Mixed gas treatment and recovery system for organic compounds

Abstract

The utility model relates to the technical field of recovery systems, in particular to a treatment and recovery system for mixed gas of organic compounds, which mainly aims at solving the problems of waste and economic loss caused by the fact that part of valuable organic matters in the mixed gas of the organic compounds generated in chemical production are sent to be combusted. According to the technical scheme, the device comprises a compression mechanism arranged on a feed gas conveying path, and the compression mechanism is used for increasing the pressure of feed gas to a preset value; the washing assembly is connected with the output end of the compression mechanism and is used for absorbing alcohols, esters, aldehydes and ethers in the raw material gas through circulating liquid; and the adsorption tower group is connected to the downstream of the washing assembly. According to the device, valuable alcohols, esters, aldehydes and ethers in the mixed gas can be completely recycled and liquefied into products, waste is avoided, economic benefits are improved, meanwhile, carbon emission of torch combustion is reduced, and the environment-friendly requirement is met.

Description

Technical Field

[0001] This utility model relates to the field of recycling system technology, and in particular to a mixed gas treatment and recycling system for organic compounds. Background Technology

[0002] In the production processes of petrochemical and coal chemical industries, gases such as synthesis tail gas and non-condensable gas from distillation columns are generated. These gases contain organic compounds such as alcohols, esters, aldehydes, and ethers, all of which have certain utilization value. In the past, water washing or temperature-switching adsorption processes were commonly used to treat these mixed gases. These processes can absorb a portion of the alcohols, esters, aldehydes, and ethers, and then the absorbed portion is sent for combustion treatment, while the remaining effective gases are returned to the production system to continue participating in the reaction or are flared for combustion and emission.

[0003] However, this traditional treatment method has obvious drawbacks. On the one hand, the alcohols, esters, aldehydes, and ethers that are absorbed and sent for combustion are valuable resources, but they are wasted, preventing companies from fully recycling these valuable components and causing economic losses, which does not conform to the principle of economical and efficient production. On the other hand, flaring these substances will generate a large amount of carbon emissions, negatively impacting the environment and contradicting current environmental protection principles. In view of this, this utility model proposes a mixed gas treatment and recovery system for organic compounds. Summary of the Invention

[0004] The purpose of this invention is to address the problem in the background art that when mixed gases of organic compounds generated from chemical production are washed with water or subjected to temperature-switching adsorption, some valuable organic matter is sent for combustion, resulting in waste and economic losses, and the combustion generates a large amount of carbon emissions that pollute the environment. This invention proposes a mixed gas treatment and recovery system for organic compounds.

[0005] The technical solution of this utility model is as follows: A mixed gas treatment and recovery system for organic compounds includes a compression mechanism disposed on the raw gas conveying path, the compression mechanism being used to increase the pressure of the raw gas to a preset value; a washing assembly connected to the output end of the compression mechanism, the washing assembly being used to absorb alcohols, esters, aldehydes, and ethers in the raw gas through a circulating liquid; an adsorption tower group connected downstream of the washing assembly, the adsorption tower group being used to further adsorb residual alcohols, esters, aldehydes, and ethers in the gas; a regeneration mechanism disposed beside the adsorption tower group, the regeneration mechanism being used to regenerate the adsorption towers that are saturated with adsorption and recover the desorbed organic matter; and a separation and purification assembly connected downstream of the washing assembly and the adsorption tower group, the separation and purification assembly being used to separate and purify the recovered organic matter.

[0006] Optionally, the compression mechanism includes a raw material gas pipeline and a compressor. The input end of the compressor is connected to the raw material gas pipeline, and the compressor is used to pressurize the raw material gas with a pressure lower than 1.5 MPa to above 1.5 MPa.

[0007] Optionally, the washing assembly includes a washing tower A and a washing tower B connected in series. The bottom of the washing tower A is connected to a first circulation pump, and the output end of the first circulation pump is connected to a first circulating liquid cooler. The output end of the first circulating liquid cooler is connected to the top of the washing tower A. The bottom of the washing tower B is connected to a second circulation pump, and the output end of the second circulation pump is connected to a second circulating liquid cooler. The output end of the second circulating liquid cooler is connected to the top of the washing tower B.

