WO2014024548A1 - Co2回収装置およびco2回収方法 - Google Patents
Co2回収装置およびco2回収方法 Download PDFInfo
- Publication number
- WO2014024548A1 WO2014024548A1 PCT/JP2013/064925 JP2013064925W WO2014024548A1 WO 2014024548 A1 WO2014024548 A1 WO 2014024548A1 JP 2013064925 W JP2013064925 W JP 2013064925W WO 2014024548 A1 WO2014024548 A1 WO 2014024548A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- water
- washing
- section
- absorbing
- exhaust gas
- Prior art date
Links
Images
Classifications
-
- 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
-
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
-
- 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
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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 CO 2 recovery apparatus and a CO 2 recovery method for reducing the concentration of basic amine compounds released and remaining in a decarbonized exhaust gas from which CO 2 has been removed by contact with an absorbing solution.
- Patent Document 1 the amine compound entrained in the decarbonized exhaust gas is recovered by bringing the cleaning water into gas-liquid contact with the decarbonized exhaust gas from which CO 2 has been absorbed and removed by gas-liquid contact with the absorbent. It is shown that a plurality of water washing sections are provided, and the recovery treatment of the amine compounds accompanying the decarbonized exhaust gas is sequentially performed in the plurality of water washing sections. Washing water of Patent Document 1, in a process of reproducing the amine absorbing solution to remove CO 2 from the amine-based absorbing solution that has absorbed CO 2, the condensed water separated by condensing the moisture contained in the CO 2 is It is used.
- Patent Document 2 the cooling unit that cools the decarbonized exhaust gas from which CO 2 has been absorbed and removed by gas-liquid contact with the absorbing liquid, and the countercurrent contact between the condensed water condensed in the cooling unit and the decarbonized exhaust gas.
- the amine compound entrained in the decarbonized exhaust gas is recovered by bringing the cleaning water into gas-liquid contact with the decarbonized exhaust gas from which CO 2 has been absorbed and removed by gas-liquid contact with the absorbent.
- the washing water, condensed water from which CO 2 has been condensed in the cooling tower for cooling the exhaust gas before being recovered is used.
- the present invention solves the above-described problems, and provides a CO 2 recovery apparatus and a CO 2 recovery method that can further reduce the concentration of basic amine compounds that remain and are released in decarbonation exhaust gas. This is the issue.
- the first aspect of the present invention to solve the above problems, and the CO 2 absorber to remove CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, the CO 2 and absorbing solution regeneration tower to separate the CO 2 to play the CO 2 absorbing solution from the absorbed CO 2 absorbing solution, CO reusing lean solution from which CO 2 has been removed by the absorbing solution regeneration tower in the CO 2 absorber a 2 recovery apparatus, the CO 2 absorption tower, and the CO 2 absorbing section for absorbing the CO 2 in the CO 2 content in the exhaust gas by the CO 2 absorbing liquid, provided in the gas flow downstream side of the CO 2 absorbing section , to cool the CO 2 flue gas by washing water, the washing comprising the present rinsing unit for recovering entrained CO 2 absorbing solution by the washing water, the CO 2 absorbing liquid that has been recovered by the liquid reservoir of the present rinsing unit
- a circulation line that circulates by supplying water from the top side of the main water washing section; O 2 will be and a
- a second invention is the CO 2 recovery apparatus according to the first invention, further comprising a cooling means for cooling a part of the extracted wash water.
- a third invention is the first or second invention, further comprising a finish water washing unit provided on the downstream side of the gas flow of the main water washing unit and finish-washed with washing water supplied from the outside of the main water washing unit. It is in the CO 2 recovery device characterized by this.
- the 4th invention is equipped with the concentration part which removes the volatile substance contained in a part of washing water withdrawn from the said main water washing part in any one of 1st thru
- the concentration which removed the volatile substance A CO 2 recovery apparatus is characterized in that water is supplied as washing water to the preliminary washing section.
- a fifth invention is a CO 2 recovery apparatus according to any one of the first to fourth inventions, comprising a plurality of stages of the main water washing section.
- the CO 2 absorption tower for removing CO 2 by contacting the CO 2 containing exhaust gas and the CO 2 absorbing liquid containing CO 2, separating the CO 2 from the CO 2 absorbent having absorbed CO 2 and by using the absorbent regenerator to regenerate the CO 2 absorbing solution, the lean solution from which CO 2 has been removed by the absorbing solution regeneration tower a CO 2 recovery method be reused in the CO 2 absorber, the CO 2
- the CO 2 removal exhaust gas is cooled by the wash water, and a part of the wash water of the main water washing part for recovering the accompanying CO 2 absorbing liquid is extracted, and on the front side of the main water washing part, the CO 2 removal exhaust gas after CO 2 recovery with precleaning, the pre-wash water was pre-washed and flow down directly to the CO 2 absorbing portion, the CO 2 recovery method, characterized in that for combining the CO 2 absorbing solution is there.
- a seventh aspect of the invention is the CO 2 recovery method according to the sixth aspect of the invention, characterized in that finish cleaning is performed with a finish cleaning water supplied from the outside of the water washing section on the downstream side of the main water washing section.
- a part of the washing water in the main washing section is withdrawn, volatile substances in the extracted washing water are removed and concentrated to obtain concentrated water. It is in a CO 2 recovery method characterized by being used as cleaning water for cleaning.
- the present invention it is possible to further reduce the concentration of the basic amine compounds in the absorbing solution that remains and is released in the decarbonized exhaust gas, and to reuse the collected absorbing solution.
- FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment.
- FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment.
- FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment.
- FIG. 4 is a graph comparing entrained substance concentrations in the absorption tower outlet gas in Test Example 1.
- FIG. 5 is a graph comparing the concentration of entrained substances in the absorption tower outlet gas in Test Example 2.
- FIG. 6 is a graph comparing the concentration of volatile substances in the absorption tower outlet gas in Test Example 3.
