WO2017039131A1 - Système de recueil de gaz acides et procédé de recueil de gaz acides utilisant celui-ci - Google Patents

Système de recueil de gaz acides et procédé de recueil de gaz acides utilisant celui-ci Download PDF

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Publication number
WO2017039131A1
WO2017039131A1 PCT/KR2016/006713 KR2016006713W WO2017039131A1 WO 2017039131 A1 WO2017039131 A1 WO 2017039131A1 KR 2016006713 W KR2016006713 W KR 2016006713W WO 2017039131 A1 WO2017039131 A1 WO 2017039131A1
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Prior art keywords
acid gas
absorbent
reboiler
stripping column
stripping
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PCT/KR2016/006713
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English (en)
Korean (ko)
Inventor
곽노상
장경룡
심재구
이인영
이지현
이동욱
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한국전력공사
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Priority to CN201680032377.2A priority Critical patent/CN107743416B/zh
Publication of WO2017039131A1 publication Critical patent/WO2017039131A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/12—Washers with plural different washing sections
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20494—Amino acids, their salts or derivatives
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the present invention relates to an acid gas collection system and an acid gas collection method using the same.
  • Fossil fuels such as coal, petroleum, and LNG, which are used as energy sources in the industrial sector, generate acidic gases such as CO 2 , H 2 S, and COS during combustion.
  • acid gases especially carbon dioxide, have been identified as a major cause of global warming, and regulations on emissions and disposal are becoming more stringent.
  • the capture technology is classified into pre-combustion, in-combustion, and post-combustion methods according to the treatment position of carbon dioxide, and may be classified into absorption method, adsorption method, membrane separation method, deep cooling method, etc.
  • the general acid gas absorption and stripping system includes a regeneration step of performing a stripping process of separating the absorbent and carbon dioxide after injecting the absorbent absorbing the acid gas to the top of the stripping column.
  • the conventional acid gas absorption and stripping system consumes a lot of energy in the heat supply process for regenerating the absorbent, and there is a problem that additional equipment is required because the stripping efficiency is not high.
  • One object of the present invention is to use a steam condensate recycling apparatus connected to the reboiler in the process of separating and recovering the acid gas from the exhaust gas, the acid gas collection system that can reduce the heat consumption of the reboiler, and improve the economic efficiency and using the same It is to provide an acid gas collection method.
  • One embodiment of the present invention absorbs the acid gas contained in the exhaust gas in the absorbent to produce an acid gas saturated absorbent;
  • a first heat exchanger configured to heat up the acid gas saturating absorbent and the absorbent discharged from the stripping tower by first heat exchange;
  • a stripping column for separating the acid gas saturated absorbent into an acid gas and an absorbent;
  • a reboiler for supplying thermal energy to the stripping column using steam;
  • a condensate recycling apparatus for recycling steam condensate discharged from the reboiler. It relates to an acid gas collection system comprising a.
  • Another embodiment of the present invention relates to an acid gas collection method using the acid gas collection system described above.
  • Acid gas collection system of the present invention and acid gas collection method using the same by using a steam condensate recycling apparatus connected to the reboiler in the process of separating and recovering the acid gas from the exhaust gas, it is possible to reduce the heat consumption of the reboiler, and improve the economic efficiency have.
  • FIG. 1 is a view showing an acid gas collection system of the first embodiment of the present invention.
  • FIG. 2 is a view showing an acid gas collection system according to a second embodiment of the present invention.
  • FIG 3 is a view showing an acid gas collection system of a third embodiment of the present invention.
  • FIG. 4 is a view showing an acid gas collection system according to a fourth embodiment of the present invention.
  • FIG. 5 is a view showing an acid gas collection system of Comparative Example 1 of the present invention.
  • FIG. 6 illustrates a reboiler used in an embodiment of the present invention.
  • One embodiment of the present invention absorbs the acid gas contained in the exhaust gas in the absorbent to produce an acid gas saturated absorbent;
  • a first heat exchanger configured to heat up the acid gas saturating absorbent and the absorbent discharged from the stripping tower by first heat exchange;
  • a stripping column for separating the acid gas saturated absorbent into an acid gas and an absorbent;
  • a reboiler for supplying thermal energy to the stripping column using steam;
  • a condensate recycling apparatus for recycling steam condensate discharged from the reboiler. It relates to an acid gas collection system comprising a.
