WO2012169192A1 - Dispositif d'élimination de dioxyde de carbone - Google Patents

Dispositif d'élimination de dioxyde de carbone Download PDF

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Publication number
WO2012169192A1
WO2012169192A1 PCT/JP2012/003722 JP2012003722W WO2012169192A1 WO 2012169192 A1 WO2012169192 A1 WO 2012169192A1 JP 2012003722 W JP2012003722 W JP 2012003722W WO 2012169192 A1 WO2012169192 A1 WO 2012169192A1
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WIPO (PCT)
Prior art keywords
exhaust gas
washing
water
amine compound
section
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PCT/JP2012/003722
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English (en)
Japanese (ja)
Inventor
宮本　英治
横山　公一
成仁 高本
島村　潤
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バブコック日立株式会社
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Publication of WO2012169192A1 publication Critical patent/WO2012169192A1/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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—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
    • B01D53/1412—Controlling the absorption process
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a carbon dioxide removal device. More specifically, the present invention is low-cost in that the amine compound is released into the atmosphere accompanying the exhaust gas from which carbon dioxide (CO 2 ) has been removed (hereinafter sometimes referred to as de-CO 2 exhaust gas). It is related with the carbon dioxide removal apparatus which can be suppressed as much as possible.
  • CO 2 carbon dioxide
  • Patent Document 1 Since the release of a large amount of amine compound is concerned about the influence on the environment, it is desired to suppress the concentration of the amine compound contained in the de-CO 2 exhaust gas to about several ppm.
  • a water washing section is provided at the upper part of the CO 2 absorption tower, and the reflux water of the regeneration tower is supplied to the water washing section to remove the CO 2 exhaust gas.
  • Patent Document 2 proposes to install a plurality of stages of the water washing section.
  • the reflux water in the regeneration tower is weakly acidic water containing CO 2 up to a saturation concentration, the amine compound absorbability is high.
  • the washing with refluxing water is useful in terms of suppressing the atmospheric release of the amine compound.
  • the concentration of the amine compound contained in the de-CO 2 exhaust gas may increase due to load fluctuation.
  • this requires large pump power and leads to an increase in utilities.
  • One possible measure is to add a strong acid such as sulfuric acid to the wash water.
  • An object of the present invention is that the amine compound entrained in the exhaust gas from which CO 2 has been removed to provide a carbon dioxide removal device can be suppressed as much as possible at low cost from being released into the atmosphere.
  • [2] of CO 2 is brought into contact with absorption liquid consisting of exhaust gas and the amine compound aqueous solution in the exhaust gas containing CO 2 is absorbed into the absorbing liquid to obtain a de-CO 2 exhaust gas step (1), A step (2a) of removing the amine compound accompanying the de-CO 2 exhaust gas by contacting the de-CO 2 exhaust gas obtained in the step (1) with washing water; A step (3) of heating the absorbing solution that has absorbed CO 2 obtained in step (1) to drive CO 2 out of the absorbing solution; A step of cooling the CO 2 expelled in the step (3) and condensing water accompanying the CO 2 ; Supplying the condensed water obtained in step (4) to step (2a) as washing water (5), The step of measuring the temperature of the wash water in step (2a) and the concentration of the amine compound contained in the wash water passed through step (2a), and estimating the concentration of the amine compound contained in the de-CO 2 exhaust gas passed through step (2a) (6b) and carbon dioxide having a step (7b) of adjusting the amount
  • the method further comprises a step (8a) of returning a part of the washing water having undergone the step (2a) to the step (2a) and joining the remaining portion to the absorbent having undergone the step (1).
  • the method of description [4]
  • the method further comprises the step (8b) of returning a part of the washing water that has passed through the step (2a) to the step (2a) and joining the remaining part to the absorbent used in the step (1).
  • step (2)a the de-CO 2 exhaust gas obtained in step (1) is brought into contact with the wash water that has passed through step (2a) to be entrained in the de-CO 2 exhaust gas. Further comprising at least one step (2b) of removing compounds, The method according to [1] or [2], wherein the de-CO 2 exhaust gas obtained through step (2b) is supplied to step (2a) instead of the de-CO 2 exhaust gas obtained in step (1).
