KR20140042393A - Apparatus for treating acidic gas and methof thereof - Google Patents

Abstract

The present invention relates to an apparatus for treating acidic gas and method thereof capable of Reducing the amount of steam consumption in a regeneration tower by generating and supplying high-temperature steam with the configuration of a flash drum and a compressor, preventing high temperature degradation and corrosion from being generated by exchanging heat with the flash drum not by immediately injecting hot steam to the regeneration tower, enhancing gas-liquid separation efficiency and the total amount of steam generation by raising operating temperature of the flash drum under reduced pressure. The apparatus for treating acidic gas comprises: an absorption tower removing carbon dioxide in exhaust gas inputted through a gas injection line by combining with an absorbent; a heat exchanger receiving the carbon dioxide absorbed absorbent through a pump to exchange heat; a regeneration tower stripping carbon dioxide chemically bonded to the heat exchanged absorbent; a condenser condensing mixed gas in which carbon dioxide discharged from the regeneration tower and moister are mixed; a gas-liquid separation device connected to the condensate to separate condensate to send the condensate back to the regeneration tower; a reboiler supplying thermal energy to the regeneration tower; a flash drum generating stream by flash -evaporating lean amine discharged from the bottom of the regeneration tower; a compressor compressing steam generated from the flash drum into high-temperature and high-pressure steam; and a heat exchanger lower the temperature of the carbon dioxide stripped regenerated absorbent supplied from the regeneration tower by the pump under the level of that in the absorption tower and supplying the regenerated absorbent to the absorption tower.

Description

Apparatus for treating acidic gas and methof

The present invention relates to an acid gas treatment apparatus and method, and more specifically, to configure a flash drum and a compressor to generate a high temperature steam and supply it into the regeneration tower to reduce the steam consumption in the regeneration tower, It is possible to prevent high temperature deterioration and corrosion by exchanging heat with the flash drum without directly inputting it to the regeneration tower, and by increasing the operating temperature of the flash drum, it is possible to increase the gas-liquid separation efficiency and increase the total vapor generation under the same reduced pressure conditions. The present invention relates to an acid gas treatment apparatus and method. article

Due to the increasing use of fossil fuels such as coal, petroleum, and LNG used in the energy industry since the early 19th century, the industrialization of acidic gases such as CO ₂ , CH ₄ , H ₂ S, and carbonyl sulfide (COS) The concentration sharply increased. These acid gases, especially carbon dioxide, have been found to warm the earth, and regulations on emissions and disposal are becoming more stringent worldwide. In June 1992, the United Nations Conference on Environment and Development in Rio, Brazil, raised international attention to global warming, and developed countries including the United States and Japan agreed to reduce global greenhouse gas emissions by 5.2% compared to 1990. There is international agreement on how to reduce acid gases.

Techniques to curb increased carbon dioxide emissions include energy saving technologies to reduce carbon dioxide emissions, carbon dioxide capture and storage (CCS) from emissions, technologies to use or immobilize carbon dioxide, and not to emit carbon dioxide. Alternative energy technologies.

Among them, CCS technology is recognized as the most effective technology for dealing with the large amount of greenhouse gases emitted from power plants and industrial facilities. Therefore, international powers such as G-8, Intergovernmental Panel on Climate Change (IPCC), and International Energy Agency (IEA) The organization actively encourages the development and use of technologies.

Among the CCS technologies, carbon dioxide capture technology is an important technology that accounts for a large part of the total cost. The technologies studied so far are divided into pre-combustion, in-combustion and post-combustion methods according to the treatment position of carbon dioxide. , Adsorption method, membrane separation method and deep cooling method.

Absorption method is suitable for large-capacity and low-density gas separation, so it is easy to be applied to most large industries and power plants, and the process of ABB lummus Crest is carried out in Trona, CA, USA) and Shady Point, Oklahoma, USA, and related technologies are disclosed in Korean Patent Publication No. 2010-35335.

1 is a block diagram of a general acid gas treatment apparatus.