  • the acid gas collection system recycles steam condensate discharged from the reboiler, thereby remarkably reducing the reboiler heat consumption and improving economic efficiency.
  • the absorption tower reacts the chemical process gas and the combustion exhaust gas with the absorbent to produce an acid gas saturated absorbent in which the acid gas contained in the chemical process gas or the combustion exhaust gas is absorbed into the absorbent.
  • the acid gas may include one or more of carbon dioxide, hydrogen sulfide, sulfur dioxide, nitrogen dioxide and carbonyl sulfide.
  • the acid gas absorbent may include one or more of an amine-based, amino acid salt and inorganic salt solution.
  • the acid gas saturated absorbent may be a rich amine saturated with carbon dioxide.
  • the acid gas absorbent discharged to the bottom of the stripping column after the acidic gas saturated absorbent is stripped may be lean amine. In this case, the collection efficiency for acidic gas, especially for carbon dioxide may be excellent.
  • the washing zone may be installed in two or more stages in the absorption tower.
  • the absorption tower may include two to three stages or more of the cleaning stages, and in this case, the effect of preventing the loss of the absorbent may be improved.
  • the first heat exchanger heats up the acid gas saturated absorbent generated in the absorption tower by first heat exchange with the absorbent discharged from the stripping column.
  • the heat of the absorbent discharged from the bottom of the stripping column is supplied to the acid gas saturated absorbent to increase the energy efficiency, and the acid gas saturated absorbent is partially removed by the elevated temperature before the injection of the stripping column so as to remove the acid gas capture system.
  • the stripping efficiency can be improved.
  • the first heat exchanger may be heated to about 95 °C ⁇ 105 °C by first heat-exchanging the rich amine, the acid gas saturated absorbent with the lean amine from the bottom of the stripping column.
  • the amine absorbent when used, the collection efficiency of carbon dioxide in the acid gas may be further improved, and the stripping effect by the first heat exchange may be more excellent.
  • the acid gas saturated absorbent and the absorbent discharged from the stripping column may have a temperature difference of about 10 ° C. or less, for example, about 5 ° C. or less.
  • the heat exchange efficiency in the first heat exchanger and the effect of reducing the total energy usage of the acidic gas collection system can be further improved.
  • the first heat exchanger may include an inlet for introducing the absorbent discharged from the stripping tower and an outlet for sending the acid gas saturated absorbent heated after the heat exchange to a device of a next stage (such as a reboiler or stripping tower). In this case, it is more advantageous to perform heat exchange between the absorbent discharged from the stripper bottom and the acid gas saturated absorbent.
  • the stripping column receives an acid gas saturated absorbent and separates the acid gas and the absorbent.
  • the acidic gas saturated absorbent supplied to the stripping column may be in a state where some stripping is performed by performing a first heat exchange by the first heat exchange. In this case, the effect of reducing the total energy consumption of the acid gas collection system is more excellent.
  • the process of regenerating the acid gas saturated absorbent into the absorbent in the stripping column is performed by stripping reaction at a temperature of about 110 ° C. to 140 ° C. and a pressure of about atmospheric pressure, and supplies heat through a reboiler to maintain such regeneration conditions. Receive.
  • the reboiler supplies steam to the stripping column using steam. Specifically, the reboiler transfers the heat energy of the steam introduced from the outside to the acid gas saturated absorbent injected into the reboiler, and partially vaporizes it, and then some of the acid gas absorbents which have been heated without being vaporized with some of the acid gas absorbent vaporized. Thermal energy can be supplied by resupplying the gas absorbent into the stripping column. Through this, the stripping column may be supplied with thermal energy from the heated acid gas saturated absorbent to achieve a regeneration temperature condition.
  • the reboiler may be disposed between the stripping tower and the first heat exchanger or at a rear end of the stripping tower. This arrangement can reduce the amount of heat consumed to produce the steam used in the reboiler.
  • the reboiler when the reboiler is disposed between the stripping tower and the first heat exchanger, the reboiler is supplied with a saturated acid gas saturated absorber heated in the first heat exchanger to reheat it using steam,
  • the steam generated upon reheating may be resupplied to the upper region of the stripping column, and may serve to supply a portion of the remaining liquid acid gas saturated absorbent to the central region of the stripping column.