  • a CO 2 absorber having a function of obtaining a de-CO 2 exhaust gas by countercurrently contacting an exhaust gas containing CO 2 and an absorption liquid composed of an aqueous amine compound solution to absorb CO 2 in the exhaust gas into the absorption liquid;
  • a cleaning unit having a function of removing an amine compound of de CO 2 exhaust gas obtained in the CO 2 absorbing section by the washing water and the flow contact entrained in de CO 2 gas,
  • An absorption liquid regeneration unit having a function of heating the absorption liquid that has absorbed CO 2 obtained in the CO 2 absorption part to drive CO 2 out of the absorption liquid;
  • a condenser having a function of condensing the water entrained in the CO 2 cooled the CO 2 expelled in the absorbent solution regeneration section,
  • a pipe for supplying the condensed water obtained in the condenser to the washing section as washing water;
  • a CO 2 absorber having a function of obtaining a de-CO 2 exhaust gas by countercurrently contacting an exhaust gas containing CO 2 and an absorbing solution composed of an amine compound aqueous solution to absorb CO 2 in the exhaust gas into the absorbing solution;
  • a cleaning unit having a function of removing an amine compound of de CO 2 exhaust gas obtained in the CO 2 absorbing section by the washing water and the flow contact entrained in de CO 2 gas,
  • An absorption liquid regeneration unit having a function of heating the absorption liquid that has absorbed CO 2 obtained in the CO 2 absorption part to drive CO 2 out of the absorption liquid;
  • a condenser having a function of condensing the water entrained in the CO 2 cooled the CO 2 expelled in the absorbent solution regeneration section,
  • a pipe for supplying the condensed water obtained in the condenser to the washing section as washing water;
  • the amine compound accompanying the de-CO 2 exhaust gas obtained in the CO 2 absorbing section by washing water countercurrent contact through the cleaning section to the de-CO 2 gas At least one additional cleaning section having the function of removing,
  • a pipe for returning a part of the washing water that has passed through the washing part to the washing part and supplying the remaining part to the additional washing part The apparatus according to [12], further including a pipe that returns a part of the washing water that has passed through the additional washing section to the additional washing section and joins the remaining portion to the absorbing solution that has passed through the CO 2 absorption section.
  • the apparatus according to [12] further including a pipe that returns a part of the washing water that has passed through the additional washing unit to the additional washing unit, and joins the remaining part to the absorbent used in the CO 2 absorption unit.
  • the carbon dioxide removal method and the carbon dioxide removal apparatus of the present invention it is possible to suppress the amine compound from being released into the atmosphere accompanying the exhaust gas from which CO 2 has been removed as much as possible at a low cost.
  • exhaust gas (for example, combustion exhaust gas) 11 containing CO 2 is supplied to the absorption tower 1 through a line 3.
  • the pressure of the exhaust gas containing CO 2 may be normal pressure or pressurized, and is preferably normal pressure.
  • the temperature of the exhaust gas containing CO 2 is not particularly limited, and may be low or high.
  • Exhaust gas containing CO 2 is brought into counter-current contact with an aqueous amine compound solution (hereinafter also referred to as absorption liquid) having a constant concentration supplied from the nozzle 6 in the CO 2 absorption section 2.
  • absorption liquid aqueous amine compound solution having a constant concentration supplied from the nozzle 6 in the CO 2 absorption section 2.
  • the CO 2 in the exhaust gas 11 is absorbed and removed by the absorbing solution, and the obtained de-CO 2 exhaust gas goes to the cleaning unit 24b.
  • amine compounds contained in the absorption liquid include monoethanolamine, alcoholic hydroxyl group-containing primary amines such as 2-amino-2-methyl-1-propanol, and alcoholic hydroxyl groups such as diethanolamine and 2-methylaminoethanol. Containing secondary amines, alcoholic hydroxyl group-containing tertiary amines such as triethanolamine and N-methyldiethanolamine, polyethylene polyamines such as ethylenediamine, triethylenediamine and diethylenetriamine, piperazines, piperidines and pyrrolidines Examples include cyclic amines, polyamines such as xylylenediamine, amino acids such as methylaminocarboxylic acid, and the like, and mixtures thereof. Further, the absorbing liquid may contain a CO 2 absorption accelerator, a corrosion inhibitor, and methanol, polyethylene glycol, sulfolane and the like as other media.