[0008] Optionally, both washing tower A and washing tower B are equipped with wire mesh demisters at their tops, and a pressure reducing valve is connected between washing tower A and washing tower B.

[0009] Optionally, the adsorption tower group includes at least four adsorption towers, each filled with an adsorbent selected from one or more of activated carbon, 5A molecular sieve, and 13X molecular sieve. The inlet ends of the multiple adsorption towers are connected to adsorption tower inlet pipes, which are connected to the outlet of washing tower A.

[0010] Optionally, the regeneration mechanism includes a regeneration gas heater and a heat exchanger. The outlet of the adsorption tower is connected in sequence to the heat exchanger and the regeneration gas heater. The output end of the regeneration gas heater is connected to the adsorption tower to be regenerated through a pipeline. The bottom of the adsorption tower to be regenerated is connected to an adsorption tower regeneration gas return pipe, which is connected to the scrubbing tower B.

[0011] Optionally, the regeneration mechanism further includes a low-pressure nitrogen pipeline, which is sequentially connected to a nitrogen heater and a programmable valve group, and the programmable valve group is connected to the adsorption tower.

[0012] Optionally, the separation and purification assembly includes a flash evaporator, a light component removal tower, and a heavy component removal tower connected in sequence. The flash evaporator is connected to the bottom of washing tower A and washing tower B. The top of the light component removal tower is connected to a light component removal tower top condenser, which is connected to an ether collection tank. The top of the heavy component removal tower is connected to a heavy component removal tower top condenser, which is connected to an alcohol and ester collection tank.

[0013] Optionally, a reboiler for removing light pollutants is installed at the bottom of the light pollutant removal tower, a reboiler for removing heavy pollutants is installed at the bottom of the heavy pollutant removal tower, and a circulating scrubbing liquid lean reflux pump is connected to the bottom of the heavy pollutant removal tower. The output end of the circulating scrubbing liquid lean reflux pump is connected to scrubbing tower A and scrubbing tower B.

[0014] Optionally, it also includes a control unit, wherein the compressor, the first circulating pump, the second circulating pump, the regenerated gas heater, and the programmable valve group are all electrically connected to the control unit, and a concentration sensor is installed at the outlet of the adsorption tower, wherein the concentration sensor is electrically connected to the control unit.

[0015] In summary, this application includes at least one of the following beneficial technical effects:

[0016] This invention utilizes the synergistic effect of a two-stage washing and adsorption tower assembly to fully recover and liquefy organic compounds such as alcohols, esters, aldehydes, and ethers in the raw gas into products, avoiding the waste of such substances in traditional processes and significantly improving resource utilization efficiency.

[0017] Furthermore, by adopting an isobaric regeneration method, the adsorption tower is backflushed by heating the gas at the top outlet of the adsorption tower with a regeneration gas heater. This eliminates the need to introduce a large amount of regeneration gas and avoids the loss of organic matter caused by traditional depressurization regeneration, resulting in a significant reduction in energy consumption. At the same time, the alcohols, esters, aldehydes, and ethers in the treated gas meet national emission standards, reducing carbon emissions from flare combustion and thus having environmental value.

[0018] In summary, this invention can fully recover valuable alcohols, esters, aldehydes, and ethers from mixed gases and liquefy them into products, avoiding waste and improving economic efficiency, while reducing carbon emissions from flare combustion, thus meeting environmental protection requirements. Attached Figure Description

[0019] Figure 1 This is a schematic diagram of a mixed gas treatment and recovery system for organic compounds.