- FIG. 1 is a schematic diagram of a CO 2 recovery apparatus according to the first embodiment.
- CO 2 recovery apparatus 10A according to the present embodiment, CO 2 containing exhaust gas 11A and the CO 2 absorbing liquid containing CO 2 with (lean solution 12B) and contacting the removing CO 2 CO and 2 absorber (hereinafter referred to as "absorption column") 13, an absorbing solution regeneration tower 14 for reproducing CO 2 absorbent having absorbed CO 2 (the rich solution 12A), said absorbent regenerator (hereinafter referred to as "regeneration tower” ) 14 lean solution 12B which CO 2 has been removed by a CO 2 reused in the CO 2 absorber 13, the CO 2 absorption tower 13, the CO 2 absorbent at a CO 2 content in the flue gas CO and CO 2 absorbing section 13A that absorbs 2, the CO 2 provided in the gas flow downstream side of the absorbent portion 13A, to cool the CO 2 flue gas by the washing water 20,
- the circulation line L 1 but so as to extract a portion 20a of the washing water 20 containing the CO 2 absorbing solution
- the present invention is not limited thereto, separately from the circulation line L 1, CO 2 You may make it provide the storage part which stores the part 20a of the wash water 20 containing an absorption liquid, and may extract from here.
- the CO 2 -containing exhaust gas 11 ⁇ / b > A is in counterflow contact with the CO 2 absorption liquid 12 based on, for example, an alkanolamine in a CO 2 absorption section 13 ⁇ / b > A provided on the lower side of the CO 2 absorption tower 13.
- CO 2 in the CO 2 containing exhaust gas 11A is absorbed by the CO 2 absorbing liquid 12 by a chemical reaction (R-NH 2 + H 2 O + CO 2 ⁇ R-NH 3 HCO 3).
- R-NH 2 + H 2 O + CO 2 ⁇ R-NH 3 HCO 3 As a result, almost no CO 2 remains in the CO 2 removal exhaust gas 11B passing through the CO 2 absorption section 13A and rising inside the CO 2 absorption tower 13.
- the CO 2 -containing gas 11A rising in the CO 2 absorption part 13A in the absorption tower 13 is accompanied by water vapor because of the saturated vapor pressure at that temperature.
- a very small part of the CO 2 absorbing liquid 12 becomes steam from the relationship of saturated vapor pressure, and accompanies the exhaust gas as mist due to entrainment. .
- the CO 2 absorbing liquid 12 is slightly contained in the CO 2 removal exhaust gas 11B that has passed through the CO 2 absorbing portion 13A.
- the cleaning water 20 that is condensed water is generated from the water vapor accompanying the exhaust gas, and the CO 2 absorbing liquid 12 accompanying the exhaust gas is dissolved,
- the cleaning water 20 will contain a small amount of the CO 2 absorbent 12.
- the CO 2 absorbing liquid 12 in the CO 2 removal gas 11B is cooled in the main water washing section 13C to condense the moisture in the CO 2 removal exhaust gas, thereby removing excess.
- the pre-wash water that has been removed is washed away.
- a cooling unit 23 may be provided in the extraction line L 2 to cool a part 20 a of the cleaning water 20 to a predetermined temperature (for example, 40 ° C. or less).
- the CO 2 removal exhaust gas 11C that has passed through the preliminary water washing section 13B rises to the main water washing section 13C via the chimney tray 16 and comes into gas-liquid contact with the washing water 20 supplied from the top side of the water washing section 13C.
- the CO 2 absorbing liquid 12 accompanying the CO 2 removal exhaust gas 11C is recovered by circulation cleaning.
- the washing water 20 stored in the liquid storage section 21 of the chimney tray 16 is circulated through the circulation line L 1 to perform circulation washing.
- the circulation line L 1 of the cooling unit 22 is provided, it is cooled to a predetermined temperature (e.g., 40 ° C. or less).
- Reference numeral 73 denotes a mist eliminator that captures mist in the gas.
- the preliminary water washing section 13B and the main water washing section 13C are provided, and the CO 2 absorbent 12 dissolved in the condensed water accompanying the CO 2 removal gas 11B, 11C is washed and removed in two stages. Therefore, the CO 2 absorbent 12 accompanying the CO 2 removal exhaust gas 11B, 11C can be reliably recovered and removed.
- the concentration of the basic amine compounds remaining and released in the CO 2 absorbing liquid removal exhaust gas 11D released to the outside can be further reduced.
- the rich solution 12 ⁇ / b > A that has absorbed CO 2 is pressurized by a rich solvent pump 51 interposed in the rich solution supply pipe 50, and the lean solution 12 ⁇ / b> B regenerated in the absorbent regenerator 14 in the rich / lean solution heat exchanger 52. And is supplied to the top side of the absorption liquid regeneration tower 14.
- the rich solution 12A released into the tower from the top side of the regeneration tower 14 releases most of the CO 2 by heating with water vapor from the bottom of the tower.
- the CO 2 absorbent 12 that has released part or most of the CO 2 in the regeneration tower 14 is referred to as a “semi-lean solution”.
- the semi-lean solution (not shown) flows down to the bottom of the regeneration tower 14, it becomes a lean solution 12B from which almost all of the CO 2 has been removed.
- the lean solution 12B is heated by saturated steam 62 in the regeneration heater 61 interposed in the circulation line L 20.
- the saturated steam 62 after heating becomes steam condensed water 63.
- the CO 2 gas 41 accompanied by water vapor dissipated from the rich solution 12A and a semi-lean solution (not shown) is released from the top 14a of the regeneration tower 14 in the tower.
- CO 2 gas 41 accompanied by water vapor is derived by the gas discharge line L 21
- the water vapor is condensed by a condenser 42 which is interposed in the gas discharge line L 21
- condensed water 44 is separated in the separation drum 43
- the CO 2 gas 45 is discharged out of the system, and post-processing such as compression recovery is performed separately.