As shown in FIG. 1, a general acidic gas treatment value includes an absorption tower 2 for removing carbon dioxide of exhaust gas input through a gas injection line 1 with an absorbent, and an absorbent 3 absorbing carbon dioxide. Heat exchanger (12) for receiving heat through the pump (9) for heat exchange, a regeneration tower (4) for removing carbon dioxide chemically bonded to the heat exchanged absorbent, and carbon dioxide discharged from the regeneration tower (4); A condenser (not shown) for condensing the mixed gas 8 of water vapor, and a gas-liquid separator (not shown) connected to the condenser (not shown) to separate condensate and supply it back to the regeneration tower 4; The reboiler 5 for supplying thermal energy to the regeneration tower 4 and the regeneration absorber 6 from which the carbon dioxide supplied by the pump 10 is removed from the regeneration tower 4 are lowered to the temperature of the absorption tower level. It comprises a heat exchanger (11) for supplying to the absorption tower (2).

The action of the general acidic gas treatment apparatus according to the above configuration is as follows.

The cooled exhaust gas of the gas injection line 1 flows into the absorption tower 2 and comes into contact with the absorbent 6 at a temperature of 40 to 60 ° C. In the process, carbon dioxide is combined with the absorbent 6 and removed.

The exhaust gas 7 from which carbon dioxide has been removed is discharged from the absorption tower 2 while preventing the absorbent or vapor from being splashed using the washing water circulated by the pump. The concentration of carbon dioxide in the exhaust gas 7 can be reduced by chemical reaction with the absorbent 6, but the absorption tower 2 must be high to maintain a low carbon dioxide concentration. The operating temperature of the absorption tower 2 may vary depending on the type of absorbent, for example, it may be maintained in the range of 40 ℃ to 60 ℃.

The absorbent (3) absorbing carbon dioxide by chemical bonding in the absorption tower (2) is transferred to the heat exchanger (12) through the pump (9) and heated by the heat exchanger (12), and thus the heat exchanger (12) The absorbent heated by is injected into the top of the regeneration tower 4.

In the regeneration tower 4, regeneration of the absorbent is performed at a high temperature (110-140 ° C) and a pressure of atmospheric pressure. In order to maintain such a high temperature regeneration condition, a heat source such as turbine steam is supplied from the reboiler 5, and heat energy is consumed in this process. Thermal energy supplied to the regeneration tower 4 strips carbon dioxide chemically bound to the absorbent.

The mixed gas 8 of carbon dioxide and water vapor thus removed from the absorbent is condensed in a condenser (not shown), separated into carbon dioxide gas and condensate in a gas-liquid separator (not shown), and the condensate is regenerated in a regeneration tower 4. Is supplied again.

The regenerated absorbent from which carbon dioxide has been removed is supplied to the heat exchanger 11 by the pump 10, and is lowered to the temperature of the absorption tower level through the heat exchanger 11 and then transferred to the absorption tower 2.

However, the conventional acidic gas treatment apparatus as described above has a problem in that high temperature deterioration and corrosion are caused by high temperature steam directly entering the regeneration tower.

An object of the present invention is to solve the conventional problems as described above, acid gas treatment that can prevent the high temperature deterioration and corrosion by heat exchange with the flash drum without directly inputting the high temperature steam to the regeneration tower An apparatus and method are provided.

Another object of the present invention is to provide an acid gas treating apparatus and method capable of increasing gas-liquid separation efficiency and increasing total vapor generation under the same reduced pressure by increasing the operating temperature of a flash drum.

As a means for achieving the above object, the configuration of the apparatus of the present invention, the absorption tower to remove the carbon dioxide of the exhaust gas input through the gas input line with the absorbent, and the absorber absorbing carbon dioxide through the pump through the heat exchanger A heat exchanger for regeneration, a regeneration tower for removing carbon dioxide chemically bonded to the heat-exchanging absorbent, a condenser for condensing the mixed gas of carbon dioxide and water vapor discharged from the regeneration tower, and a condenser connected to the condenser to separate and regenerate A gas-liquid separator for feeding back to the tower, a reboiler for supplying thermal energy to the regeneration tower, a flash drum for generating vapor by flash evaporating leanamine discharged from the bottom of the regeneration tower, and a steam generated from the flash drum Compressor compressed with high pressure steam and regeneration tower From lowering the regenerated sorbent is stripped of carbon dioxide to be supplied by the pump to the temperature of the absorber level preferably comprising including a heat exchanger for supplying the absorption tower.

The configuration of the apparatus of the present invention is preferably such that the flash drum is made of a stainless steel jacket type.

The configuration of the apparatus of the present invention is preferably such that the operating pressure of the flash drum is 0.1 to 1.0 barg.

In the configuration of the apparatus of the present invention, it is preferable that the operating pressure of the compressor is operated 0.1 to 0.5 barg higher than the operating pressure of the regeneration tower.