  • the absorbing liquid that has absorbed CO 2 has a higher temperature than the temperature in the nozzle 6 due to the heat of absorption.
  • the absorbing solution that has absorbed CO 2 is extracted from the line 10, heated by the heat exchanger 22, and then supplied to the regeneration tower 13.
  • the absorption liquid evaporates due to heating by the reboiler 23, the vapor and the absorption liquid supplied from the nozzle 14 come into countercurrent contact in the lower absorption liquid regeneration section 15, and CO 2 is expelled from the absorption liquid.
  • the absorption liquid from which CO 2 has been purged (regenerated) is extracted from the bottom of the regeneration tower, cooled by the heat exchanger 22, and returned to the absorption tower 1.
  • the CO 2 was expelled from the absorbing solution is brought into contact with reflux water supplied from the nozzle 20, to remove the absorbing solution accompanying the CO 2 from the CO 2.
  • CO 2 is cooled by the cooler 19 to condense the water accompanying the CO 2 .
  • the CO 2 separator 17 separates condensed water (hereinafter sometimes referred to as reflux water) and CO 2, and the CO 2 is supplied to the CO 2 recovery step through the line 18.
  • a part of the reflux water is refluxed to the regeneration tower 13 by the pump 16.
  • the remainder of the reflux water is supplied to the absorption tower 1 through the line 21.
  • the de-CO 2 exhaust gas obtained in the CO 2 absorption unit 2 and the reflux water (hereinafter sometimes referred to as “washing water”) are brought into counter-current contact with the washing unit 24a and the washing unit 24b. This makes it possible to remove the amine compound accompanying the de-CO 2 gas from the de-CO 2 gas.
  • the cleaning units 24a and 24b may be a packed bed or a shelf type. In FIG. 1, the cleaning unit is provided in two stages, but it may be one stage or three or more stages.
  • Demisters may be installed in the CO 2 absorption unit 2 and the cleaning units 24a and 24b. By installing the demister, a part of the absorption liquid mist supplied to the CO 2 absorption unit 2 and a part of the washing water mist supplied to the cleaning units 24a and 24b are discharged to the outside of the tower together with the de-CO 2 exhaust gas. And the loss of the amine compound can be prevented.
  • cooler 19 In the apparatus shown in FIG. 1, only one cooler 19 is provided above the regeneration tower 13, but two or more coolers 19 may be provided in series.
  • the cooler 19 is composed of two units, the reflux water from the first cooler is supplied from the regeneration tower side to the first-stage washing unit 24b, and the reflux water from the second cooler is two-stage. Supplying to the eye washing part 24a is preferable from the viewpoint of the removal efficiency of the amine compound.
  • a part of that is part of the upstream side of that stage (that is, the side closer to the absorbing part) May be supplied to the stage).
  • a part of the cleaning water that has passed through the cleaning unit 24a can be returned to the cleaning unit 24a through the cooler 8a, and the remaining cleaning water that has passed through the cleaning unit 24a can be supplied to the cleaning unit 24b.
  • the amount supplied to the washing unit 24b can be adjusted based on the concentration of the amine compound contained in the washing water that has passed through the washing unit 24a. For example, when the concentration of the amine compound contained in the washing water exceeds a predetermined value In addition, the remainder can be supplied to the cleaning unit 24b.
  • a part of the concentration may be supplied to the absorption liquid supplied from the regeneration tower. . Specifically, a part of the washing water that has passed through the washing unit 24b is returned to the washing unit 24b through the cooler 8b, and the remaining part is merged with the absorption solution that has passed through the CO 2 absorption unit 2 or the absorption solution that is supplied from the nozzle 6. Can do.
  • the amount to be merged with the absorption liquid that has passed through the CO 2 absorption section 2 or the absorption liquid supplied from the nozzle 6 can be adjusted based on the concentration of the amine compound contained in the cleaning water that has passed through the cleaning section 24b. When the concentration of the amine compound contained in the water exceeds a predetermined value, the remaining part can be merged with the absorption liquid supplied from the nozzle 6.
  • the concentration of the carbonate ion contained in the washing water that has passed through the washing section 24a and / or the concentration of the amine compound contained in the de-CO 2 exhaust gas that has passed through the washing section 24a is measured.