- Condensed water 44 separated in the separation drum 43 is supplied to the upper portion of the absorbing solution regeneration tower 14 by the condensed water circulation pump 46 interposed in condensate line L 22.
- a portion of the condensed water 44 is fed into the circulation line L 1 of the washing water 20 containing the CO 2 absorbing solution, used for the absorption of CO 2 absorbing liquid 12 accompanying the CO 2 flue gas 11C You may do it.
- the regenerated CO 2 absorbent (lean solution 12B) is sent to the CO 2 absorption tower 13 side by the lean solution pump 54 via the lean solution supply pipe 53, and is circulated and used as the CO 2 absorbent 12.
- the lean solution 12B is cooled to a predetermined temperature by the cooling unit 55 and is supplied into the CO 2 absorbing unit 13A through the nozzle 56. Therefore, the CO 2 absorbing liquid 12 forms a closed path for circulating a CO 2 absorption tower 13 and the absorption solution regenerator 14 is reused in the CO 2 absorbing section 13A of the CO 2 absorber 13.
- the CO 2 absorbent 12 is supplied from a replenishment line (not shown) as necessary, and the CO 2 absorbent 12 is regenerated by a reclaimer (not shown) as needed.
- the CO 2 -containing exhaust gas 11A supplied to the CO 2 absorption tower 13 is cooled by the cooling water 71 in the cooling tower 70 provided on the upstream side thereof, and then introduced into the CO 2 absorption tower 13. Incidentally, it is fed to the top 13a of the washing unit 13C a portion of the cooling water 71 as wash water 20 of the CO 2 absorber 13, is sometimes used for cleaning the CO 2 absorbing liquid 12 accompanying the CO 2 flue gas 11B .
- Reference numeral 72 denotes a circulation pump
- 74 denotes a circulation line
- 75 denotes a cooler.
- the CO 2 absorbing liquid 12 to be circulated utilizing the CO 2 absorption tower 13 and the absorption solution regenerator 14 is entrained in a CO 2 flue gas 11B, in a preliminary water washing section 13B and the water washing section 13C
- the CO 2 removal exhaust gas 11B, 11C from which CO 2 has been removed is brought into countercurrent contact with the cleaning water 20, and the CO 2 absorbing liquid 12 accompanying the CO 2 removal exhaust gas 11B, 11C is absorbed and removed by the cleaning water 20. In this way, emission to the outside of the absorption tower 13 is prevented.
- the preliminary water washing section 13B is provided in addition to the conventional water washing section 13C using the conventional circulating washing water, the CO 2 absorbing liquid accompanying the CO 2 removal exhaust gas 11B and 11C Recovery effect is improved. That is, in the present washing section 13C, with circulating wash with washing water 20 circulating, withdrawn in withdrawal line L 2 a portion 20a of the washing water 20 which has been subjected to cleaning, because it is providing to the pre-washing unit 13B Since the portion 20a of the extracted wash water 20 has a low concentration of CO 2 absorbing liquid (for example, about several percent), the preliminary washing section 13B can be cleaned well.
- the preliminary washing unit 13B uses the excess of the washing water 20 used in the main washing unit 13C, and the supply amount only needs to be adjusted by the adjustment valve 24, so that the apparatus configuration is simplified.
- the CO 2 removal exhaust gas 11C is cooled by the wash water 20, and the gaseous water accompanying the CO 2 removal exhaust gas 11C condenses to become surplus water. This is because it can be used for cleaning.
- the concentration of the recovered CO 2 absorbent in the preliminary washing section 13B is increased. since becomes high, the effect of removing the CO 2 in the CO 2 containing exhaust gas 11A in the CO 2 absorbing section 13A can be improved.
- FIG. 2 is a schematic diagram of a CO 2 recovery apparatus according to the second embodiment.
- the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted.
- the CO 2 recovery apparatus 10A shown in FIG. 1 is further provided on the downstream side of the gas flow of the main water washing section 13C.
- a finishing water washing section 13D for finishing washing with washing water 20 supplied from the outside is provided.
- the cooling unit 25 provided in the branch line L 23, may be to cool the part 44a of the condensed water 44 to a predetermined temperature (e.g., 40 ° C. or less).
- a part 44 a of the condensed water 44 is separated from the CO 2 gas 41 accompanied with water vapor discharged from the regeneration tower 14 to the outside. Therefore, since the condensed water 44 is water that is hardly accompanied by the CO 2 absorbing solution, the efficiency of the finish cleaning is exhibited. Moreover, you may make it supply ion-exchange water separately as using the part 44a of the condensed water 44 as finishing washing water in the finishing washing part 13D.
- a liquid having a low concentration of gas entrained substances such as a CO 2 absorbent is used as finish washing water, and the CO 2 absorbent is removed on the most downstream side (tower 13a side) in the final stage of the washing section.
- the exhaust gas 11D By bringing the exhaust gas 11D into gas-liquid contact, it is possible to further reduce the concentration of the CO 2 absorbent that is diffused from the tower top 13a of the absorption tower 13 to the outside.
- FIG. 3 is a schematic diagram of a CO 2 recovery apparatus according to the third embodiment. Note that the CO 2 recovery apparatus 10A same configuration as that according to the first embodiment shown in FIG. 1, and redundant description are denoted by the same reference numerals will be omitted. As shown in FIG. 3, in the CO 2 recovery apparatus 10C of the present embodiment, in the CO 2 recovery apparatus 10A shown in FIG. 1, CO 2 absorption is further performed from the circulation line L 1 of the cleaning liquid 20 circulating in the main water washing section 13C.
- a gas introduction line L 4 for introducing the component 32 to the tower top 13 a side of the absorption tower 13 is provided.
- the gas-liquid separation unit 30A and the concentration unit 30B constitute a concentration unit.
