WO2014175338A1 - 二酸化炭素の回収方法及び回収装置 - Google Patents
二酸化炭素の回収方法及び回収装置 Download PDFInfo
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- WO2014175338A1 WO2014175338A1 PCT/JP2014/061445 JP2014061445W WO2014175338A1 WO 2014175338 A1 WO2014175338 A1 WO 2014175338A1 JP 2014061445 W JP2014061445 W JP 2014061445W WO 2014175338 A1 WO2014175338 A1 WO 2014175338A1
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
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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
- B01D53/1406—Multiple stage absorption
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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
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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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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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
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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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
- B01D53/34—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
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
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- 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
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- 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
- B01D2252/2041—Diamines
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- 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
- B01D2252/20436—Cyclic amines
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- 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
- B01D2252/20436—Cyclic amines
- B01D2252/20442—Cyclic amines containing a piperidine-ring
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- 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
- B01D2252/20436—Cyclic amines
- B01D2252/20447—Cyclic amines containing a piperazine-ring
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- 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
- B01D2252/20478—Alkanolamines
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- 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
- B01D2252/20478—Alkanolamines
- B01D2252/20484—Alkanolamines with one hydroxyl group
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- 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
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
- B01D2259/652—Employing advanced heat integration, e.g. Pinch technology using side coolers
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- 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
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
Definitions
- the present invention relates to a carbon dioxide recovery method and recovery device for separating and recovering carbon dioxide from a gas containing carbon dioxide such as combustion gas and reducing clean gas to the atmosphere.
- the absorbent In the chemical absorption method, mainly alkanolamine-based basic compounds are used as the absorbent.
- an aqueous liquid containing the absorbent is generally used as the absorbent, and carbon dioxide contained in the gas is absorbed into the absorbent.
- the absorbing solution is circulated so as to alternately repeat the absorbing step to be performed and the regeneration step of regenerating the absorbing solution by releasing the absorbed carbon dioxide from the absorbing solution (see, for example, Patent Document 1 below).
- heating for releasing carbon dioxide is necessary, and in order to reduce the operating cost of carbon dioxide recovery, it is important to reduce the energy required for heating / cooling for regeneration.
- Patent Document 2 For the purpose of reducing the energy required for recovering carbon dioxide from the absorbing liquid, in Patent Document 2 below, steam condensed water generated from a regenerative heater for extracting the absorbing liquid in the regeneration process and exchanging heat with high-temperature steam is used. Residual heat is used to heat the absorbent. Furthermore, in the following Patent Document 3, it is described that a stripping gas is introduced so as to accompany carbon dioxide in order to promote the release of absorbed carbon dioxide. Further, in Patent Document 4 below, the energy required for heating is reduced by using two regeneration towers, each heated to a high temperature or a low temperature, and supplying the absorption liquid regenerated at the low temperature to the interruption of the absorption tower. Is described.
- Patent Document 5 for the purpose of recovering thermal energy from the gas discharged from the regeneration process, a compressor that compresses the gas containing carbon dioxide discharged from the regeneration tower, and the compressor discharges the gas. It describes that the absorption liquid which a regeneration tower holds is supplied to a heat exchanger using a heat exchanger which performs heat exchange of gas, is heated by heat exchange with gas, and is returned to a regeneration tower. Moreover, the following patent document 6 or patent document 7 describes the treatment process of combustion exhaust gas and process exhaust gas for the purpose of reducing the energy required for recovering carbon dioxide from the absorbent.
- the energy required to regenerate the absorption liquid is to compensate for the sensible heat required to raise the temperature of the absorption liquid, the heat of reaction when carbon dioxide is released from the absorption liquid, and the heat loss due to moisture evaporation of the absorption liquid.
- recovery related to these heats is performed, but there is still room for improvement in order to efficiently recover and reuse energy related to latent heat.
- An object of the present invention is to provide a carbon dioxide recovery method and a recovery apparatus that can solve the above-described problems and reduce the energy required for regenerating the absorbing liquid to reduce the operation cost.