  • the measuring means is not particularly limited. Examples thereof include gas chromatography, liquid chromatography, ion chromatography, ICP emission spectroscopic analysis / mass spectrometry, and the like.
  • the carbonate ion concentration may be measured on-line with the measuring device 28a by extracting the washing water almost continuously from the line 26a, or it may be measured off-line with the measuring device by extracting the washing water from the line 26a at a predetermined time interval. May be.
  • the amine compound concentration may be measured on-line with the measuring device 28b by extracting the de-CO 2 exhaust gas almost continuously from the line 4, or with the measuring device by extracting the de-CO 2 exhaust gas from the line 4 at a predetermined time interval. You may measure offline.
  • the measured carbonate ion concentration and / or amine compound concentration data is sent to the control device 30 through the signal lines 29a and / or 31.
  • the degree of deviation is estimated by comparing the measured carbonate ion concentration and / or amine compound concentration with the control target concentration set to a predetermined value.
  • the adjustment range of the flow rate of the cleaning water is calculated by a known control algorithm such as PID control, and the value is transmitted as a control signal to the flow rate adjusting means.
  • the flow rate adjusting means 27 that has received the control signal adjusts the valve opening and the like in accordance with the signal to change the flow rate of the cleaning water supplied to the cleaning unit 24a.
  • from the concentration measurement to the flow rate change is performed by online automatic control, but from the concentration measurement to the flow rate change may be performed by offline manual control.
  • the reflux water from the cooler 19 contains CO 2 to a concentration close to saturation at that temperature. For example, when the temperature of the reflux water is 40 ° C., about 400 ppm of CO 2 is contained.
  • Reflux water washing section of the absorption tower 1 is supplied, the de-CO 2 to the exhaust gas and the countercurrent contact, the amine contained in the de-CO 2 exhaust gas generates the amine carbonate reacts with CO 2 contained in the wash water.
  • amine carbonate has a higher boiling point than amine.
  • the amine absorption rate from the de-CO 2 exhaust gas into the wash water decreases, and the amine concentration in the de-CO 2 exhaust gas does not decrease sufficiently.
  • the flow rate of the washing water in countercurrent contact with the de-CO 2 exhaust gas it is possible to promote gas-liquid contact and increase the amine absorption rate.
  • the amine absorption rate from the de-CO 2 exhaust gas to the wash water is optimized, and the amine concentration in the de-CO 2 exhaust gas is determined by the economical use of the wash water and power consumption. Can be less than or equal to the value.
  • the temperature of the absorption liquid supplied to the absorption tower 1 is adjusted by the heat exchanger 22, but a cooler may be further provided between the heat exchanger 22 and the absorbent supply port 6 as necessary.
  • the temperature of the absorption liquid supplied to the absorption tower 1 is usually constant, so that the temperature of the de-CO 2 exhaust gas hardly rises due to the absorbed heat, and the combustion exhaust gas supply port Therefore, the absorption tower 1 is raised and discharged at substantially the same temperature as that in FIG.
  • the same is not a strict meaning, and it is included in the same range in a state where the water balance of the absorption tower 1 is maintained even if a slight temperature difference occurs.
  • the amine compound can be released out of the system by the apparatus and method of the present invention using the reflux water from the regeneration tower 13 for the absorption tower 1. To be prevented.
  • the apparatus shown in FIG. 2 is the same as the apparatus shown in FIG. 1 except that the measurement value that is the basis of the flow rate adjustment is different.
  • the temperature of the cleaning water in the cleaning unit 24a and the concentration of carbonate ions contained in the cleaning water that has passed through the cleaning unit 24a are measured.
  • the concentration measuring means is the same as that in the apparatus shown in FIG.
  • the temperature can be measured with a known temperature sensor such as a thermocouple.
  • the measured temperature and carbonate ion concentration data is sent to the controller 30 through signal lines 29d and 34.
  • the concentration of the amine compound contained in the de-CO 2 exhaust gas that has passed through the cleaning layer 24a is estimated from the measured temperature and carbonate ion concentration.
  • the method of estimation is not particularly limited. For example, since the vapor pressure of the amine compound is determined by the temperature of the washing water, the concentration of the amine compound contained in the gas phase can be estimated from the concentration of the amine compound contained in the washing water and the vapor pressure. The degree of deviation is estimated by comparing the estimated value with the control target value set to a predetermined value. From the estimation result, the adjustment range of the flow rate of the cleaning water is calculated by a known control algorithm such as PID control, and the value is transmitted as a control signal to the flow rate adjusting means.
