Alcohol amine liquid deacidification regeneration system and process

Abstract

The invention provides an alcohol amine liquid deacidification regeneration system and process, the regeneration system comprises a regeneration tower, a regeneration reboiler, an acid gas collection unit, a control instrument and a control system, the top of the regeneration tower is communicated with the acid gas collection unit, the bottom of the regeneration tower is communicated with the regeneration reboiler, and the control instrument is communicated with the control system. The side line of a bottom tower plate of the regeneration tower is communicated with a heat circulation unit; the control instrument is installed on the pipeline, the control system is in electric signal connection with the control instrument, and the control instrument comprises a flow meter, a pressure sensor, a thermometer and a liquid level meter. The heat circulation unit is communicated with the side line of the bottom tower plate of the regeneration tower, so that the tower bottom hot steam of the regeneration tower is continuously recycled, only a small amount of hot steam is fed to the tower top for preheating, heat loss is avoided, the heat load of the regeneration tower is reduced by one order of magnitude, and a large amount of hot steam is prevented from being lost from the tower top; and the air cooler needs a large amount of load to cool the acid gas.

Description

Technical Field

[0001] The present invention belongs to the technical field of associated gas purification, and particularly relates to an alcohol amine solution deacidification and regeneration system and process. Background Art

[0002] H 2 S and CO 2 and other acidic components in the associated gas from oil fields will cause serious corrosion to pipelines, and there are potential safety hazards caused by leakage. Therefore, the improvement of the deacidification process in the field of associated gas purification has never stopped. At present, the mature alcohol amine method process is adopted for the deacidification of associated gas, and its main process flow is as follows: In the absorption tower, the associated gas containing acidic components such as H 2 S and CO 2 flows countercurrently from the bottom of the tower to contact with the alcohol amine solution from the top of the tower. The purified associated gas after removing the acid gas is sent from the top of the tower for further treatment. The rich alcohol amine solution that has absorbed H 2 S and CO 2 flows out from the bottom of the tower. The rich alcohol amine solution is sent to the top of the regeneration tower and is heated by the hot steam in the reboiler at the bottom of the tower. The acid gas is resolved from the alcohol amine solution, and the acid gas is sent out from the top of the tower, cooled, de-liquored and then further treated. The lean alcohol amine solution flowing out from the bottom of the regeneration tower is sent to the absorption tower for reuse.

[0003] The patent with the application number 202220368299.6 and the patent name "A Flue Gas Alcohol Amine Method Decarbonization Device System" publicly disclosed by the State Intellectual Property Office on February 23, 2022, uses alcohol amine solutions with different regeneration degrees to perform staged absorption on CO 2 in the flue gas. While ensuring the flue gas purification effect, it reduces the circulation volume of the regenerated alcohol amine solution, thereby reducing the energy consumption of the flue gas alcohol amine method decarbonization device system and achieving green energy conservation. Among them, the alcohol amine solution regeneration unit includes a regeneration tower, a regeneration gas condensation device and a regeneration gas separation device connected in sequence. The rich alcohol amine solution is changed into a lean alcohol amine solution through a large amount of heat exchange. This process has high purification degree and less hydrocarbon absorption, and is mature in industrial application. The disadvantage is that the energy consumption of the alcohol amine solution regeneration tower is high and a large amount of heat needs to be absorbed. Since the alcohol amine method process was developed early and is mature, it is the main choice for the current associated gas deacidification process. Summary of the Invention

[0004] The purpose of the present invention is to provide an alcohol amine solution deacidification and regeneration system to overcome the above technical problems existing in the prior art.

[0005] The purpose of the present invention is to provide an alcohol amine solution deacidification and regeneration process. By extracting a gas phase from the side line of the last tray at the bottom of the regeneration tower, the gas phase is re-pressurized and then recycled into the regeneration tower, and the hot steam rich in heat is recycled, thereby reducing the load.

[0006] To this end, the technical solution provided by the present invention is as follows: An amine solution deacidification and regeneration system includes a regeneration tower, a regeneration reboiler, an acid gas collection unit, control instruments, and a control system. The top of the regeneration tower is connected to the acid gas collection unit, the bottom of the regeneration tower is connected to the regeneration reboiler, and a heat circulation unit is connected to the side line of the bottom tray of the regeneration tower; The control instruments are installed on the pipelines, and the control system is electrically connected to the control instruments. The control instruments include a flow meter, a pressure sensor, a thermometer, and a liquid level gauge. The heat circulation unit includes a side line gas compressor, an electric valve I, and a flow meter I. The flow meter I is installed on the pipeline between the inlet of the side line gas compressor and the regeneration tower, the electric valve I is installed on the pipeline between the outlet of the side line gas compressor and the regeneration tower. Both the flow meter I and the electric valve I are electrically connected to the control system, and the electric valve I and the flow meter are interlocked through the control system.