[0020] Attached reference numerals: 1. Raw gas pipeline; 2. Compressor; 3. Scrubber A; 4. First circulating liquid cooler; 5. First circulating pump; 6. First liquid level regulating valve; 7. First outlet pipeline; 8. Pressure reducing regulating valve; 9. Scrubber B; 10. Second circulating liquid cooler; 11. Second circulating pump; 12. Second liquid level regulating valve; 13. Circulating liquid outlet pipe; 14. Flash evaporator; 15. Light weight removal tower; 16. Upper outlet pipe of light weight removal tower; 17. Bottom outlet pipe of the light component removal tower; 18. Heavy component removal tower; 19. Reboiler of the light component removal tower; 20. Reboiler of the heavy component removal tower; 21. Lean liquor reflux pump for circulating wash liquor; 22. Second lean liquor reflux pipe; 23. First lean liquor reflux pipe; 24. Reflux pump for the heavy component removal tower; 25. Alcohol and ester collection tank; 26. Product alcohol and ester outlet pipe; 27. Top condenser of the heavy component removal tower; 28. Top outlet pipe of the flash evaporator; 29. ​​Top condenser of the light component removal tower; 30. Light component removal tower 31. Reflux pump; 32. Ether collection tank; 33. Product ether outlet pipe; 34. Non-condensable gas outlet pipe; 35. Adsorption tower regeneration gas reflux pipe; 36. Heat exchanger; 37. Regeneration gas heater; 38. Adsorption tower A; 39. Adsorption tower C; 40. Adsorption tower D; 41. Adsorption tower E; 42. Intermediate buffer tank; 43. Low-pressure nitrogen pipeline; 44. Nitrogen flow regulating valve; 45. Nitrogen heater; 46. Tenth 47. Third programmable valve; 48. Seventh programmable valve; 49. Pressure boosting programmable valve; 50. Eighth programmable valve; 51. Ninth programmable valve; 52. First programmable valve; 53. Second programmable valve; 54. Sixth programmable valve; 55. Fourth programmable valve; 56. Fifth programmable valve; 57. Adsorption tower inlet pipe; 58. Second outlet pipe; 59. Cooling outlet pipe; 60. Pressure relief pipe; 61. Pressure boosting and replacement pipe; 62. Regenerated gas outlet pipe. Detailed Implementation

[0021] The technical solution of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are some embodiments of this utility model, but not all embodiments.

[0022] The components of the present invention embodiments described and shown in the accompanying drawings can typically be arranged and designed in a variety of different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention.

[0023] Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this utility model.

[0024] In the description of this utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings and are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0025] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.

[0026] Example:

[0027] like Figure 1 As shown, the present invention proposes a mixed gas treatment and recovery system for organic compounds, including a compression mechanism disposed on the raw gas conveying path. The compression mechanism is used to increase the pressure of the raw gas to a preset value. The compression mechanism includes a raw gas pipeline 1 and a compressor 2. The input end of the compressor 2 is connected to the raw gas pipeline 1. The compressor 2 is used to pressurize the raw gas with a pressure lower than 1.5MPa to above 1.5MPa. By increasing the pressure, the absorption effect of the subsequent circulating liquid on alcohols, esters, aldehydes and ethers in the raw gas can be enhanced, laying the foundation for efficient recovery.

[0028] Furthermore, the aforementioned recovery system includes a scrubbing assembly connected to the output of the compression mechanism. This assembly absorbs alcohols, esters, aldehydes, and ethers from the raw material gas through a circulating liquid. The scrubbing assembly includes scrubbing towers A3 and B9 connected in series. A first circulating pump 5 is connected to the bottom of scrubbing tower A3, and its output is connected to a first circulating liquid cooler 4. The output of the first circulating liquid cooler 4 is connected to the top of scrubbing tower A3. The circulating liquid at the bottom of scrubbing tower A3 is pumped by the first circulating pump 5 to the first circulating liquid cooler 4 for cooling before being returned to the top, achieving cooling and circulation of the circulating liquid and ensuring its temperature is controlled below 39 degrees Celsius, thus improving absorption efficiency. A second circulating pump 11 is connected to the bottom of scrubbing tower B9, and its output is connected to a second circulating liquid cooler 10. The output of the second circulating liquid cooler 10 is connected to the top of scrubbing tower B9, similarly cooling and circulating the circulating liquid within scrubbing tower B9 to ensure its absorption effect. A second outlet pipe 58 is connected to the top of scrubbing tower B9 for output. Both scrubbing towers A3 and B9 are equipped with wire mesh demisters at their tops, which can effectively capture mist droplets in the gas and reduce the loss of alcohols, esters, aldehydes, and ethers. A pressure reducing valve 8 connects scrubbing towers A3 and B9, and the first outlet pipe 7 is connected to the pressure reducing valve 8, which can regulate the gas pressure entering scrubbing tower B9.