- the liquid 31 and the gas component 32 are separated by first dissipating the extracted liquid, and the gas component 32 is separated from the extracted liquid.
- the gas component 32 is a highly volatile material such as ammonia contained in the CO 2 absorbent 12 such as ammonia gas, and is discharged to the gas introduction line L 4 .
- the liquid 31 from which the gas component 32 has been separated by the gas-liquid separation unit 30A is introduced into the concentration tower 30B.
- Air 35 is blown into the concentrating tower 30B, and the gas component 32 remaining in the liquid 31 is further extracted.
- the concentrating tower 30B is provided with a line for recovering the volatile substance in the liquid phase and discharging it separately as necessary.
- a volatile substance such as ammonia can be removed from the liquid 31 to obtain a concentrated liquid 33.
- the ammonia concentrate 33 removed is fed through line L 3 to the preliminary washing unit 13B side, so that use as a pre-wash water.
- the concentration of the basic amine compounds and the concentration of the volatile substances remaining and released in the CO 2 absorbent removal exhaust gas 11D released to the outside can be further reduced as compared with the first embodiment. .
- Example 1 A test was conducted to confirm the effect of Example 1 of the present invention. That is, 200 Nm 3 / h of combustion exhaust gas containing 14% of carbon dioxide was supplied to the CO 2 absorbing portion 13A of the absorption tower 13 and brought into countercurrent contact with a basic amine solution (CO 2 absorbing solution) to absorb carbon dioxide.
- the preliminary water washing part 13B was provided on the downstream (upper part) side of the CO 2 absorption part 13A.
- the washing water in the preliminary washing section 13B is used to extract the excess of the washing water in the main washing section 13C, bring it into countercurrent contact with the exhaust gas, and directly flow down to the CO 2 absorbent, and in the main washing section 13C, the washing water and liquid / gas Countercurrent contact was made at a ratio of 4 L / Nm 3 and the demister 73 at the outlet was passed.
- FIG. FIG. 4 is a graph comparing entrained substance concentrations in the absorption tower outlet gas in Test Example 1.
- the left side is a conventional method, in which there is no preliminary water washing portion, and the right side is a case in which there is a preliminary water washing portion.
- Example 2 A test was conducted to confirm the effect of Example 2 of the present invention. That is, 200 Nm 3 / h of combustion exhaust gas containing 14% of carbon dioxide was supplied to the CO 2 absorbing portion 13A of the absorption tower 13 and brought into countercurrent contact with a basic amine solution (CO 2 absorbing solution) to absorb carbon dioxide.
- the preliminary water washing section 13B is provided on the downstream (upper) side of the CO 2 absorbing section 13A
- the finishing water washing section 13D is provided on the downstream (upper) side of the main water washing section 13C.
- the washing water of the preliminary washing unit 13B extracts the excess of the washing water of the main washing unit 13C, makes it counter-contact with the exhaust gas, and directly flows down to the CO 2 absorbing liquid 12, and the washing water and liquid / A counterflow contact with the gas is performed at a gas ratio of 4 L / Nm 3 , and the finishing flush unit 13D introduces a part of the recirculating tower reflux water and makes a countercurrent contact with the gas to directly flow down to the cleaning liquid of the main flush unit 13C. Passed through the demister 73 at the exit. The result is shown in FIG. FIG. 5 is a graph comparing the concentration of entrained substances in the absorption tower outlet gas in Test Example 2. In FIG.
- the left side is Test Example 1 and provided with the preliminary washing unit, but there is no finishing washing unit, and the right side is the case where the preliminary washing unit and the finishing washing unit are provided before and after the main washing unit.
- the concentration ratio of the entrained substance in the absorption tower outlet gas (CO 2 absorbent removal exhaust gas 11E) is 1 / Reduced to 10. Therefore, it is reduced to 1/100 compared with the conventional method of Test Example 1 (one in which the preliminary washing unit and the finishing washing unit are not provided).
- Example 3 A test was conducted to confirm the effect of Example 3 of the present invention. That is, 200 Nm 3 / h of combustion exhaust gas containing 14% of carbon dioxide was supplied to the CO 2 absorbing portion 13A of the absorption tower 13 and brought into countercurrent contact with a basic amine solution (CO 2 absorbing solution) to absorb carbon dioxide.
- the preliminary water washing section 13B is provided on the downstream (upper) side of the CO 2 absorption section 13A, and the concentrating means 30 is provided in the extraction line L 2 of the main water washing section 13C.
- the washing water in the preliminary washing section 13B is used to extract the excess of the washing water in the main washing section 13C, bring it into countercurrent contact with the exhaust gas, and directly flow down to the CO 2 absorbent, and in the main washing section 13C, the washing water and liquid / gas Countercurrent contact was made at a ratio of 4 L / Nm 3 , and the demister 73 at the outlet was passed.
- FIG. FIG. 6 is a graph comparing the concentration of volatile substances in the absorption tower outlet gas in Test Example 3.
- the left side is Test Example 1, where there is no concentrating part, and the right side is the case where there is a concentrating part.
- the concentration ratio of the volatile entrained substance in the absorption tower outlet gas (CO 2 absorbent removal exhaust gas 11D) was reduced to 2/5.