The structure of the method of the present invention is characterized in that (a) the mixed gas is introduced into the absorption tower; (C) the absorbent reacted with the acidic gas in the mixed gas in the absorption tower is transferred to the regeneration tower via a pump, (d) the high temperature steam or thermal energy produced by the lower reboiler in the regeneration tower. Separating the acid gas chemically bound to the absorbent by means of (e) transferring the absorbent (lean amine absorbent) from which carbon dioxide (CO ₂ ) has been removed by hot steam or thermal energy at the bottom of the regeneration tower to a flash drum. , (f) the high temperature and high pressure lean amine absorbents transferred to the flash drum were separated by vapor and liquid absorbents under reduced pressure, and the liquid absorbents were recycled to the absorption tower. (G) recompressing the steam delivered to the compressor into high temperature and high pressure steam by mechanical rotation; and (h) connecting the steam discharged from the compressor to an external jacket of the flash drum to Heat exchange, (i) the flash drum and the heat exchanged steam is preferably carried out including a step of re-transmitting to the regeneration tower.

As for the structure of the method of this invention, it is preferable that the said flash drum uses the jacket type of stainless material.

The configuration of the method of the present invention is preferably such that the operating pressure of the flash drum is operated at 0.1 to 1.0 barg.

In the configuration of the method of the present invention, it is preferable that the operating pressure of the compressor is operated 0.1 to 0.5 barg higher than the operating pressure of the regeneration tower.

As for the structure of the method of this invention, it is preferable to use amine type, amino acid salt, inorganic salt solution, ammonia water, etc. individually or in mixture as said absorbent.

The present invention reduces the amount of steam used in the regeneration tower by generating a flash drum and a compressor to generate high temperature steam and supplying it into the regeneration tower, and heat exchanges with the flash drum without directly supplying the high temperature steam to the regeneration tower. Deterioration and corrosion can be prevented from occurring, and by increasing the operating temperature of the flash drum, it is possible to increase gas-liquid separation efficiency and increase total vapor generation under the same reduced pressure conditions.

1 is a block diagram of a conventional acid gas treatment apparatus.
2 is a block diagram of an acid gas treatment apparatus according to an embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings, so that those skilled in the art can easily carry out the present invention. Other objects, features, and operational advantages, including the purpose, operation, and effect of the present invention will become more apparent from the description of the preferred embodiments.

It is to be understood that both the foregoing general description and the following detailed description of the present invention are exemplary and explanatory only and are not to be construed as limiting the scope of the invention as disclosed in the accompanying claims. It is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, is intended to cover various modifications and similarities, many of which are within the scope of the present invention.

Also, terms and words used in the description and claims of the present invention are defined based on the principle that the inventor can properly define the concept of a term in order to explain its invention in the best way, And should not be construed as limited to only the prior art, and should be construed in a meaning and concept consistent with the technical idea of the present invention. For example, the terms relating to directions are set on the basis of the position represented on the drawing for convenience of explanation.

2 is a block diagram of an acid gas treatment apparatus according to an embodiment of the present invention.

As shown in Figure 2, the configuration of the acid gas treatment apparatus according to an embodiment of the present invention, the absorption tower 23 for removing the carbon dioxide of the exhaust gas input through the gas injection line 21 by combining with the absorbent. And a heat exchanger 16 for receiving heat absorber 24 absorbing carbon dioxide through a pump 25 and heat exchanger 16, a regeneration tower 27 for removing carbon dioxide chemically bonded to the heat exchanged absorbent agent, A condenser (not shown) for condensing the mixed gas 32 of carbon dioxide and water vapor discharged from the regeneration tower 27 and a condenser (not shown) are separated to supply condensed water to the regeneration tower 32. A vapor-liquid separator (not shown), a reboiler (integrated with a regeneration tower) for supplying thermal energy to the regeneration tower 32, and a lean amine discharged from the bottom of the regeneration tower 27 to flash evaporate The flash drum 33 to be generated, the compressor 28 for compressing the steam generated from the flash drum 33 into steam of high temperature and high pressure, and the carbon dioxide supplied by the pump 29 from the regeneration tower 27 are removed. It comprises a heat exchanger (30) for lowering the regeneration absorbent (33) to the temperature of the absorption tower level to supply to the absorption tower (23).

The flash drum 33 is made of a stainless steel jacket type, the operating pressure is made of 0.1 to 1.0 barg.