- Another object of the present invention is to reduce the burden on the apparatus and the absorbing liquid, improve the durability of the equipment and the stability of processing, and reduce the energy required to regenerate the absorbing liquid without reducing the carbon dioxide recovery rate. Then, it is providing the recovery method and recovery apparatus of a carbon dioxide which can collect
- an object of the present invention is to provide a configuration of a carbon dioxide recovery device that can be applied to an existing carbon dioxide recovery device to realize improvement in energy efficiency related to regeneration of an absorbing solution.
- the present inventors have conducted extensive research, and as a result, in order to reduce the amount of water vapor contained in the recovered carbon dioxide in order to sufficiently recover the thermal energy related to latent heat, the absorption process and In the adjustment and management of processing conditions, it is advantageous to use a configuration in which the regeneration process is divided into at least two stages, and the absorption liquid is circulated using a circulation system that partially diverges and merges.
- the present invention has been found to be effective, and the present invention has been completed with high applicability and applicability.
- a carbon dioxide recovery device is an absorption device that causes a gas to contact an absorption liquid and causes the absorption liquid to absorb carbon dioxide contained in the gas, and includes a first absorption unit and a second absorption unit.
- the absorption device having an absorption portion and disposed so that the gas is supplied to the second absorption portion through the first absorption portion, and heating the absorption liquid that has absorbed carbon dioxide by the absorption device
- the gist includes a compressor that compresses the recovered gas as it is, and a heat recovery system that recovers the heat of the recovered gas compressed by the compressor and supplies the recovered gas to the regenerator.
- the method for recovering carbon dioxide is an absorption process in which gas is brought into contact with an absorbing liquid and carbon dioxide contained in the gas is absorbed into the absorbing liquid. 2 absorption processes, the gas releases the carbon dioxide by heating the absorption process supplied to the second absorption process through the first absorption process and the absorption liquid that has absorbed carbon dioxide in the absorption process.
- a regeneration process for regenerating the absorbing solution which includes a first regeneration step and a second regeneration step, wherein the first regeneration step is performed using an external heating means, and the second regeneration step is the first regeneration step.
- the regeneration treatment heated by the heat of the gas released in the step, the circulation step for circulating the absorption liquid between the second absorption step and the first regeneration step, and the absorption liquid circulated in the circulation step A part is before the second absorption step A circulation process having a tributary process for diverting toward the first regeneration process via the first absorption process and the second regeneration process in sequence, and recovery including water vapor and carbon dioxide discharged from the regeneration process
- the gist of the invention is to have a compression step of compressing the gas as it is and a heat recovery step of recovering the heat of the recovered gas compressed in the compression step and supplying it to the regeneration process.
- the efficiency of recovery and reuse of heat used for regeneration of an absorbing solution is improved, and regeneration is required without reducing the recovery rate of carbon dioxide. Since thermal energy can be reduced, a carbon dioxide recovery method and recovery apparatus effective for reducing operating costs are provided.
- it is easy to detect and adjust the concentration fluctuation of the circulating absorption liquid by circulating the single absorption liquid, and according to the content fluctuation of the gas to be processed. It can easily cope with changes in condition settings. Energy efficiency is high, and the absorbent can be used stably by setting and changing the processing conditions.
- FIG. 1 is a schematic configuration diagram showing a first embodiment of a carbon dioxide recovery apparatus according to the present invention.
- the schematic block diagram which shows 2nd Embodiment of the collection
- the schematic block diagram which shows 3rd Embodiment of the collection
- the schematic block diagram which shows 4th Embodiment of the collection
- absorption treatment that absorbs carbon dioxide contained in the gas into a low-temperature absorption liquid and high-temperature regeneration that regenerates the absorption liquid by releasing the absorbed carbon dioxide from the absorption liquid
- the absorption liquid is circulated between the treatments, and the absorption treatment and the regeneration treatment are alternately repeated.
- the regeneration rate of the absorbent in the regeneration process depends on the heating temperature of the absorbent, and the higher the temperature, the more carbon dioxide gas is released and the residual carbon dioxide concentration in the absorbent becomes lower (see: Jong I. Lee, Frederick D. Otto and Alan E. Mather, "EquilibriumetBetween carbon Dioxide and Aqueous Monoethanolamine Solutions", J.sappl.
- the absorbing liquid in the regeneration process is maintained near the boiling temperature by external heating means using thermal energy supplied from an external heat source.