Landscapes
- 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)
- Health & Medical Sciences (AREA)
- Organic Chemistry (AREA)
- Biomedical Technology (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Description
図1に示すように、本実施例に係るCO2回収装置10Aは、CO2を含有するCO2含有排ガス11AとCO2吸収液(リーン溶液12B)とを接触させてCO2を除去するCO2吸収塔(以下「吸収塔」という)13と、CO2を吸収したCO2吸収液(リッチ溶液12A)を再生する吸収液再生塔14と、前記吸収液再生塔(以下「再生塔」という)14でCO2が除去されたリーン溶液12BをCO2吸収塔13で再利用するCO2回収装置であって、前記CO2吸収塔13が、CO2吸収液によりCO2含有排ガス中のCO2を吸収するCO2吸収部13Aと、前記CO2吸収部13Aのガス流れ後流側に設けられ、洗浄水20によりCO2除去排ガスを冷却すると共に、同伴するCO2吸収液を前記洗浄水20により回収する本水洗部13Cと、前記本水洗部13Cの液貯留部21で回収されたCO2吸収液を含む洗浄水20を前記本水洗部13Cの頂部側から供給して循環する循環ラインL1と、前記CO2吸収部13Aと本水洗部13Cとの間に設けられる予備水洗部13Bとを具備してなり、前記循環ラインL1から、CO2吸収液を含む洗浄水20の一部20aを抜き出すと共に、該予備水洗部13Bにおいて、前記洗浄水20の一部20aを本水洗部13C側から供給し、CO2吸収部13AでCO2が吸収された排ガス11B中に同伴されるCO2吸収液を該洗浄水20の一部20aで予備洗浄して回収すると共に、この予備洗浄した予備洗浄水を、CO2吸収部13A側に直接流下させつつ、CO2吸収液12と合流するものである。
本実施例では、循環ラインL1から、CO2吸収液を含む洗浄水20の一部20aを抜き出すようにしているが、本発明はこれに限定されず、別途循環ラインL1から、CO2吸収液を含む洗浄水20の一部20aを貯留する貯留部を設け、ここから抜き出すようにしてもよい。
この結果、CO2吸収部13Aを通過して、CO2吸収塔13の内部を上昇するCO2除去排ガス11Bには、CO2が殆ど残存しないものとなる。
この水蒸気を含むCO2除去ガスとCO2吸収液12とが対向接触することで、CO2吸収液12の極一部が飽和蒸気圧の関係から蒸気として、飛沫同伴によりミストとして排ガスに同伴する。
この結果、CO2吸収部13Aを通過したCO2除去排ガス11B中には、CO2吸収液12が僅かに含まれることとなる。
本水洗部13Cでは、CO2除去排ガス11Bの冷却により、排ガス中に同伴している水蒸気から凝縮水である洗浄水20を生じ、排ガス中に同伴するCO2吸収液12が溶解することにより、洗浄水20中にCO2吸収液12が僅かに含まれることになる。
なお、抜き出しラインL2には冷却部23を設け、洗浄水20の一部20aを所定の温度(例えば40℃以下)まで冷却するようにしてもよい。
なお、循環ラインL1には冷却部22を設け、所定の温度(例えば40℃以下)まで冷却している。
この循環する洗浄水20による本洗浄によって、CO2除去排ガス11Cに同伴するCO2吸収液12を更に回収・除去することができる。
そして、水蒸気を伴ったCO2ガス41がガス排出ラインL21により導出され、ガス排出ラインL21に介装されたコンデンサ42により水蒸気が凝縮され、分離ドラム43にて凝縮水44が分離され、CO2ガス45が系外に放出されて、別途圧縮回収等の後処理がなされる。
分離ドラム43にて分離された凝縮水44は凝縮水ラインL22に介装された凝縮水循環ポンプ46にて吸収液再生塔14の上部に供給される。
なお、図示していないが、一部の凝縮水44はCO2吸収液を含む洗浄水20の循環ラインL1に供給され、CO2除去排ガス11Cに同伴するCO2吸収液12の吸収に用いるようにしてもよい。
よって、CO2吸収液12は、CO2吸収塔13と吸収液再生塔14とを循環する閉鎖経路を形成し、CO2吸収塔13のCO2吸収部13Aで再利用される。なお、必要に応じて図示しない補給ラインによりCO2吸収液12は供給され、また必要に応じて図示しないリクレーマによりCO2吸収液12を再生するようにしている。
すなわち、本水洗部13Cでは、循環する洗浄水20により循環洗浄すると共に、洗浄に供された洗浄水20の一部20aを抜き出しラインL2で抜き出して、予備水洗部13Bに供給しているので、抜き出した洗浄水20の一部20aは、CO2吸収液の濃度が低い(例えば数%程度)ので、予備水洗部13Bでの洗浄が良好となる。
これは、本水洗部13Cでは、洗浄水20によりCO2除去排ガス11Cが冷却され、CO2除去排ガス11Cに同伴される気体状の水分が凝縮し、余剰水となるので、その余剰分を予備洗浄に用いることができることとなるからである。
その結果、予備洗浄に供されてCO2吸収液を回収した予備洗浄水は、循環ラインL1から抜き出した洗浄水の一部20aよりもCO2吸収液を若干多く含むこととなるので、CO2吸収部13AでCO2の回収に寄与することとなる。
すなわち、例えば30%濃度のCO2吸収液のリーン溶液12Bに、数%+α分のCO2吸収液を含む洗浄水20aを合流することとなる。
この結果、従来において、水洗部で回収された凝縮水を、CO2吸収塔13の底部13b側に供給するような場合と較べた場合、予備水洗部13BにおけるCO2吸収液の回収分だけ濃度が高いものとなるので、CO2吸収部13AにおけるCO2含有排ガス11A中のCO2を除去する効果が向上することとなる。
図2に示すように、本実施例のCO2回収装置10Bでは、図1に示すCO2回収装置10Aにおいて、さらに、前記本水洗部13Cのガス流れ後段側に設けられ、本水洗部13Cの外部から供給される洗浄水20で仕上洗浄する仕上水洗部13Dを具備している。
本実施例では、再生塔14の塔頂部14aからは外部に放出された水蒸気を伴ったCO2ガス41中から分離された凝縮水44の一部44aを分岐ラインL23により供給して、仕上水洗部13Dでの洗浄水として用いるようにしている。
なお、分岐ラインL23には冷却部25を設け、凝縮水44の一部44aを所定の温度(例えば40℃以下)まで冷却するようにしてもよい。
また、仕上水洗部13Dでの仕上洗浄水として、凝縮水44の一部44aを用いる以外には、イオン交換水を別途供給するようにしてもよい。
図3に示すように、本実施例のCO2回収装置10Cでは、図1に示すCO2回収装置10Aにおいて、さらに、本水洗部13Cを循環する洗浄液20の循環ラインL1から、CO2吸収液12を含む洗浄水20の一部20aを抜出液として抜出す抜出しラインL2と、抜出液からガス成分32を分離する気液分離部30Aと、抜出液20a中のCO2吸収液12を濃縮し、ガス成分32を分離する濃縮塔30Bと、CO2吸収液12を濃縮した濃縮液33を予備水洗部13Bに予備洗浄水として導入する導入ラインL3と、分離されたガス成分32を吸収塔13の塔頂部13a側に導入するガス導入ラインL4とを具備するものである。本実施例では、気液分離部30Aと濃縮部30Bとから濃縮手段を構成している。
このガス成分32は、CO2吸収液12中に含まれるアンモニア等の揮発性の高い、例えばアンモニアガス等であり、ガス導入ラインL4へ排出される。