The operating pressure of the compressor 28 is configured to operate 0.1 to 0.5 barg higher than the operating pressure of the regeneration tower 27.

In the acid gas treatment method according to the present invention, (a) the mixed gas is introduced into the absorption tower 23, (b) the mixed gas and the absorbent supplied to the absorption tower 23 is in counter-current contact in the mixed gas The acid value is selectively reacted with the absorbent, (c) the absorbent reacted with the acidic gas in the mixed gas in the absorption tower 23 is transferred to the regeneration tower 27 through the pump 25, (d) the regeneration tower Separating the acid gas chemically bound with the absorbent by hot steam or thermal energy generated in the lower reboiler in (27), (e) hot steam or thermal energy in the lower part of the regeneration tower 27 Transferring the absorbent (lean amine absorbent) from which carbon dioxide (CO ₂ ) has been removed to the flash drum (33), (f) reducing the high temperature and high pressure lean amine absorbent transferred to the flash drum 33, Liquid phase absorbent and then liquid absorption Recycle to the absorption tower 23, the generated steam is sent to the compressor 28, (g) the steam sent to the compressor 28 is recompressed into steam of high temperature and high pressure by mechanical rotation, ( h) heat exchange with the flash drum 33 by connecting the steam discharged from the compressor 28 to the outer jacket of the flash drum 33, (i) the steam having undergone heat exchange with the flash drum 33 is a regeneration tower 27 Retransmission).

The absorbent described above is an absorbent applicable to the wet acid gas treatment process, and may be used alone or in combination with an amine, an amino acid salt, an inorganic salt solution, and ammonia water.

With the above configuration, the operation of the acidic gas treating apparatus and method according to the embodiment of the present invention is as follows.

The process for treating acid gas can be divided into two stages in absorption tower and stripping column. Details of each step are as follows.

Stage 1: Absorption Tower

After the mixed gas containing the acidic gas is first cooled by the cooling device, the mixed gas is transferred to the lower portion of the absorption tower through the gas blower 22 to overcome the pressure drop generated by the absorption tower 23. The mixed gas transported through the gas blower 22 passes through the absorption tower 23 in the opposite direction to the absorbent, and chemically combines the acid gas and the absorbent in the exhaust gas. The interior of the absorption tower 23 constitutes a random or structured filler to improve the reactivity between the gaseous flue gas and the liquid absorbent.

As such, the mixed gas introduced into the absorption tower 23 chemically reacts with the absorbent, and the gas from which the acidic gas is removed passes through the scrubber at the top of the absorption tower, and a small amount of the absorbent and moisture contained in the gas are scrubbers. Is collected and recycled to the absorption tower 23, and the degassed gas 31 is discharged to the atmosphere. The operating temperature of the absorption tower 23 may vary depending on the type of absorbent used and the exhaust gas composition. Generally, the operation is performed in the range of 25 to 60 ° C.

Step 2: Play Tower

The acid gas saturated absorbent chemically reacted with the acid gas in the absorption tower 23 is preheated through the heat exchanger 26 and then supplied to the upper portion of the regeneration tower 27. The acid introduced into the upper portion of the regeneration tower 27 is absorbed. As the gas saturating absorber moves to the lower part of the regeneration tower 27, the acid gas is removed by steam or thermal energy generated by the reboiler (regeneration tower integrated) at the lower part of the regeneration tower 27, and the absorbent is regenerated. At the top of the regeneration tower 27, stripped acidic gas 32 containing water (H ₂ O) component is transferred to a cooler (not shown), where most of the steam is cooled to form a fluid in two phases of gas / liquid. Is generated and then transferred to a reflux drum (not shown).

Reflux drums (not shown) are phase separated into gaseous acid gases and condensate, which can then be transferred to recovery and treatment processes for storage or other useful high value chemicals depending on the application. The condensate is transported back to the top of the regeneration tower 27 through a reflux drum (not shown), and serves to clean the suspended matter present in the gas rising to the top of the regeneration tower 27.

The regenerated absorbent conveyed from the reboiler (integrated regeneration tower) is transferred to the upper portion of the absorption tower 23 through the heat exchanger 30 through the absorbent circulation pump 29. The operating temperature of the regeneration tower 32 may vary depending on the type of absorbent and the exhaust gas composition. Generally, the operation is performed in the range of 90 to 14 0 ° C.