- the high-temperature regenerated absorbent (lean liquid) that has released carbon dioxide in the regeneration process exchanges heat with the absorbent (rich liquid) that has absorbed carbon dioxide in the absorption process, so that the heated rich liquid is supplied to the regenerative process. Heat energy is recovered and reused.
- the gas containing carbon dioxide released from the absorbing solution in the regeneration process is discharged in a high temperature state including the heat, and the amount of heat contained in the exhaust gas is wasted.
- the temperature of the exhaust gas can be lowered, that is, the top temperature of the regenerator can be lowered by lowering the heat exchange rate between the rich liquid and the lean liquid, but the sensible heat recovered in the heat exchange is reduced. Does not contribute to the reduction of heat.
- the absorption process and the regeneration process are each divided into two stages to constitute two sets of the absorption process and the regeneration process, and when the absorbent is circulated through two independent circulation paths, the heat exchange rate is not lowered.
- the top temperature of the regenerator can be lowered, the amount of heat contained in the exhaust gas can be reduced, and the heat recovered by heat exchange can be used for the regeneration of the absorbent.
- the semi-rich liquid that has undergone the absorption process at the upper part of the absorber is actively heated using an external heat source at the lower part of the regenerator to sufficiently regenerate the lean liquid, and then refluxed to the upper part of the absorber.
- the rich liquid that has sufficiently absorbed carbon dioxide through the absorption process at the lower part of the apparatus is heated at the upper part of the regenerator using the heat released from the gas that rises from the lower part of the regenerator to regenerate it into a semi-lean liquid. If it comprises so that it may recirculate
- the above-described configuration has a property that the concentration of the absorption liquid in the two circulation paths is likely to be increased due to the water vapor evaporated from the absorption liquid in one circulation path being transferred to the absorption liquid in the other circulation path.
- a circulation mechanism in which one of the two circulation paths is configured as a branch flow path that branches from the other circulation path and joins. That is, the concentration fluctuation of the absorbing solution that can occur in the branched path by partially coupling the two circulation paths is eliminated by the merge.
- a circulation system having a branch flow path that divides and merges another set of absorption process and regeneration process from the circulation path that circulates through one set of absorption process and regeneration process is used. Then, a single absorbing liquid is circulated, and based on this configuration, the thermal energy contained in the recovered gas discharged from the regenerator is recovered and reused.
- the use efficiency of thermal energy is improved by suppressing and collecting exhaust heat, and a carbon dioxide recovery method and a recovery device having a configuration in which the absorption liquid can be easily managed are provided. Adjustment is easy, which is advantageous for reducing the regenerative energy required for carbon dioxide recovery and improving the carbon dioxide recovery efficiency.
- FIG. 1 shows an embodiment of the carbon dioxide recovery apparatus of the present invention.
- the recovery apparatus 1 contacts the gas G containing carbon dioxide with the absorption liquid to absorb the carbon dioxide into the absorption liquid, and heats the absorption liquid that has absorbed the carbon dioxide to release the carbon dioxide from the absorption liquid.
- a regenerator 20 that regenerates the absorbing liquid.
- the absorber 10 and the regenerator 20 are each configured as a tower-shaped counter-current gas-liquid contact device, and are filled with fillers 11 and 21 for increasing the contact area.
- an aqueous liquid containing a compound having an affinity for carbon dioxide such as alkanolamines as an absorbent is used.
- the fillers 11 and 21 are made of a material having durability at a processing temperature and corrosion resistance, and can be appropriately selected and used in a shape capable of providing a desired contact area. Although those made of an iron-based metal material such as steel are used, it is not particularly limited. Furthermore, you may provide the cooling tower for maintaining the gas G supplied to the absorber 10 at the low temperature suitable for absorption of a carbon dioxide as needed.
- the gas G containing carbon dioxide is supplied from the lower part of the absorber 10.
- the absorption device 10 is partitioned into a lower first absorption portion 12a in which the filler 11a is accommodated and an upper second absorption portion 12b in which the filler 11b is accommodated, and the first absorption portion 12a and the second absorption portion 12b.
- the partition member 13 by which the tubular wall was standingly arranged in the center hole periphery of a horizontal annular plate is interposed.