図示していないが、この濃縮塔30Bには、揮発性物質を液相に回収して別途排出するラインを必要に応じて設けるようにする。
この結果、液体31から揮発性物質である例えばアンモニア等を除去して、濃縮液33とすることができる。
本実施例では、このアンモニア等が除去された濃縮液33を予備水洗部13B側へ供給ラインL3を介して供給し、予備洗浄水として用いるようにしている。
本発明の実施例1の効果を確認する試験を行った。
即ち、二酸化炭素14%を含む燃焼排ガス200Nm3/hを吸収塔13のCO2吸収部13Aに供給し、塩基性アミン溶液(CO2吸収液)と向流接触させて二酸化炭素を吸収した。
試験例では、予備水洗部13BをCO2吸収部13Aの後流(上部)側に設けた。
予備水洗部13Bの洗浄水は本水洗部13Cの洗浄水の余剰分を抜き出して排ガスと向流接触させてCO2吸収液に直接流下させると共に、本水洗部13Cにて洗浄水と液/ガス比4L/Nm3で向流接触させ出口のデミスタ73を通過させた。
この結果を図4に示す。図4は、試験例1における吸収塔出口ガス中の同伴物質濃度を対比したグラフである。図4中、左側は従来法であり、予備水洗部が無い場合であり、右側は予備水洗部が有る場合である。
試験例1のように予備水洗部を設けた場合には、吸収塔出口ガス(CO2吸収液除去排ガス11D)中の同伴物質の濃度比が、1/10に低減した。
本発明の実施例2の効果を確認する試験を行った。
即ち、二酸化炭素14%を含む燃焼排ガス200Nm3/h を吸収塔13のCO2吸収部13Aに供給し、塩基性アミン溶液(CO2吸収液)と向流接触させて二酸化炭素を吸収した。
試験例では、予備水洗部13BをCO2吸収部13Aの後流(上部)側に設けるとともに、仕上水洗部13Dを本水洗部13Cの後流(上部)側に設けた。
予備水洗部13Bの洗浄水は本水洗部13Cの洗浄水の余剰分を抜き出して排ガスと向流接触させてCO2吸収液12に直接流下させると共に、本水洗部13Cにて洗浄水と液/ガス比4L/Nm3でガスと向流接触させ、仕上水洗部13Dでは再生塔リフラックス水の一部を導入してガスと向流接触させて本水洗部13Cの洗浄液に直接流下させ、ガスは出口のデミスタ73を通過させた。
この結果を図5に示す。図5は、試験例2における吸収塔出口ガス中の同伴物質濃度を対比したグラフである。図5中、左側は試験例1であり、予備水洗部を設けたが、仕上水洗部が無い場合であり、右側は予備水洗部及び仕上水洗部を本水洗部の前後に設けた場合である。
試験例2のように予備水洗部及び仕上水洗部を本水洗部の前後に設けた場合には、吸収塔出口ガス(CO2吸収液除去排ガス11E)中の同伴物質の濃度比が、1/10に低減した。よって、試験例1の従来法(予備水洗部及び仕上水洗部を設けないもの)と較べると1/100に低減したこととなる。
本発明の実施例3の効果を確認する試験を行った。
即ち、二酸化炭素14%を含む燃焼排ガス200Nm3/h を吸収塔13のCO2吸収部13Aに供給し、塩基性アミン溶液(CO2吸収液)と向流接触させて二酸化炭素を吸収した。
試験例では、予備水洗部13BをCO2吸収部13Aの後流(上部)側に設けると共に、本水洗部13Cの抜き出しラインL2に濃縮手段30を設けた。
予備水洗部13Bの洗浄水は本水洗部13Cの洗浄水の余剰分を抜き出して排ガスと向流接触させてCO2吸収液に直接流下させると共に、本水洗部13Cにて洗浄水と液/ガス比4L/Nm3で向流接触させ出口のデミスタ73を通過させた。
この結果を図6に示す。図6は、試験例3における吸収塔出口ガス中の揮発性物質濃度を対比したグラフである。図6中、左側は試験例1であり、濃縮部が無い場合であり、右側は濃縮部が有る場合である。
試験例3のように濃縮部を設けた場合には、吸収塔出口ガス(CO2吸収液除去排ガス11D)中の揮発性同伴物質の濃度比が、2/5に低減した。
11A CO2含有排ガス
12 CO2吸収液
12A リッチ溶液
12B リーン溶液
13 CO2吸収塔(吸収塔)
13A CO2吸収部
13B 予備水洗部
13C 本水洗部
13D 仕上水洗部
14 吸収液再生塔(再生塔)
20 洗浄水
20a 洗浄水の一部
Claims (8)
- CO2を含有するCO2含有排ガスとCO2吸収液とを接触させてCO2を除去するCO2吸収塔と、
CO2を吸収したCO2吸収液からCO2を分離してCO2吸収液を再生する吸収液再生塔と、
前記吸収液再生塔でCO2が除去されたリーン溶液をCO2吸収塔で再利用するCO2回収装置であって、
前記CO2吸収塔が、
CO2吸収液によりCO2含有排ガス中のCO2を吸収するCO2吸収部と、
前記CO2吸収部のガス流れ後流側に設けられ、洗浄水によりCO2除去排ガスを冷却すると共に、同伴するCO2吸収液を前記洗浄水により回収する本水洗部と、
前記本水洗部の液貯留部で回収されたCO2吸収液を含む洗浄水を前記本水洗部の頂部側から供給して循環する循環ラインと、
前記CO2吸収部と本水洗部との間に設けられる予備水洗部とを具備してなり、
前記本水洗部から、CO2吸収液を含む洗浄水の一部を抜き出すと共に、該予備水洗部において、前記洗浄水の一部を本水洗部側から供給し、CO2吸収部でCO2が吸収された排ガス中に同伴されるCO2吸収液を該洗浄水の一部で予備洗浄して回収すると共に、
予備洗浄した予備洗浄水を、CO2吸収部側に直接流下させることを特徴とするCO2回収装置。 - 請求項1において、
前記抜き出した洗浄水の一部を冷却する冷却手段を具備することを特徴とするCO2回収装置。 - 請求項1又は2において、
前記本水洗部のガス流れ後段側に設けられ、前記本水洗部の外部から供給される洗浄水で仕上げ洗浄する仕上水洗部を具備することを特徴とするCO2回収装置。 - 請求項1乃至3のいずれか一つにおいて、
前記本水洗部から抜き出す洗浄水の一部に含まれる揮発性物質を除去する濃縮部を具備し、揮発性物質を除去した濃縮水を、洗浄水として予備水洗部に供給することを特徴とするCO2回収装置。 - 請求項1乃至4のいずれか一つにおいて、
前記本水洗部を複数段具備することを特徴とするCO2回収装置。 - CO2を含有するCO2含有排ガスとCO2吸収液とを接触させてCO2を除去するCO2吸収塔と、CO2を吸収したCO2吸収液からCO2を分離してCO2吸収液を再生する吸収液再生塔とを用い、前記吸収液再生塔でCO2が除去されたリーン溶液をCO2吸収塔で再利用するCO2回収方法であって、
前記CO2吸収塔の後流側において、洗浄水によりCO2除去排ガスを冷却すると共に、同伴するCO2吸収液を回収する本水洗部の一部の洗浄水を抜出し、
本水洗部の前段側において、CO2回収後のCO2除去排ガスを予備洗浄すると共に、
予備洗浄した予備洗浄水を、CO2吸収部側に直接流下させ、CO2吸収液と合流させることを特徴とするCO2回収方法。 - 請求項6において、
前記本水洗部の後流側で、水洗部の外部から供給される仕上げ洗浄水で仕上げ洗浄することを特徴とするCO2回収方法。 - 請求項6又は7において、
本水洗部の一部の洗浄水を抜出し、抜き出した洗浄水中の揮発性物質を除去して濃縮して濃縮水とし、この濃縮水を予備洗浄の洗浄水として用いることを特徴とするCO2回収方法。
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP13828178.7A EP2893970B1 (en) | 2012-08-08 | 2013-05-29 | Co2 recovery device and co2 recovery method |