  • the reboiler supplies the reheated liquid acid gas to the central region of the stripping column to increase the utilization rate of the thermal energy of the stripping tower, to lower the thermal energy consumption of the reboiler, and to remove the water contained in the absorber inside the stripping column. It can prevent evaporation and induce stripping by diffusion.
  • the reboiler may further supply the reheated steam to the upper region of the stripping column to further improve the acid gas capture rate.
  • the reboiler 12 may be a kettle type reboiler, as shown in FIG. 6.
  • the kettle-type reboiler may be used as a reboiler in which boiling occurs on the shell side.
  • This reboiler 12 has the simplest structure and can easily obtain cheap steam.
  • the reboiler's bundle uses a U-tube type, a double head type, and a fixed type, and evaporation may occur well at the shell side, and vapor may be separated to separate liquid and gas. There is a thread. In the case of using such a reboiler, the applicability to the acid gas collection system of the present invention may be more excellent.
  • the condensate recycling apparatus may reduce the amount of thermal energy used by the acid gas collection system by recycling steam condensate discharged from the reboiler.
  • the condensate recycling apparatus may include one or more of a Thermal Vapor Recompression (TVR) apparatus or a stripping tower reheat heat exchanger.
  • TVR Thermal Vapor Recompression
  • the TVR (Thermal Vapor Recompression) device includes a flash drum (Flash drum) for separating the steam condensate generated in the reboiler into a gas and a liquid, and pressurizes the separated gas through the flash drum to supply to the reboiler steam It may be. In this case, the amount of heat used for steam supply of the reboiler can be reduced.
  • flash drum Flash drum
  • the stripping tower reheating heat exchanger (second heat exchanger) heats up the heat condensate generated from the reboiler and the absorbent discharged from the stripping column by heat exchange for a second heat exchanger, and the absorber heated by the second heat exchanger is heated to the upper portion of the stripping column. It may be to reflux.
  • the steam condensate is condensed by steam transferring heat to the acid gas saturated absorbent, but since the steam still contains residual heat, the stripping tower reheating heat exchanger (second heat exchanger) uses the residual heat in the middle of the stripping column.
  • the absorbent discharged can be further heated. In this case, heat can be additionally supplied to the stripping column, thereby further reducing the amount of energy consumed in the entire acid gas collection system.
  • the acidic gas collection system may include the stripping column reheat heat exchanger and the Thermal Vapor Recompression (TVR) device at the same time.
  • the steam condensate discharged from the reboiler is connected to the stripping column reheating heat exchanger to further increase the absorbent discharged from the stripping column, and then moves to the TVR unit including the flash drum to separate the gas and liquid. It can be reused as boiler steam.
  • the acid gas collection system may further include an ultrasonic device (Ultrasonic Horn) for regenerating the acid gas saturated absorbent prior to the stripping column injection.
  • the ultrasonic apparatus may remove the acid gas saturated absorbent before injection of the stripping column by using a cavitation phenomenon and particle acceleration effects.
  • the ultrasonic device may be disposed between the absorption tower and the reboiler or the first heat exchanger. In this case, the temperature of the acid gas saturated absorbent removed in advance by the ultrasonic device can be added to further remove the effect.
  • the ultrasonic device may be disposed between the reboiler or the first heat exchanger and the stripping column. In this case, an additional stripping effect can be added to the acid gas saturated absorbent heated by the reboiler.
  • the ultrasonic device may separate the acid gas, for example, in an ultrasonic band of about 20 KHz to about 1 MHz. In this case, the stripping effect performed by the ultrasonic device may be more excellent.
  • the acid gas collection system of Example 1 includes: an absorption tower 9 for absorbing acid gas contained in exhaust gas into an absorbent to generate an acid gas saturated absorbent; A first heat exchanger 10 configured to heat up the acid gas saturated absorbent and the absorbent discharged from the stripping column by first heat exchange; A stripping column 11 for separating the acid gas saturated absorbent into an acid gas and an absorbent; A reboiler (12) for supplying thermal energy to the stripping column using steam; And a condensate recycling apparatus for recycling steam condensate discharged from the reboiler.
  • FIG. 1 shows a washing apparatus 22 installed in two stages in a stripping column, a reboiler 12 is arranged in a rear end of the stripping column, and a TVR device 21 is installed in the reboiler 12.
  • An example of a capture system is shown. In this case, the steam supplied to the reboiler 12 is refluxed through the TVR apparatus 21, thereby reducing the heat consumption of the reboiler.