A flash drum 33 and a compressor 28 are installed at the lower end of the regeneration tower 27 to flash evaporate the lean amine 34 discharged from the lower end of the regeneration tower 27 to generate steam, and generate the steam again. By supplying the regeneration tower 27 into the interior, the steam recompression process may be added to reduce the amount of steam used in the regeneration tower 27. The operating pressure of the regeneration tower 27 is preferably in the range of 1.5 to 2.5 barg for linkage with the steam recompression process. If the operating pressure is less than 1.5barg, it is not preferable because the amount of steam generated in the flash drum 33 is less after that, and if the operating pressure is more than 2.5barg, the operating cost increases because the amount of steam required for regenerating the absorbent is increased. Therefore, it is not preferable.

Pressure control of the flash drum 33 is finely adjusted using a globe valve or the like installed in the outlet line 33-2 connected to the compressor 28, and an operating pressure of 0.1 to 1.0 barg is appropriate. In the case where the operating pressure is less than 0.1 barg, since the compression ratio in the subsequent compression process increases, it is not preferable to apply a multistage compression process, and when operating at 1.0 barg or more, the steam generated in the flash drum 33 It is difficult to expect the effect of steam recompression technology because of the reduced amount.

Since the temperature of the steam 28-1 passing through the compressor 28 is very high, 170 degrees Celsius or higher, when high temperature steam is directly introduced into the regeneration tower 27, high temperature deterioration may occur and device corrosion may intensify. Not desirable

Therefore, the flash drum 33 is configured in the form of a stainless jacket, so that the hot steam generated through the compressor 28 is introduced into the outer jacket of the flash drum 33, thereby increasing the operating temperature of the flash drum 33. And heat exchange such that the hot steam temperature is relatively low. In the steam recompression technique, when the operating temperature of the flash drum 33 increases, the amount of steam generated under the same pressure increases, and consequently, the amount of steam used in the regeneration tower 27 may be reduced.

Example 1 Combustion gas was introduced at a flow rate of 2 m 3 / hr through the gas input line 21 at the bottom of the absorption tower 23. The temperature of the gas introduced into the absorption tower 23 was adjusted to 40 ° C so as to have the same value as the operating conditions discharged after the desulfurization tower of the coal-fired power plant, and the flow rate of the absorbent circulating in the process was fixed at 100 ml / min per minute. It was. The operating temperature and the operating pressure of the lower part of the regeneration tower 27 are 110 ° C, respectively. Adjust to 2.0 barg. The lean amine absorbent discharged from the bottom of the regeneration tower was then transferred to the flash drum 33, and the operating pressure of the flash drum 33 was adjusted to 0.5 barg so that the hot amine absorbent was reduced by the pressure reduction in the flash drum 33. Gas-liquid separation was made. The steam generated in the flash drum 33 is then introduced into the compressor 28, the operating pressure of the compressor 28 was operated at 2.5 barg. The high temperature and high pressure steam generated by the compressor 28 is then connected to the outer jacket of the flash drum 33 again, and the steam after heat exchange with the flash drum 33 is introduced into the regeneration tower 27 again. After performing the experiment for these conditions, the experimental results including the amount of steam used in the regeneration tower 27 is shown in Table 1 below.

<Example 2> In Example 1, except that the operating pressure of the flash drum 33 was operated at 1.0 barg, it was carried out in the same manner as in Example 1, in the regeneration tower 27 obtained through this Table 1 shows the steam consumption and other operating conditions.

<Comparative Example 1> In Example 1, except that the high-temperature, high-pressure steam generated by the compressor 28 is directly fed to the regeneration tower 23 without being transferred to the flash drum 33, Example 1 It was carried out in the same manner as shown in Table 1 shows the steam consumption and other operating conditions in the regeneration tower 27 obtained through this.

Comparative Example 2 In Example 1, except that steam generated through the flash drum 33 and the compressor 28 is directly introduced into the regeneration tower 27 without heat exchange with the flash drum 33, It was carried out in the same manner as in Example 1, it was shown in Table 1 the steam consumption and other operating conditions in the regeneration tower 27 obtained through this.