CA2877926A CA2877926C (en) | 2012-08-08 | 2013-05-29 | Co2 recovery unit and co2 recovery method |
AU2013300927A AU2013300927B2 (en) | 2012-08-08 | 2013-05-29 | CO2 recovery device and CO2 recovery method |
US14/409,889 US9914088B2 (en) | 2012-08-08 | 2013-05-29 | CO2 recovery unit and CO2 recovery method |
DK13828178.7T DK2893970T3 (en) | 2012-08-08 | 2013-05-29 | CO2 recovery unit |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2012-176131 | 2012-08-08 | ||
JP2012176131A JP6004821B2 (ja) | 2012-08-08 | 2012-08-08 | Co2回収装置およびco2回収方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2014024548A1 true WO2014024548A1 (ja) | 2014-02-13 |
Family
ID=50067791
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2013/064925 WO2014024548A1 (ja) | 2012-08-08 | 2013-05-29 | Co2回収装置およびco2回収方法 |
Country Status (7)
Country | Link |
---|---|
US (1) | US9914088B2 (ja) |
EP (1) | EP2893970B1 (ja) |
JP (1) | JP6004821B2 (ja) |
AU (1) | AU2013300927B2 (ja) |
CA (1) | CA2877926C (ja) |
DK (1) | DK2893970T3 (ja) |
WO (1) | WO2014024548A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2627847C2 (ru) * | 2015-12-30 | 2017-08-14 | Игорь Анатольевич Мнушкин | Способ и колонна абсорбционной очистки газов от нежелательных примесей |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
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 |
EP3181540B1 (de) * | 2015-12-18 | 2019-07-24 | L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Verfahren zur trennung von methanol aus gasgemischen |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH05245340A (ja) * | 1992-03-03 | 1993-09-24 | Kansai Electric Power Co Inc:The | 燃焼排ガスの処理方法 |
JPH0880421A (ja) | 1991-03-07 | 1996-03-26 | Mitsubishi Heavy Ind Ltd | 燃焼排ガスの脱炭酸ガス装置及び方法 |
JP2002126439A (ja) | 2000-10-25 | 2002-05-08 | Kansai Electric Power Co Inc:The | アミン回収方法及び装置並びにこれを備えた脱炭酸ガス装置 |
JP2007284272A (ja) * | 2006-04-13 | 2007-11-01 | Mitsubishi Heavy Ind Ltd | Co2回収装置及びco2回収方法 |
JP2011136258A (ja) * | 2009-12-25 | 2011-07-14 | Mitsubishi Heavy Ind Ltd | Co2回収装置およびco2回収方法 |
JP2012236166A (ja) * | 2011-05-12 | 2012-12-06 | Mitsubishi Heavy Ind Ltd | Co2回収装置およびco2回収方法 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5378442A (en) | 1992-01-17 | 1995-01-03 | The Kansai Electric Power Co., Inc. | Method for treating combustion exhaust gas |
JP2786559B2 (ja) * | 1992-01-17 | 1998-08-13 | 関西電力株式会社 | 燃焼排ガス中の炭酸ガスの回収方法 |
AU2009284712A1 (en) * | 2008-08-22 | 2010-02-25 | Commonwealth Scientific And Industrial Research Organisation | Treatment of CO2-depleted flue gases |
JP5351728B2 (ja) * | 2009-12-03 | 2013-11-27 | 三菱重工業株式会社 | Co2回収装置およびco2回収方法 |
US9314734B2 (en) * | 2010-01-14 | 2016-04-19 | Alstom Technology Ltd | Wash water method and system for a carbon dioxide capture process |
DK2691163T3 (en) * | 2011-03-31 | 2015-08-17 | Basf Se | DETENTION OF AMINES FOR REMOVAL OF SURE GAS EMISSIONS BY AMIN-absorbents |
US8529857B2 (en) * | 2011-03-31 | 2013-09-10 | Basf Se | Retention of amines in the removal of acid gases by means of amine absorption media |
CA2886800C (en) * | 2012-10-11 | 2018-04-10 | Mitsubishi Heavy Industries, Ltd. | Air pollution control system and air pollution control method |
-
2012