  • An acid gas collection system of Example 2 includes: an absorption tower 9 for absorbing acid gas contained in exhaust gas into an absorbent to generate an acid gas saturated absorbent; A first heat exchanger 10 configured to heat up the acid gas saturated absorbent and the absorbent discharged from the stripping column by first heat exchange; A stripping column 11 for separating the acid gas saturated absorbent into an acid gas and an absorbent; A reboiler (12) for supplying thermal energy to the stripping column using steam; And a condensate recycling apparatus for recycling steam condensate discharged from the reboiler.
  • Embodiment 2 shows a collection system of Embodiment 2 in which a reboiler 12 is disposed between a stripping column 11 and a first heat exchanger 10, and a stripping column reheating heat exchanger 18 is installed in the reboiler 12.
  • a reboiler 12 is disposed between a stripping column 11 and a first heat exchanger 10
  • a stripping column reheating heat exchanger 18 is installed in the reboiler 12.
  • the steam condensate generated from the reboiler 12 and the absorbent discharged from the stripping column are heated and heated to the second heat exchanger through the stripping column reheating heat exchanger, and the absorbent heated by the heat exchanger is refluxed to the upper portion of the stripping column.
  • the heat consumption of the reboiler can be further reduced, and the acid gas saturated absorbent can be further removed from the apparatus other than the stripping column, so that the regeneration efficiency of the absorbent can be further improved.
  • FIG. 3 is a view showing an acid gas collection system according to a third embodiment of the present invention.
  • FIG. 3 shows the acid gas collection system of Example 3 which was implemented in the same manner as in Example 2 except that an ultrasonic device (Ultrasonic Horn) was additionally installed between the reboiler 12 and the stripping column 11. In this case it is possible to add an additional stripping effect to the partially stripped acid gas saturated absorbent which is heated up by the first heat exchanger and the reboiler.
  • an ultrasonic device Ultrasonic Horn
  • FIG. 4 is a view showing an acid gas collection system according to a fourth embodiment of the present invention.
  • FIG. 4 shows the acid gas collection system of Example 4 which was carried out in the same manner as in Example 2 except that an ultrasonic device (Ultrasonic Horn) was further installed between the absorption tower 9 and the first heat exchanger 10. .
  • an ultrasonic device Ultrasonic Horn
  • the reboiler and the stripping column several times, a more excellent stripping effect can be added.
  • Another embodiment of the present invention relates to an acid gas collection method using the acid gas collection system of the above-described embodiment.
  • the omitted part of the description of the acid gas collection method of the present invention is replaced by the description of the acid gas collection system mentioned above.
  • the acid gas collecting method includes contacting the absorbent and the exhaust gas in the absorption tower 9 to collect the acid gas, and through this process, the absorbent and carbon dioxide exotherm to generate an acid gas absorbent liquid (acid gas saturated absorbent). .
  • the acid gas collection method includes heat-exchanging the acid gas saturated absorbent generated in the absorption tower 9 with the lean amine discharged from the lower part of the stripping column 11 by using the heat exchanger 10 to raise the temperature.
  • heat exchange of the acidic gas saturated absorbent and lean amine may be referred to as lean-rich heat exchange.
  • the acid gas collection method includes sending the acid gas saturated absorbent to the stripping column 11 to separate the acid gas and the absorbent by heat supplied from the stripping column.
  • the acid gas collection method includes supplying heat energy by supplying steam to the stripping column 11 using the reboiler 12.
  • the acid gas collection method may be disposed between the reboiler 12 between the heat exchanger 10 and the stripping column 11 to significantly reduce the amount of renewable energy consumed in the carbon dioxide capture process.
  • This acid gas collection method can increase the stripping efficiency while significantly reducing the reboiler heat consumption than when the reboiler is generated at the rear of the stripping column.
  • the acid gas collection method is to remove the acid gas saturated absorbent first by lean-rich heat exchange, and then secondary stripping through the reboiler in the step before injection of the stripping column, and to perform the third stripping through the stripping tower. Can be.
  • the first to third processes may further improve the stripping efficiency of the entire system as well as further increase the heating rate before being injected into the stripping column, thereby further improving the regeneration efficiency.
  • a TVR device to be described later is added to further reduce heat consumption, or additional quaternary stripping is performed using a stripping column reheat heat exchanger.