  • PID control a known control algorithm
  • the flow rate adjusting means 27 that has received the control signal adjusts the valve opening and the like in accordance with the signal to change the flow rate of the cleaning water supplied to the cleaning unit 24a.
  • from the concentration measurement to the flow rate change is performed by online automatic control, but from the concentration measurement to the flow rate change may be performed by offline manual control.
  • the amine absorption rate from the de-CO 2 exhaust gas to the wash water is optimized, and the amine concentration in the de-CO 2 exhaust gas is determined by the economical use of the wash water and power consumption. Can be less than or equal to the value.
  • CO 2 was supplied to the flue gas 30 Nm 3 / h containing 10% CO 2 absorbing section 2 of the absorption tower 1 was monoethanolamine 30% by weight aqueous solution (absorption solution) by countercurrent contact to absorb CO 2.
  • the de-CO 2 exhaust gas obtained in the CO 2 absorption unit 2 was brought into countercurrent contact with the cleaning water at a liquid / gas ratio (hereinafter referred to as L / G) of 2 L / Nm 3 in the cleaning unit 24b.
  • L / G liquid / gas ratio
  • the de-CO 2 exhaust gas was brought into counter-current contact with the cleaning water at a liquid / gas (L / G) ratio of 2 L / Nm 3 in the cleaning section 24a.
  • the de-CO 2 exhaust gas was discharged out of the system through a demister provided in the upper part of the cleaning unit 24a.
  • a two-stage cooler was provided at the top of the regeneration tower 13.
  • the inlet gas temperatures in the first stage cooler (not shown) and the second stage cooler were 100 ° C. and 70 ° C., respectively.
  • Condensed water from the first stage cooler is supplied at 0.5 L / h as cleaning water to the first stage cleaning section 24b of the absorption tower 1, and condensed water from the second stage cooler is absorbed at 0.6 L / h. This was supplied as cleaning water to the first second-stage cleaning unit 24a.
  • the gas temperature at the outlet of the second stage cooler was 30 ° C.
  • the combustion exhaust gas flow rate is decreased from 30 Nm 3 / h to 15 Nm 3 / h, since the carbonate ion concentration in the wash water in the cleaning section 24a is increased to 0.1 mol / L, and the washing water of the washing unit 24a de the flow rate ratio L / G of CO 2 exhaust gas by adjusting the opening of the valve 27 has been changed from 2L / Nm 3 in 1L / Nm 3.
  • the concentration of the amine compound contained in the de-CO 2 exhaust gas in the line 4 did not increase, and the pump power for washing water circulation could be reduced to about 1 ⁇ 2.
  • the flow rate ratio L / G of the cleaning water and de-CO 2 exhaust gas in the cleaning unit 24 a is set to the opening degree of the valve 27. It was adjusted and changed from 2 L / Nm 3 to 4.0 L / Nm 3 . As a result, the amine compound concentration contained in the de-CO 2 exhaust gas in line 4 was reduced to 2 ppm.
  • CO 2 was fed to the CO 2 absorbing section of the absorption tower flue gas 30 Nm 3 / h containing 10 percent aqueous solution containing monoethanolamine 30% by weight (absorbing liquid) by countercurrent contact to absorb CO 2.
  • the de-CO 2 exhaust gas obtained in the CO 2 absorption part was brought into counter-current contact with the cleaning water at a cleaning part having a one-stage configuration at a liquid / gas ratio (hereinafter referred to as L / G) of 2 L / Nm 3 .
  • L / G liquid / gas ratio
  • the de-CO 2 exhaust gas was discharged out of the system through a demister provided at the outlet of the cleaning section.
  • a single-stage cooler was provided at the top of the regeneration tower. The inlet gas temperature of the cooler was 100 ° C.
  • Condensed water from the cooler was supplied at 1.1 L / h to the washing section of the absorption tower as washing water. After reaching a steady state, 10 ml of washing water from the washing section was extracted and the carbonate ion concentration was measured by ion chromatography to be 0.03 mol / L. The amine compound concentration measured by gas chromatography was 0.2 mol / L. The temperature of the washing water in the washing part was 40 ° C. The amine concentration in the gas corresponding to the saturated vapor pressure of monoethanolamine was estimated to be 10 ppm from the vapor-liquid equilibrium.