Whether to apply steam recompression Flash Drum Heat Exchanger Flash drum pressure
(barg) Flash drum
Temperature
(° C) Renewable Energy in Regeneration Tower
(GJ / tCO ₂ ) Example 1 ○ ○ 0.5 110 3.5 Example 2 ○ ○ 1.0 106 3.6 Comparative Example 1 X - - - 4.1 Comparative Example 2 ○ X 0.5 96 3.8

As a result of the analysis, it can be seen that in Example 1 and Example 2, compared to Comparative Example 1 of the same condition, the regeneration energy of the regeneration tower 27 is greatly reduced due to the use of steam by the addition of the flash drum 33. have. In addition, when there is no heat exchange with the flash drum 33 of Comparative Example 2, the temperature of the flash drum 33 was lower than 10 degrees compared with the case of Examples 1 and 2, resulting in reduced gas-liquid separation and steam Since the amount of generation is reduced, it can be seen that the effect of improving the renewable energy is lower than in Example 1 and Example 2.

Therefore, in the present invention, a flash drum and a compressor may be configured to generate vapor by flash evaporating lean amine discharged from the bottom of the regeneration tower, and to reduce the amount of steam used in the regeneration tower by supplying the generated steam back into the regeneration tower. .

In addition, the present invention by heat exchange with the flash drum without directly entering the high temperature steam passed through the compressor into the regeneration tower, there is a problem such as high temperature degradation and corrosion that may occur when the high temperature steam enters the regeneration tower directly In addition, by increasing the operating temperature of the flash drum to increase the gas-liquid separation efficiency under the same reduced pressure conditions and to increase the overall steam generation effect.

In addition, the present invention can not only improve the economics of the entire process as the amount of steam generated under the same pressure increases and the amount of steam injected into the regeneration tower is relatively reduced, and in the case of the existing process, it is discharged after steam recompression. Due to the high temperature of the steam is required to additionally configure the water supply tank and the auxiliary line, but the process according to the present invention is not necessary because the configuration of the process can be simplified.

23: absorption tower 27: regeneration tower
28: compressor 33: flash drum

Claims (4)

An absorption tower for removing the carbon dioxide of the exhaust gas input through the gas injection line by combining with the absorbent;
A heat exchanger for heat-exchanging the absorbent absorbing carbon dioxide through a pump,
A regeneration tower for removing carbon dioxide chemically bound to the heat exchanged absorbent,
A condenser for condensing the mixed gas of carbon dioxide and water vapor discharged from the regeneration tower,
A gas-liquid separator connected to the condenser to separate the condensate and supply it to the regeneration tower;
A reboiler that supplies thermal energy to the regeneration tower,
A flash drum for generating vapor by flash evaporating lean amine discharged from the bottom of the regeneration tower,
A compressor for compressing steam generated from the flash drum into steam of high temperature and high pressure;
And a heat exchanger for lowering the regeneration absorbent from which the carbon dioxide supplied by the pump from the regeneration tower is removed to a temperature of the absorption tower and supplying the regeneration absorber to the absorption tower. The method according to claim 1,
The flash drum is made of a stainless steel jacket type, the operating pressure of the flash drum is made of 0.1 to 1.0 barg, the operating pressure of the compressor is operated 0.1 to 0.5 barg higher than the operating pressure of the regeneration tower. Acid gas treatment apparatus, characterized in that. (a) introducing a mixed gas into the absorption tower;
(b) reacting the acid gas in the mixed gas selectively with the absorbent by countercurrent contacting the mixed gas and the absorbent supplied to the absorption tower,
(c) transferring the absorbent reacted with the acidic gas in the mixed gas in the absorption tower to the regeneration tower through a pump;
(d) separating the acid gas chemically bound to the absorbent by hot steam or thermal energy generated by the lower reboiler in the regeneration tower;
(e) transferring an absorbent (lean amine absorbent) from which carbon dioxide (CO ₂ ) has been removed by hot steam or thermal energy at the bottom of the regeneration tower to a flash drum,
(f) separating the high temperature and high pressure lean amine absorbent, which is transferred to the flash drum, into a vapor and a liquid absorbent by depressurizing it, and then recycling the liquid absorbent to the absorption tower and transferring the generated steam to a compressor.
(g) recompressing the steam delivered to the compressor into high temperature, high pressure steam by mechanical rotation,
(h) heat exchange with the flash drum by connecting steam discharged from the compressor to an outer jacket of the flash drum,
(i) the flash drum and the heat exchanged steam are re-transmitted to a regeneration tower. The method of claim 3,
The flash drum uses a jacket type of stainless material, the operating pressure of the flash drum is operated at 0.1 to 1.0 barg, the operating pressure of the compressor is operated to 0.1 to 0.5 barg higher than the operating pressure of the regeneration tower. Acid gas treatment method characterized in that.

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