  • the acid gas collection system separates steam condensate generated after reheating the acid gas absorbent in the reboiler 12 into a gas and a liquid through a flash drum, and then separates the separated gas into a TVR (Thermal Vapor Recompression).
  • the method may further include repressurizing and supplying the reboiler steam.
  • the acid gas collection method uses a stripping tower reheating heat exchanger connected to a reboiler, heats up the heat condensate generated in the reboiler and the absorbent discharged from the stripping column, and heats up the absorbent heated by the heat exchanger. It may further comprise reflux to the top.
  • the acid gas collection method is further characterized in that the acid gas collection system is to regenerate the absorbent by separating the acid gas in the ultrasonic band of 20KHz ⁇ 1MHz using an ultrasonic device (Ultrasonic Horn) prior to injection of the saturated acid absorbent gas stripping tower It may include.
  • the ultrasonic apparatus may remove the acid gas saturated absorbent before injection of the stripping column by using a cavitation phenomenon and particle acceleration effects.
  • the acid gas collection system of Example 1 includes an absorption tower (9) including a storage tank for temporarily storing the absorbent heated by the exothermic reaction of the absorbent and carbon dioxide and separating the gas-liquid, and the acid gas saturated absorbent discharged from the absorption tower.
  • an absorption tower 9 including a storage tank for temporarily storing the absorbent heated by the exothermic reaction of the absorbent and carbon dioxide and separating the gas-liquid, and the acid gas saturated absorbent discharged from the absorption tower.
  • first heat exchanger (10), stripping column (11), stripping column (11) of supplying to the upper end of the stripping column after the first heat exchange with a high temperature absorbent (lean amine) discharged from the stripping column It is arranged to include a reboiler 12 connected to the rear end and a TVR device 21 connected to the reboiler.
  • the absorption tower was installed to include a washing stage in two stages, the steam condensed water from the reboiler to separate the gas and liquid through the flash drum 20 to pressurize only the gas to the Thermal Vapor Recompression (21). Resupply with boiler steam.
  • the acidic gas collection system of this Example 1 is shown in FIG.
  • the carbon dioxide concentration of the flue-gas before entering the absorption tower and passing through the absorption tower was measured using a gas analyzer, and the reboiler heat consumption per ton of carbon dioxide (ton) when the carbon dioxide removal rate was 90% was calculated. 1 is shown.
  • the acid gas collection system of Example 2 includes an absorption tower (9) including a storage tank for temporarily storing the absorbent and the absorbent heated by the exothermic reaction of carbon dioxide and separating the gas-liquid, and the acid gas saturated absorbent discharged from the absorption tower.
  • an absorption tower 9 including a storage tank for temporarily storing the absorbent and the absorbent heated by the exothermic reaction of carbon dioxide and separating the gas-liquid, and the acid gas saturated absorbent discharged from the absorption tower.
  • the absorbent liquid from the absorption tower is removed by passing the absorbent in the order of the first heat exchanger with the high temperature absorbent liquid from the stripping tower, and then passing through the absorbent in the order of the reboiler and the stripping column. It was then refluxed to the stripping column.
  • the acidic gas collection system of this Example 2 is shown in FIG.
  • the carbon dioxide concentration of the flue-gas before entering the absorption tower and passing through the absorption tower was measured using a gas analyzer, and the reboiler heat consumption per ton of carbon dioxide (ton) when the carbon dioxide removal rate was 90% was calculated. 1 is shown.
  • Example 3 was arranged by adding an ultrasonic device 19 between the reboiler 12 and the stripping column 11.
  • the absorption liquid exiting the absorption tower was subjected to the same method as in Example 2 except that the first heat exchange was performed with the high temperature absorption liquid from the stripping column, and further regenerated after the first heat exchange using the ultrasonic device 19.
  • the acidic gas collection system of this Example 3 is shown in FIG.
  • the carbon dioxide concentration of the flue-gas before entering the absorption tower and passing through the absorption tower was measured using a gas analyzer, and the reboiler heat consumption per ton of carbon dioxide (ton) when the carbon dioxide removal rate was 90% was calculated. 1 is shown.
  • Example 4 was disposed by adding the ultrasonic device 19 between the absorption tower 9 and the first heat exchanger 10. The absorption liquid exiting the absorption tower was removed in advance by an ultrasonic device and then carried out in the same manner as in Example 2 except for the first heat exchange.