  • the combustion exhaust gas flow rate is reduced to 15 Nm 3 / h, since the carbonate ion concentration in the washing water of the washing unit is increased to 0.1 mol / L, the washing water of the washing unit and the de-CO 2 gas
  • the flow rate ratio L / G was adjusted to 1 L / Nm 3 by adjusting the opening of the valve.
  • the amine concentration in the de-CO 2 exhaust gas that passed through the washing section did not increase, and the pump power for washing water circulation could be reduced to about 1 ⁇ 2.
  • the flow rate ratio L / G of the washing water of the washing section and the de-CO 2 exhaust gas is adjusted to the valve opening degree. To 4.0 L / Nm 3 . As a result, it was possible to suppress an increase in amine concentration in the de-CO 2 exhaust gas that passed through the cleaning section.
  • the flow rate ratio L / G of the wash water and de-CO 2 exhaust gas in the wash unit 24a is set to the valve opening degree. It was changed to 3.5 L / Nm 3 by adjustment. As a result, an increase in the amine concentration of the de-CO 2 exhaust gas in the line 4 could be suppressed.

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  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)
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  • Carbon And Carbon Compounds (AREA)

Abstract

L'invention concerne un dispositif d'élimination de dioxyde de carbone qui possède : une section absorbant le CO2 ayant la fonction de mettre en contact du gaz d'échappement contenant du CO2 avec une solution aqueuse d'un composé aminé, ceci provoquant l'absorption du CO2 par le liquide absorbant pour obtenir du gaz d'échappement dont le CO2 a été éliminé ; une section de lavage ayant la fonction de mettre en contact le gaz d'échappement dont le CO2 a été éliminé obtenu à la section absorbant le CO2 avec de l'eau de lavage, éliminant ainsi le composé aminé ; une section de régénération du liquide absorbant ayant la fonction de chauffer le liquide absorbant qui a absorbé le CO2 et qui est obtenu à la section absorbant le CO2, ceci chassant le CO2 du liquide absorbant ; un condenseur ayant la fonction de refroidir le CO2 chassé dans la section de régénération du liquide absorbant, condensant ainsi l'eau entraînée dans le CO2 ; un tube qui amène l'eau condensée obtenue au condenseur à la section de lavage en tant qu'eau de lavage ; un système de mesure de la concentration d'ions carbonate contenus dans l'eau de lavage qui est passée à travers la section de lavage et/ou un système de mesure de la concentration en composé aminé contenu dans le gaz d'échappement dont le CO2 a été éliminé qui est passé à travers la section de lavage ; et un système pour ajuster la quantité d'eau de lavage amenée à la section de lavage sur la base de la valeur mesurée de la concentration en composé aminé et/ou la concentration en ions carbonate.
PCT/JP2012/003722 2011-06-07 2012-06-07 Dispositif d'élimination de dioxyde de carbone WO2012169192A1 (fr)

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JP2011127265A JP5697250B2 (ja) 2011-06-07 2011-06-07 燃焼排ガス中の二酸化炭素除去装置の制御方法および制御装置
JP2011-127265 2011-06-07

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WO2016066553A1 (fr) * 2014-10-27 2016-05-06 Thyssenkrupp Industrial Solutions Ag Colonne avec zones d'absorption, de lavage et de refroidissement et procédé de nettoyage d'un gaz
JP2020082017A (ja) * 2018-11-29 2020-06-04 株式会社東芝 二酸化炭素回収システムおよびその運転方法
JP2020179379A (ja) * 2019-04-26 2020-11-05 株式会社東芝 酸性ガスの除去装置および除去方法

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JP6347359B2 (ja) * 2014-01-31 2018-06-27 三菱重工エンジニアリング株式会社 ガス吸収・再生装置及びその運転方法
JP6581768B2 (ja) 2014-11-04 2019-09-25 三菱重工エンジニアリング株式会社 Ｃｏ２回収装置およびｃｏ２回収方法
JP6811759B2 (ja) * 2018-11-09 2021-01-13 三菱重工エンジニアリング株式会社 Ｃｏ２回収装置およびｃｏ２回収方法

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