[0007] The steam outlet of the regeneration reboiler is connected to the regeneration tower through a pipeline. The liquid phase outlet of the regeneration reboiler is connected to a heat exchanger through a pipeline, and the heat exchanger is connected to an absorption tower through a pipeline. The regeneration reboiler is respectively connected to a hot oil supply pipeline and a hot oil return pipeline through pipelines.

[0008] A liquid level gauge is installed on the regeneration reboiler, and an electric valve II is installed on the pipeline between the regeneration reboiler and the heat exchanger. Both the liquid level gauge and the electric valve II are electrically connected to the control system, and the electric valve II and the liquid level gauge are interlocked through the control system.

[0009] A thermometer I is installed on the pipeline between the acid gas collection unit and the regeneration tower, and an electric valve III is installed on the hot oil return pipeline. Both the electric valve III and the thermometer I are electrically connected to the control system, and the electric valve III and the thermometer I are interlocked through the control system.

[0010] The acid gas collection unit includes an acid gas air cooler, an acid gas after cooler, an acid gas separator, and an acid water reflux pump that are connected in sequence. The acid gas after cooler is respectively connected to a circulating water return pipeline and a circulating water supply pipeline; An electric valve IV is installed on the pipeline between the acid gas after cooler and the circulating water return pipeline. A thermometer II and a pressure sensor are installed on the pipeline between the acid gas after cooler and the acid gas separator. An electric valve V is installed on the gas phase outlet pipeline of the acid gas separator. The thermometer II, the pressure sensor, the electric valve IV, and the electric valve V are all electrically connected to the control system. The pressure sensor and the electric valve V are interlocked through the control system, and the thermometer II and the electric valve IV are interlocked through the control system.

[0011] An amine solution deacidification and regeneration process uses the amine solution deacidification and regeneration system and includes the following steps: Step 1) The rich alkanolamine solution from the absorption tower is transported to the top of the regeneration tower after heat exchange. Step 2) The hot steam in the regeneration reboiler enters the regeneration tower. Part of the gas phase in the regeneration tower is drawn out from the side line of the bottom tray of the regeneration tower, pressurized by the side line gas compressor, and then enters the regeneration tower. Step 3) The rich alkanolamine solution flowing from the top to the bottom of the regeneration tower is heated by the hot steam from the regeneration reboiler at the bottom of the tower, so that H 2 S and CO 2 are stripped out, and the rich alkanolamine solution becomes lean alkanolamine solution. Step 4) After the lean amine solution is gradually cooled by the heat exchanger, it is re-transported to the top of the absorption tower for recycling by the circulating pump.

[0012] During the process that part of the gas phase in the regeneration tower is drawn out from the side line of the bottom tray of the regeneration tower in Step 2), Flowmeter 1 detects the gas flow rate in real time and sends it to the control system. When the flow rate reaches the set value, the control system sends a signal to Electric Valve 1, and Electric Valve 1 opens. The gas phase pressurized by the side line gas compressor enters the regeneration tower.

[0013] Part of the gas phase in Step 2) is 70 - 80% of the volume of the hot steam entering the regeneration tower.

[0014] The beneficial effects of the present invention are as follows: By connecting a heat circulation unit to the side line of the bottom tray of the regeneration tower in the present invention, the hot steam at the bottom of the regeneration tower is continuously recycled. Only a small amount of hot steam rises to the top of the tower for preheating, avoiding heat loss, reducing the heat load of the regeneration tower by an order of magnitude, and preventing a large amount of hot steam from flowing out from the top of the tower, which may cause the temperature of the acid gas at the top of the tower to be too high and require a large load of the air cooler to cool the acid gas.