[0029] Furthermore, the aforementioned recovery system also includes an adsorption tower group connected downstream of the scrubbing assembly. This adsorption tower group is used to further adsorb residual alcohols, esters, aldehydes, and ethers in the gas. The adsorption tower group includes at least four adsorption towers, such as adsorption tower A37, adsorption tower B38, adsorption tower C39, adsorption tower D40, and adsorption tower E41. The adsorption towers are filled with adsorbent selected from one or more of activated carbon, 5A molecular sieve, and 13X molecular sieve, which can efficiently adsorb alcohols, esters, aldehydes, and ethers in the gas. The inlet ends of multiple adsorption towers are connected to adsorption tower inlet pipes 57, which are connected to the outlet of scrubbing tower A3. The adsorption tower inlet pipes 57 are equipped with a first programmable valve 52, a second programmable valve 53, and a sixth programmable valve 54, etc., to control the gas entering different adsorption towers. The regenerated gas after passing through the adsorption towers is discharged through the regenerated gas outlet pipe 62.

[0030] In one implementation, the above-mentioned recovery system includes a regeneration mechanism located beside the adsorption tower group. This regeneration mechanism is used to regenerate the adsorption towers that have reached adsorption saturation and recover the desorbed organic matter. The regeneration mechanism includes a regeneration gas heater 36 and a heat exchanger 35. The outlet of the adsorption tower is sequentially connected to the heat exchanger 35 and the regeneration gas heater 36, allowing the heat from the outlet gas of the adsorption tower to preheat the regeneration gas. The output end of the regeneration gas heater 36 is connected to the adsorption tower to be regenerated via a pipeline, which is equipped with a seventh control valve 48, an eighth control valve 50, etc. The bottom of the adsorption tower to be regenerated is connected to an adsorption tower regeneration gas return pipe 34, which is connected to a scrubbing tower B9. This pipe is equipped with a fourth control valve 55 and a fifth control valve 56. The regeneration mechanism also includes a low-pressure nitrogen pipeline 43, which is connected in sequence to a nitrogen heater 45 and a programmable valve group. The programmable valve group is connected to the adsorption tower. The low-pressure nitrogen pipeline 43 is equipped with a nitrogen flow regulating valve 44, which can regulate the nitrogen flow. After being heated by the nitrogen heater 45, the nitrogen enters the adsorption tower through the tenth programmable valve 46 and other programmable valves, and is used as supplementary regeneration gas when the regeneration gas quantity is insufficient.

[0031] Furthermore, the aforementioned recovery system also includes a separation and purification component connected downstream of the washing assembly and the adsorption tower assembly. This component is used to separate and purify the recovered organic matter. The separation and purification component includes a flash evaporator 14, a light-weight removal tower 15, and a heavy-weight removal tower 18 connected in sequence. The flash evaporator 14 is connected to the bottom of the washing tower A3 and the washing tower B9. The bottom of the washing tower A3 is connected to the flash evaporator 14 via a first level regulating valve 6, and the bottom of the washing tower B9 is connected to the flash evaporator 14 via a second level regulating valve 12 and a circulating liquid outlet pipe 13. The top of the light-weight removal tower 15 is connected to a light-weight removal tower top condenser 29, which is connected to an ether collection tank 31. The ether collection tank 31 is connected to a product ether outlet pipe 32, which can collect and output ether products. The top of the heavy removal tower 18 is connected to a top condenser 27, which is connected to an alcohol and ester collection tank 25. The alcohol and ester collection tank 25 is connected to a product alcohol and ester outlet pipe 26 for collecting and discharging alcohol and ester products. The bottom of the light removal tower 15 is equipped with a reboiler 19 to provide a heat source for the light removal tower 15. The bottom of the heavy removal tower 18 is equipped with a reboiler 20 to provide a heat source for the heavy removal tower 18. The bottom of the heavy removal tower 18 is connected to a circulating wash liquid lean reflux pump 21. The output of the circulating wash liquid lean reflux pump 21 is connected to washing tower A3 and washing tower B9 through a second lean reflux pipe 22 and a first lean reflux pipe 23, realizing the recycling of the circulating liquid. The top of the light removal tower 15 has an upper outlet pipe 16 connected to the top condenser 29, and the bottom of the light removal tower has a bottom outlet pipe 17 connected to the heavy removal tower 18. The flash tower 14 has a top outlet pipe 28 connected to the top condenser 29 of the light-weight gas removal tower. The top condenser 29 is connected to a light-weight gas removal tower reflux pump 30 for returning the condensate to the light-weight gas removal tower 15. The heavy-weight gas removal tower 18 is connected to a heavy-weight gas removal tower reflux pump 24 for returning the condensate to the heavy-weight gas removal tower 18. Non-condensable gases are discharged through a non-condensable gas outlet pipe 33.