- 2012-08-08 JP JP2012176131A patent/JP6004821B2/ja active Active
-
2013
- 2013-05-29 EP EP13828178.7A patent/EP2893970B1/en active Active
- 2013-05-29 CA CA2877926A patent/CA2877926C/en active Active
- 2013-05-29 WO PCT/JP2013/064925 patent/WO2014024548A1/ja active Application Filing
- 2013-05-29 US US14/409,889 patent/US9914088B2/en active Active
- 2013-05-29 DK DK13828178.7T patent/DK2893970T3/en active
- 2013-05-29 AU AU2013300927A patent/AU2013300927B2/en active Active
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0880421A (ja) | 1991-03-07 | 1996-03-26 | Mitsubishi Heavy Ind Ltd | 燃焼排ガスの脱炭酸ガス装置及び方法 |
JPH05245340A (ja) * | 1992-03-03 | 1993-09-24 | Kansai Electric Power Co Inc:The | 燃焼排ガスの処理方法 |
JP2002126439A (ja) | 2000-10-25 | 2002-05-08 | Kansai Electric Power Co Inc:The | アミン回収方法及び装置並びにこれを備えた脱炭酸ガス装置 |
JP2007284272A (ja) * | 2006-04-13 | 2007-11-01 | Mitsubishi Heavy Ind Ltd | Co2回収装置及びco2回収方法 |
JP2011136258A (ja) * | 2009-12-25 | 2011-07-14 | Mitsubishi Heavy Ind Ltd | Co2回収装置およびco2回収方法 |
JP2012236166A (ja) * | 2011-05-12 | 2012-12-06 | Mitsubishi Heavy Ind Ltd | Co2回収装置およびco2回収方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2893970A4 |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2627847C2 (ru) * | 2015-12-30 | 2017-08-14 | Игорь Анатольевич Мнушкин | Способ и колонна абсорбционной очистки газов от нежелательных примесей |
WO2017116284A3 (en) * | 2015-12-30 | 2017-08-17 | Mnushkin Igor Anatol`Evich | Absorption gas treatment method and column |
Also Published As
Publication number | Publication date |
---|---|
US20150182906A1 (en) | 2015-07-02 |
JP6004821B2 (ja) | 2016-10-12 |
EP2893970A1 (en) | 2015-07-15 |
US9914088B2 (en) | 2018-03-13 |
AU2013300927B2 (en) | 2016-03-03 |
AU2013300927A1 (en) | 2015-01-22 |
CA2877926A1 (en) | 2014-02-13 |
EP2893970A4 (en) | 2016-03-30 |
DK2893970T3 (en) | 2018-07-30 |
JP2014033991A (ja) | 2014-02-24 |
CA2877926C (en) | 2017-01-17 |
EP2893970B1 (en) | 2018-05-16 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2012153812A1 (ja) | Co2回収装置およびco2回収方法 | |
JP6239519B2 (ja) | 脱硫装置およびそこで発生した凝縮水の使用方法 | |
JP5507584B2 (ja) | アミン放出物制御のための方法およびプラント | |
WO2013039041A1 (ja) | Co2回収装置およびco2回収方法 | |
JP5968159B2 (ja) | Co2回収装置およびco2回収方法 | |
US9399939B2 (en) | Combustion exhaust gas treatment system and method of treating combustion exhaust gas | |
JP5738137B2 (ja) | Co2回収装置およびco2回収方法 | |
WO2010122830A1 (ja) | Co2回収装置及びco2回収方法 | |
JP5597260B2 (ja) | 燃焼排ガス中の二酸化炭素除去装置 | |
JP2007190553A (ja) | アミン回収方法及び装置並びにこれを備えた脱炭酸ガス装置 | |
JP2015134334A (ja) | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 | |
WO2016072292A1 (ja) | Co2回収装置およびco2回収方法 | |
WO2019168180A1 (ja) | Co2回収装置及びco2回収方法 | |
JP6004821B2 (ja) | Co2回収装置およびco2回収方法 | |
JP6811759B2 (ja) | Co2回収装置およびco2回収方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 13828178 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 14409889 Country of ref document: US |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2013828178 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 2877926 Country of ref document: CA |
|
ENP | Entry into the national phase |
Ref document number: 2013300927 Country of ref document: AU Date of ref document: 20130529 Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |