrogen chloride tail gas by recovering acetic acid, employing the process described in any one of claims 1-7, characterized in that, The apparatus includes an acetic acid adsorption device and a hydrogen chloride adsorption device, which are connected in sequence. The acetic acid adsorption device contains an absorbent liquid, and the hydrogen chloride adsorption device contains deionized water. The tail gas flows through the acetic acid adsorption device and the hydrogen chloride adsorption device in sequence to separate acetic acid and hydrogen chloride, and a purified hydrochloric acid solution is obtained.

9. A system for simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 8, characterized in that, The acetic acid adsorption device is connected to an acetic acid distillation device. The adsorbent solution containing acetic acid is separated from the adsorbent rich solution by the acetic acid distillation device. The regenerated absorbent solution in the acetic acid distillation device can be returned to the acetic acid adsorption device.

10. A system for simultaneously refining hydrochloric acid from hydrogen chloride tail gas according to claim 9, characterized in that, The acetic acid adsorption device and hydrogen chloride adsorption device mentioned in S1 and S2 are absorption vessels or absorption towers.

Images