  • An acidic gas collection system of this Example 4 is shown in FIG.
  • the carbon dioxide concentration of the flue-gas before entering the absorption tower and passing through the absorption tower was measured using a gas analyzer, and the reboiler heat consumption per ton of carbon dioxide (ton) when the carbon dioxide removal rate was 90% was calculated. 1 is shown.
  • the carbon dioxide concentration of the flue-gas before entering the absorption tower and passing through the absorption tower was measured using a gas analyzer, and the reboiler heat consumption per ton of carbon dioxide (ton) when the carbon dioxide removal rate was 90% was calculated. 1 is shown.
  • Examples 1 to 4 of the present invention was confirmed that the heat consumption of the reboiler used to capture the same carbon dioxide in the removal efficiency (90%) of the same carbon dioxide. These results indicate that the application of the absorption and stripping process developed in the present invention on the basis of the same carbon dioxide removal rate can significantly reduce the amount of steam used in the reboiler. On the other hand, in Comparative Example 1, which does not include a condensate recycling apparatus, it was found that the reboiler heat consumption was higher than that of Examples 1 to 4, which consumed a lot of process costs.
  • Examples 2 to 4 of the present invention could promote additional temperature increase and thereby absorbent regeneration in devices other than the stripping column, and the reboiler is disposed between the first heat exchanger and the stripping column to further remove stripping efficiency. Excellent and lower reboiler heat usage.
  • the acid gas collection system of Examples 1 to 4 can realize an excellent stripping efficiency even when the stripping tower height of the stripping tower is low, and can reduce the initial investment cost.
  • flue gas 2 regenerated absorbent (linamine)
  • cleaning stage 4 exhaust gas from which carbon dioxide has been removed

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)

Abstract

Un mode de réalisation de la présente invention concerne un système de recueil de gaz acides comprenant : une colonne d'absorption permettant d'absorber des gaz acides contenus dans les gaz d'échappement dans un absorbant pour générer un absorbant saturé en gaz acides ; un premier échangeur thermique permettant d'augmenter la température de l'absorbant saturé en gaz acides par le biais d'un premier échange thermique entre l'absorbant saturé en gaz acides et un absorbant évacué au niveau du pied d'une colonne de régénération ; la colonne de régénération permettant de séparer l'absorbant saturé en gaz acides en gaz acides et en un absorbant ; un rebouilleur permettant de fournir de l'énergie thermique à la colonne de régénération à l'aide de vapeur ; et un appareil de recyclage d'eau de condensat permettant de recycler l'eau de condensat de vapeur évacuée par le rebouilleur.
PCT/KR2016/006713 2015-09-04 2016-06-23 Système de recueil de gaz acides et procédé de recueil de gaz acides utilisant celui-ci WO2017039131A1 (fr)

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EP3887021A4 (fr) * 2018-11-30 2022-09-21 Carbonreuse Finland OY Système et procédé de récupération de dioxyde carbone
WO2023094670A1 (fr) 2021-11-29 2023-06-01 Totalenergies Onetech Régénération de solvants utilisés dans un procédé de capture de dioxyde de carbone

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CN110180330A (zh) * 2019-06-25 2019-08-30 中国石油大学(华东) 用于脱除废气中硫化物的新型吸收剂及其制备方法和应用
KR102234534B1 (ko) 2019-09-06 2021-03-31 삼성중공업 주식회사 배기관 장치 및 그를 포함하는 선박
KR20210109744A (ko) 2020-02-28 2021-09-07 삼성중공업 주식회사 배기가스 정화장치
CN114517846B (zh) * 2020-11-20 2024-05-28 中国石油化工股份有限公司 用于酸性气的水封系统和火炬燃烧系统

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KR20130139109A (ko) * 2012-06-12 2013-12-20 한국전력기술 주식회사 재기화기 스팀응축수의 열을 이용한 이산화탄소 포집장치
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3887021A4 (fr) * 2018-11-30 2022-09-21 Carbonreuse Finland OY Système et procédé de récupération de dioxyde carbone
WO2023094670A1 (fr) 2021-11-29 2023-06-01 Totalenergies Onetech Régénération de solvants utilisés dans un procédé de capture de dioxyde de carbone

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KR20170029086A (ko) 2017-03-15
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CN107743416B (zh) 2021-01-05

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