[0032] Furthermore, the aforementioned recovery system also includes an intermediate buffer tank 42, located downstream of the adsorption tower group, used to buffer the gas at the outlet of the adsorption tower. The outlet of the adsorption tower is connected to the intermediate buffer tank 42 via a third programmable valve 47, etc. The intermediate buffer tank 42 is connected to a cooling outlet pipe 59 to send the gas to subsequent processes. The adsorption tower is also equipped with a pressure relief pipe 60 and a pressure boosting and displacement pipe 61. The pressure relief pipe 60 is used for pressure relief operations of the adsorption tower, and the pressure boosting and displacement pipe 61 is used for pressure boosting and displacement of the adsorption tower. The pipelines are equipped with a pressure boosting programmable valve 49, a ninth programmable valve 51, etc.

[0033] Finally, the above-mentioned recovery system also includes a control unit. The compressor 2, the first circulation pump 5, the second circulation pump 11, the regeneration gas heater 36, and the programmable valve group are all electrically connected to the control unit. A concentration sensor is installed at the outlet of the adsorption tower. The concentration sensor is electrically connected to the control unit. The control unit can control the operation of each device and the programmable valve according to the concentration of alcohols, esters, aldehydes, and ethers in the gas detected by the concentration sensor, so as to realize the automatic control of the system.

[0034] In this embodiment, a mixed gas containing alcohols, esters, aldehydes, and ethers (such as synthesis tail gas or non-condensable gas from a distillation column) enters the system through the raw material gas pipeline 1. If the gas pressure is below 1.5 MPa, it is pressurized to above 1.5 MPa by compressor 2 (the raw material gas with the required pressure can directly enter the next stage), utilizing the high-pressure environment to improve the dissolution efficiency of the subsequent circulating liquid for organic matter. The pressurized gas enters the scrubbing tower A3, where it comes into countercurrent contact with the circulating liquid (methanol or esters) sprayed at the top of the tower. The circulating liquid is drawn from the bottom of the tower by the first circulating pump 5, cooled to below 40°C by the first circulating liquid cooler 4, and then returned to the top of the tower, forming a closed loop. During this process, most of the alcohols, esters, aldehydes, and ethers are absorbed by the circulating liquid, and the wire mesh demister at the top of the tower captures gas-liquid droplets, reducing the escape of organic matter and reducing the organic matter content in the gas from 2%-9% to below 1.5%. The treated gas is then output through the first outlet pipeline 7. The outlet gas of scrubbing tower A3 is split through pressure reducing valve 8, with part of it entering the adsorption tower group as regeneration gas and the remainder entering scrubbing tower B9. Scrubbing tower B9 adopts the same circulation logic (second circulation pump 11 + second circulation liquid cooler 10) to further absorb residual organic matter. The wire mesh demister at the top of the tower demistes again to reduce the subsequent adsorption load. The liquid at the bottom of the tower is discharged through the second liquid level regulating valve 12 and the circulating liquid outlet pipe 13.

[0035] The washed gas enters the adsorption tower group (at least four towers) consisting of adsorption towers A37, B38, C39, D40, and E41 through the inlet pipe 57. Activated carbon, 5A molecular sieves, or 13X molecular sieves adsorb residual organic matter within the towers, concentrating it internally to form a gas-liquid mixture. When the organic matter content at the top of the adsorption tower approaches 0.01% (monitored by the outlet concentration sensor), the system switches to a new, regenerated adsorption tower via the first control valve 52 and the second control valve 53. The purified gas exiting the adsorption tower is preheated by the heat exchanger 35 and then heated to 150-180°C by the regeneration gas heater 36. It then enters the tower to be regenerated via the seventh control valve 48 and the eighth control valve 50, where backflushing desorbs the high-concentration organic gas-liquid mixture. The desorbed mixed gas enters the scrubbing tower B9 via the adsorption tower regeneration gas return pipe 34 and the fourth and fifth programmable control valves 55 and 56, where it is absorbed and liquefied by the circulating liquid. After regeneration, the adsorbent is cooled and switched to the next cycle via the third programmable control valve 47, etc. If the amount of regeneration gas is insufficient, nitrogen is introduced through the low-pressure nitrogen pipeline 43, the flow rate is controlled by the nitrogen flow regulating valve 44, and after being heated by the nitrogen heater 45, it is supplemented to the adsorption tower through the tenth programmable control valve 46.

[0036] The rich liquid (containing a large amount of organic matter) from washing tower A3 and washing tower B9 enters flash tower 14 through the first liquid level regulating valve 6 and circulating liquid outlet pipe 13 to remove light components. The top gas of flash tower enters the top condenser 29 of light component removal tower through the top outlet pipe 28 of flash tower. The bottom liquid enters light component removal tower 15. Light components (such as ethers) are condensed in the top condenser 29 of light component removal tower through the upper outlet pipe 16 of light component removal tower. Part of the light component is refluxed by the light component removal tower reflux pump 30, and the remainder is produced through the ether collection tank 31 and the product ether outlet pipe 32. The bottom liquid of light component removal tower enters heavy component removal tower 18 through the bottom outlet pipe 17 of light component removal tower. Heavy components (such as alcohols and esters) are condensed in the top condenser 27 of heavy component removal tower. Part of the heavy component is refluxed by the heavy component removal tower reflux pump 24, and the remainder is produced through the alcohol and ester collection tank 25 and the product alcohol and ester outlet pipe 26. The lean liquor at the bottom of the heavy removal tower is drawn out by the circulating washing liquor lean liquor reflux pump 21 and returned to the washing tower A3 and washing tower B9 for recycling through the second lean liquor reflux pipe 22 and the first lean liquor reflux pipe 23. The reboiler 19 of the light removal tower and the reboiler 20 of the heavy removal tower provide distillation heat sources for the two towers respectively.

[0037] After being treated by the adsorption tower group, the purified gas has an organic matter content of ≤0.01% and is sent to subsequent processes (such as methanol synthesis and ammonia synthesis) through the intermediate buffer tank 42 and cooling outlet pipe 59. A small amount of non-condensable gas is discharged through the non-condensable gas outlet pipe 33 or after combustion in a flare (meeting environmental standards). The control unit receives signals from the concentration sensor and controls the compressor 2, the first circulation pump 5, the second circulation pump 11, the regeneration gas heater 36, and the programmable valve group (such as the pressure boosting programmable valve 49, the ninth programmable valve 51, etc.) to achieve fully automatic operation.

[0038] The above specific embodiments are merely optional embodiments of this utility model. Based on the technical solution of this utility model and the relevant teachings of the above embodiments, those skilled in the art can make various alternative improvements and combinations to the above specific embodiments.

Claims

1. A mixed gas treatment and recovery system for organic compounds, characterized in that, include: A compression mechanism located on the raw gas conveying path is used to increase the pressure of the raw gas to a preset value; A washing assembly connected to the output end of the compression mechanism is used to absorb alcohols, esters, aldehydes, and ethers from the raw material gas through a circulating liquid; An adsorption tower group connected downstream of the washing assembly is used to further adsorb residual alcohols, esters, aldehydes, and ethers in the gas; The regeneration mechanism is located next to the adsorption tower group. The regeneration mechanism is used to regenerate the adsorption tower that is saturated with adsorption and recover the desorbed organic matter. A separation and purification component is connected downstream of the washing assembly and the adsorption tower assembly. The separation and purification component is used to separate and purify the recovered organic matter.

2. The mixed gas treatment and recovery system for organic compounds according to claim 1, characterized in that, The compression mechanism includes a raw gas pipeline (1) and a compressor (2). The input end of the compressor (2) is connected to the raw gas pipeline (1). The compressor (2) is used to pressurize the raw gas with a pressure lower than 1.5 MPa to above 1.5 MPa.

3. The mixed gas treatment and recovery system for organic compounds according to claim 2, characterized in that, The washing assembly includes a washing tower A (3) and a washing tower B (9) connected in series. The bottom of the washing tower A (3) is connected to a first circulating pump (5). The output end of the first circulating pump (5) is connected to a first circulating liquid cooler (4). The output end of the first circulating liquid cooler (4) is connected to the top of the washing tower A (3). The bottom of the washing tower B (9) is connected to a second circulating pump (11). The output end of the second circulating pump (11) is connected to a second circulating liquid cooler (10). The output end of the second circulating liquid cooler (10) is connected to the top of the washing tower B (9).

4. The mixed gas treatment and recovery system for organic compounds according to claim 3, characterized in that, Both the washing tower A (3) and the washing tower B (9) are equipped with wire mesh demisters at the top, and a pressure reducing valve (8) is connected between the washing tower A (3) and the washing tower B (9).

5. The mixed gas treatment and recovery system for organic compounds according to claim 4, characterized in that, The adsorption tower group includes at least four adsorption towers, each filled with an adsorbent selected from one or more of activated carbon, 5A molecular sieve and 13X molecular sieve. The inlet ends of the multiple adsorption towers are connected to adsorption tower inlet pipes (57), which are connected to the outlet of washing tower A (3).

6. The mixed gas treatment and recovery system for organic compounds according to claim 5, characterized in that, The regeneration mechanism includes a regeneration gas heater (36) and a heat exchanger (35). The outlet of the adsorption tower is connected in sequence to the heat exchanger (35) and the regeneration gas heater (36). The output end of the regeneration gas heater (36) is connected to the adsorption tower to be regenerated through a pipe. The bottom of the adsorption tower to be regenerated is connected to the adsorption tower regeneration gas return pipe (34). The adsorption tower regeneration gas return pipe (34) is connected to the scrubbing tower B (9).

7. The mixed gas treatment and recovery system for organic compounds according to claim 6, characterized in that, The regeneration mechanism also includes a low-pressure nitrogen pipeline (43), which is connected in sequence to a nitrogen heater (45) and a programmable valve group, which is connected to the adsorption tower.

8. The mixed gas treatment and recovery system for organic compounds according to claim 7, characterized in that, The separation and purification assembly includes a flash distillation tower (14), a light component removal tower (15), and a heavy component removal tower (18) connected in sequence. The flash distillation tower (14) is connected to the bottom of the washing tower A (3) and the washing tower B (9). The top of the light component removal tower (15) is connected to a light component removal tower top condenser (29), and the light component removal tower top condenser (29) is connected to an ether collection tank (31). The top of the heavy component removal tower (18) is connected to a heavy component removal tower top condenser (27), and the heavy component removal tower top condenser (27) is connected to an alcohol and ester collection tank (25).

9. The mixed gas treatment and recovery system for organic compounds according to claim 8, characterized in that, The bottom of the light removal tower (15) is equipped with a light removal tower reboiler (19), the bottom of the heavy removal tower (18) is equipped with a heavy removal tower reboiler (20), the bottom of the heavy removal tower (18) is connected to a circulating washing liquid lean liquid reflux pump (21), and the output end of the circulating washing liquid lean liquid reflux pump (21) is connected to washing tower A (3) and washing tower B (9).

10. The mixed gas treatment and recovery system for organic compounds according to claim 9, characterized in that, It also includes a control unit. The compressor (2), the first circulating pump (5), the second circulating pump (11), the regenerated gas heater (36), and the programmable valve group are all electrically connected to the control unit. A concentration sensor is installed at the outlet of the adsorption tower and is electrically connected to the control unit.

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