[0015] Due to adding a side line reflux process in the regeneration tower in the process of the present invention, compared with the original process flow, the CO in the top components of the tower 2 increases by 3.3%, and H 2 S increases by 2.1%. The load of the regeneration tower is reduced from 32.24 MW to 7.74 MW, and the load is relatively reduced by 76%. Description of the Drawings

[0016] Figure 1 is the process flow chart of an embodiment of the present invention; Figure 2 is the relationship curve diagram between the pressure of the gas phase pressurized by the side line gas compressor and the total load of the present invention.

[0017] In the figure: 1. Regeneration tower; 2. Acid gas air cooler; 3. Regeneration reboiler; 4. Acid gas after cooler; 5. Side line gas compressor; 6. Acid water reflux pump; 7. Acid gas separator; 8. Circulating water return pipeline; 9. Circulating water supply pipeline; 10. Hot oil supply pipeline; 11. Hot oil return pipeline; 12. Sewage treatment unit; 13. Thermometer 1; 14. Thermometer 2; 15. Liquid level gauge; 16. Pressure sensor; 17. Flowmeter 1; 18. Electric valve 1; 19. Electric valve 2; 20. Electric valve 3; 21. Electric valve 4; 22. Electric valve 5; 23. Flowmeter 2; 24. Electric valve 6. Detailed implementation mode

[0018] The following specific embodiments illustrate the implementation mode of the present invention. Those skilled in the art can easily understand other advantages and effects of the present invention from the content disclosed in this specification.

[0019] Now refer to the accompanying drawings to introduce the exemplary implementation mode of the present invention. However, the present invention can be implemented in many different forms and is not limited to the embodiments described here. These embodiments are provided to disclose the present invention in detail and completely, and to fully convey the scope of the present invention to those skilled in the relevant technical field. The terms in the exemplary implementation mode shown in the accompanying drawings are not limitations on the present invention. In the drawings, the same unit / element uses the same reference numeral.

[0020] Unless otherwise specified, the terms (including scientific and technical terms) used here have the ordinary meaning understood by those skilled in the relevant technical field. In addition, it can be understood that the terms defined in the commonly used dictionary should be understood as having a meaning consistent with the context of their relevant fields, and should not be understood as idealized or overly formal meanings.

[0021] Embodiment 1 This embodiment provides an alcohol amine solution deacidification and regeneration system, including a regeneration tower 1, a regeneration reboiler 3, an acid gas collection unit, control instruments and a control system. The top of the regeneration tower 1 is connected to the acid gas collection unit, the bottom of the regeneration tower 1 is connected to the regeneration reboiler 3, and the side line of the bottom tray of the regeneration tower 1 is connected to a heat circulation unit; The control instruments are installed on the pipeline, the control system is electrically connected to the control instruments, and the control instruments include a flowmeter, a pressure sensor 16, a thermometer and a liquid level gauge 15. Working principle: The rich alcohol amine solution coming from the absorption tower is transported into the top of the regeneration tower 1. The rich alcohol amine solution flowing from the top to the bottom of the regeneration tower 1 is heated by the hot steam from the regeneration reboiler 3 at the bottom of the tower, so that the H 2 S and CO 2The gas is stripped out, and the rich alkanolamine solution becomes a lean alkanolamine solution. The lean amine solution is retransported to the top of the absorption tower for recycling.

[0022] The difference from the prior art is that: a gas phase is drawn out from the side line of the last tray at the bottom of the regeneration tower 1, and the gas phase is recycled into the regeneration tower 1 after being repressurized. The principle of this process step is to recycle the hot steam rich in heat, thereby reducing the load.

[0023] Example 2 Based on Example 1, this example provides an alkanolamine solution deacidification and regeneration system, as Figure 1 shown. The heat recycling unit includes a side line gas compressor 5, an electric valve 1 18, and a flowmeter 1 17. The flowmeter 1 17 is arranged on the pipeline between the inlet of the side line gas compressor 5 and the regeneration tower 1. The electric valve 1 18 is arranged on the pipeline between the outlet of the side line gas compressor 5 and the regeneration tower 1. Both the flowmeter 1 17 and the electric valve 1 18 are electrically connected to the control system, and the electric valve 1 18 and the flowmeter are interlocked through the control system.

[0024] Part of the water vapor entering the regeneration tower 1 from the regeneration reboiler 3 enters the heat recycling unit. During this process, the flowmeter 1 17 real-time detects the gas phase flow rate and sends it to the control system. When the flow rate reaches the set value, the control system sends a signal to the electric valve 1 18, and the electric valve 1 18 opens. The gas phase pressurized by the side line gas compressor 5 enters the regeneration tower 1.

[0025] The control system in the present invention belongs to the prior art, such as a PLC controller. In order to verify that the heat recycling unit connected to the side line of the bottom tray of the regeneration tower 1 can reduce the load, this example is optimized and compared according to the Aspen HYSYS software simulation to obtain the loads under different pressurizations, as shown in Table 1 and Figure 2 . The specific process is as follows: Data input for HYSYS simulation calculation: The number of trays of the regeneration tower 1 is 12, the top pressure is controlled at 160 kPa, and the bottom pressure is controlled at 180 kPa. The rich alkanolamine solution (the number of trays entering the regeneration tower 1 is 6, the pressure is 200 kPa, and the temperature is 85 °C; the number of trays for acid water reflux is 1, and the reflux pressure is controlled at 300 kPa; the number of trays of the side line extraction gas outlet stream is 12, the flow rate is 2200 kmol / h, and it is adjusted through a flow control valve; the pressure of the side line extraction gas after pressurization is 230 kPa, and the number of trays of the tower where the side line extraction gas enters the tower after compression is the reboiler; the temperature of the stream cooled by the top air cooler is controlled at 50 °C. Table 1 Pressure and load after pressurization As can be seen from Table 1, under different pressurizations, the corresponding loads are different, and the load is reduced to the minimum when the compressor is pressurized to 230 KPa.

[0026] In the present invention, a heat circulation unit is connected to the side line of the bottom tray of the regeneration tower 1, so that the hot steam at the bottom of the regeneration tower 1 is continuously recycled. Only a small amount of hot steam rises to the top of the tower for preheating, avoiding heat loss, reducing the heat load of the regeneration tower 1 by an order of magnitude, and preventing a large amount of hot steam from escaping from the top of the tower, which may cause the temperature of the sour gas at the top of the tower to be too high and require a large load of the air cooler to cool the sour gas.

[0027] Example 3 Based on Example 1, this example provides an alcohol amine solution deacidification and regeneration system. The steam outlet of the regeneration reboiler 3 is connected to the regeneration tower 1 through a pipeline. The liquid phase outlet of the regeneration reboiler 3 is connected to a heat exchanger through a pipeline, and the heat exchanger is connected to the absorption tower through a pipeline. The regeneration reboiler 3 is respectively connected to a hot oil supply pipeline 10 and a hot oil return pipeline 11 through pipelines.

[0028] As Figure 1 shown, the hot oil heats the water in the regeneration reboiler 3 through the hot oil supply pipeline 10 to generate hot steam. The hot steam enters the regeneration tower 1, and the hot oil after heat exchange flows back to the hot oil heating unit through the hot oil return pipeline 11.

[0029] Example 4 Based on Example 3, this example provides an alcohol amine solution deacidification and regeneration system. A liquid level gauge 15 is installed on the regeneration reboiler 3, and an electric valve II 19 is installed on the pipeline between the regeneration reboiler 3 and the heat exchanger. Both the liquid level gauge 15 and the electric valve II 19 are electrically connected to the control system, and the electric valve II 19 and the liquid level gauge 15 are interlocked through the control system.

[0030] As Figure 1 shown, after the hot lean amine solution is gradually cooled by a heat exchanger (not shown in the figure), it is re-pumped into the top of the absorption tower for recycling using a circulation pump. During this process, the liquid level gauge 15 real-time detects the liquid level data of the lean amine solution in the regeneration reboiler 3 and sends it to the control system. When the liquid level reaches the upper limit, the control system sends a signal to the electric valve II 19, and the electric valve II 19 opens to allow the hot lean amine solution to enter the heat exchanger.

[0031] Example 5 Based on Example 3, this example provides an alcohol amine solution deacidification and regeneration system. A thermometer I 13 is installed on the pipeline between the sour gas collection unit and the regeneration tower 1, and an electric valve III 20 is installed on the hot oil return pipeline 11. Both the electric valve III 20 and the thermometer I 13 are electrically connected to the control system, and the electric valve III 20 and the thermometer I 13 are interlocked through the control system.

[0032] As Figure 1As shown, the thermometer 13 detects the outlet temperature of the sour gas in real time and sends it to the control system. When the temperature is higher than the set value, the control system sends a signal to the electric valve 20, causing the electric valve 20 to close, preventing the hot steam temperature from being too high, and thus reducing the load.

[0033] Embodiment 6 On the basis of Embodiment 1, this embodiment provides an alkanolamine solution deacidification and regeneration system. The sour gas collection unit includes a sour gas air cooler 2, a sour gas aftercooler 4, a sour gas separator 7, and a sour water reflux pump 6 that are connected in sequence. The sour gas aftercooler 4 is respectively connected to a circulating water return pipeline 8 and a circulating water supply pipeline 9; An electric valve 21 is installed on the pipeline between the sour gas aftercooler 4 and the circulating water return pipeline 8. A thermometer 14 and a pressure sensor 16 are installed on the pipeline between the sour gas aftercooler 4 and the sour gas separator 7. An electric valve 22 is installed on the gas phase outlet pipeline of the sour gas separator 7. The thermometer 14, the pressure sensor 16, the electric valve 21, and the electric valve 22 are all electrically connected to the control system. The pressure sensor 16 and the electric valve 22 are interlocked through the control system, and the thermometer 14 and the electric valve 21 are interlocked through the control system.

[0034] As Figure 1 shown, after the sour gas is cooled by the sour gas aftercooler, the thermometer 14 and the pressure sensor 16 respectively detect the temperature and pressure of the cooled sour gas in real time and send them to the control system. When the temperature exceeds the set value, the control system adjusts the opening degree of the electric valve 21 to make the temperature of the cooled sour gas meet the process requirements; when the pressure exceeds the set value, the control system sends a signal to the electric valve 22, and the electric valve opens to discharge the sour gas in time.

[0035] The sour water at the bottom of the sour gas separator 7 is discharged and flows through the sour water reflux pump 6 to the regeneration tower 1 for further separation or to the sewage treatment unit 12 (after the sour gas separation reaches the standard). When the flowmeter 23 detects that the acid liquid entering the regeneration tower 1 reaches the set value, the control system sends a signal to the electric valve 24 to cause the electric valve 24 to close.

[0036] Embodiment 7 An alkanolamine solution deacidification and regeneration process includes the following steps: Step 1) The rich alkanolamine solution from the absorption tower is transported to the top of the regeneration tower 1 after heat exchange; Step 2) The hot steam in the regeneration reboiler 3 enters the regeneration tower 1. Part of the gas phase in the regeneration tower 1 is drawn out from the side line of the bottom tower plate of the regeneration tower 1, pressurized by the side line gas compressor 5, and then enters the regeneration tower 1; Step 3) The rich alkanolamine solution flowing from the top to the bottom of the regeneration tower 1 is heated by the hot steam from the regeneration reboiler 3 at the bottom of the tower, so that the H in the rich alkanolamine solution 2S and CO 2 The stripping gas is removed, and the rich alkanolamine solution becomes a lean alkanolamine solution; Step 4) After the lean amine solution is gradually cooled by the heat exchanger, it is retransported to the top of the absorption tower for recycling by using a circulation pump.

[0037] Due to the addition of a side-stream reflux process in the regeneration tower 1 in the process of the present invention, compared with the original process flow, the CO in the top components 2 increases by 3.3%, and the H 2 S increases by 2.1%. The load of the regeneration tower 1 is reduced from 32.24 MW to 7.74 MW, and the load is relatively reduced by 76%.

[0038] In the process of part of the gas phase in the regeneration tower 1 being drawn out from the side line of the bottom tray of the regeneration tower 1, the flowmeter 17 detects the gas phase flow in real time and sends it to the control system. When the flow reaches the set value, the control system sends a signal to the electric valve 18, and the electric valve 18 opens. The gas phase pressurized by the side-stream gas compressor 5 enters the regeneration tower 1.

[0039] Part of the gas phase in Step 2) is 70-80% of the volume of the hot steam entering the regeneration tower 1.

[0040] Using the process of the present invention, the acid gas content output from the top of the regeneration tower 1 can reach 95-98%. The acid gas recovery rate is high, and the load of the regeneration reboiler 3 is low.

[0041] The above examples are only illustrative of the present invention and do not constitute a limitation on the protection scope of the present invention. Any design identical or similar to the present invention falls within the protection scope of the present invention.

Claims

1. An alcohol amine liquid deacidification regeneration system, characterized in that: It includes a regeneration tower, a regeneration reboiler, an acid gas collection unit, a control instrument and a control system. The top of the regeneration tower is connected to the acid gas collection unit, the bottom of the regeneration tower is connected to the regeneration reboiler, and the bottom plate side line of the regeneration tower is connected to a heat circulation unit; The control instrument is installed on the pipeline, the control system is connected with the control instrument by electrical signals, and the control instrument includes a flow meter, a pressure sensor, a thermometer and a liquid level meter.

2. The alcohol amine liquid deacidification regeneration system according to claim 1, characterized in that: The heat circulation unit includes a side-line gas compressor, an electric valve 1 and a flow meter 1. The flow meter 1 is arranged on the pipeline between the side-line gas compressor inlet and the regeneration tower. The electric valve 1 is arranged on the pipeline between the side-line gas compressor outlet and the regeneration tower. The flow meter 1 and the electric valve 1 are both connected to the control system electrical signal, and the electric valve 1 and the flow meter are interlocked through the control system.

3. The alcohol amine liquid deacidification regeneration system according to claim 1, characterized in that: The steam outlet of the regeneration reboiler is connected to the regeneration tower through a pipeline, the liquid phase outlet of the regeneration reboiler is connected to a heat exchanger through a pipeline, the heat exchanger is connected to the absorption tower through a pipeline, and the regeneration reboiler is connected to a hot oil inlet pipeline and a hot oil return pipeline through pipelines.

4. The alcohol amine liquid deacidification regeneration system according to claim 3, characterized in that: A liquid level gauge is installed on the regenerative reboiler, and an electric valve 2 is installed on the pipeline between the regenerative reboiler and the heat exchanger. The liquid level gauge and the electric valve 2 are both connected to the control system by electrical signals, and the electric valve 2 and the liquid level gauge are interlocked through the control system.

5. The alcohol amine liquid deacidification regeneration system according to claim 3, characterized in that: A thermometer 1 is installed on the pipeline between the acid gas collection unit and the regeneration tower, an electric valve 3 is installed on the hot oil return pipeline, the electric valve 3 and the thermometer 1 are both connected to the control system electrical signal, and the electric valve 3 and the thermometer 1 are interlocked through the control system.

6. The alcohol amine liquid deacidification regeneration system according to claim 1, characterized in that: The acid gas collection unit comprises an acid gas air cooler, an acid gas aftercooler, an acid gas separator and an acid water reflux pump which are connected in sequence, and the acid gas aftercooler is respectively connected with a circulating water return pipeline and a circulating water inlet pipeline; An electric valve four is installed on the pipeline between the acid gas aftercooler and the circulating water return pipeline, a thermometer two and a pressure sensor are installed on the pipeline between the acid gas aftercooler and the acid gas separator, and an electric valve five is installed on the gas phase outlet pipeline of the acid gas separator. The thermometer two, the pressure sensor, the electric valve four and the electric valve five are all connected with the control system by electrical signals, the pressure sensor and the electric valve five are interlocked through the control system, and the thermometer two and the electric valve four are interlocked through the control system.

7. Step 1) The alcohol amine solution from the absorption tower is transported to the top of the regeneration tower after heat exchange; Step 2) The hot steam in the regeneration reboiler enters the regeneration tower, wherein part of the gas phase in the regeneration tower is extracted through the side line of the bottom plate of the regeneration tower and enters the side line gas compressor for pressurization before entering the regeneration tower; Step 3) the alcohol-rich amine solution flowing from the top of the regeneration tower to the bottom is heated by the hot steam from the regeneration reboiler at the bottom of the tower, so that H2S and CO2 in the alcohol-rich amine solution are stripped out, and the alcohol-rich amine solution becomes an alcohol-lean amine solution; Step 4) After the lean amine solution is gradually cooled by the heat exchanger, it is re-transported to the top of the absorption tower for recycling using a circulation pump.

8. The deacidification and regeneration process of an alcohol amine solution according to claim 7, characterized in that: Step 2) During the process of partial gas phase in the regeneration tower being extracted through the side line of the bottom plate of the regeneration tower, flow meter 1 detects the gas phase flow in real time and sends it to the control system. When the flow reaches the set value, the control system sends a signal to electric valve 1, and electric valve 1 opens, and the gas phase pressurized by the side line gas compressor enters the regeneration tower.

9. The deacidification and regeneration process of an alcohol amine solution according to claim 7, characterized in that: The partial gas phase in step 2) is 70-80% of the volume of the hot steam entering the regeneration tower.

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