- the partition member 13 is configured so that the shade covers the upper end hole of the tubular wall, and a liquid pool is formed on the horizontal annular plate between the inner wall of the absorber 10 and the tubular wall of the partition member 13. Yes.
- the absorption liquid is supplied from the upper part of the second absorption part 12b of the absorption device 10, is stored in the liquid pool of the partition member 13 after flowing down the filler 11b, and does not flow down to the first absorption part, but the flow path L1.
- the path of this absorption liquid branches off in the tank 14.
- the flow path L 2 connects the tank 14 and the central part of the regeneration device 20
- the flow path L 3 connects the tank 14 and the central part of the absorption device 10. Connecting.
- the absorption liquid in the tank 14 is divided, and one is supplied to the regenerator 20 through the flow path L2 by the pump 16, and the other absorption liquid is supplied to the first absorption apparatus 10 through the flow path L3 by the pump 17. After being supplied to the upper part of the absorption part 12a and flowing down the filler 11a, it is stored in the bottom part of the absorption apparatus 10.
- a vent pipe V ⁇ b> 1 communicating with the second absorption unit is connected to the top of the tank 14 (indicated by a two-dot chain line in the drawing), and the flow path L ⁇ b> 3 has an absorption.
- a cooler 15 and a pump 17 for cooling the liquid are provided.
- the gas G sequentially comes into gas-liquid contact with the absorbing liquid while passing through the fillers 11a and 11b, and the carbon dioxide in the gas G is absorbed by the absorbing liquid. Since the carbon dioxide concentration of the gas after passing through the first absorption portion 12a has decreased, the absorption liquid supplied to the second absorption portion 12b comes into contact with a gas having a lower carbon dioxide concentration than the gas G.
- Absorbing liquid A2 ′ absorbed in the liquid reservoir of partition member 13 by absorbing carbon dioxide in second absorbing portion 12b is a semi-rich liquid, and a part thereof is supplied from tank 14 to regenerator 20 through flow path L2.
- the remaining portion is diverted from the tank 14 and supplied to the first absorption portion 12a via the cooler 15 to further absorb carbon dioxide to become a rich liquid and stored in the bottom of the absorption device 10.
- Absorbing liquid (rich liquid) A1 at the bottom of the absorber 10 is supplied by the pump 18 to the regenerator 20 through a flow path L4 connecting the bottom of the absorber 10 and the top of the regenerator 20.
- the gas G ′ from which carbon dioxide has been removed is discharged from the top of the absorber 10.
- a cooling condensing unit 19 for condensing water vapor or the like that can be contained in the gas G ′ is provided at the top of the absorbing device 10 as necessary. It is done. Thereby, it can suppress to some extent that water vapor
- Condensed water or the like cooled by the cooler 31 and supplied to the top of the tower maintains the cooling condensing unit 19 at a low temperature and reliably cools the gas G ′ passing through the cooling condensing unit 19.
- the drive of the pump 32 is controlled so that the temperature of the gas G ′ discharged to the outside of the tower is preferably about 60 ° C. or less, more preferably 45 ° C. or less.
- the water condensed in the cooling condensing unit 19 is supplied to the filler 11b, but the condensed water can be used to compensate for the composition variation of the absorption liquid in the tower, so that absorption is performed as necessary.
- the reproduction apparatus 20 is partitioned into a lower first reproduction unit 22a in which the filler 21a is accommodated and an upper second reproduction unit 22b in which the filler 21b is accommodated, and the first reproduction unit 22a and the second reproduction unit 22b.
- a partition member 23 that forms a liquid pool with a structure similar to that of the partition member 13 is interposed between the regenerator 22b.
- the absorption liquid A1 supplied from the bottom of the absorption device 10 through the flow path L4 is introduced into the upper part of the second regeneration unit 22b of the regeneration device 20, and is stored in the liquid reservoir of the partition member 23 after flowing down the filler 21b.
- the first regeneration unit 22a is configured to be led out of the tower by the flow path L5 and stored in the tank 24 without flowing down.
- Absorbing liquid A2 ′ supplied from the second absorption portion 12b of the absorption device 10 through the flow paths L1 and L2 is supplied to the top of the first regeneration portion 22a, and is stored at the bottom of the regeneration device 20 after flowing down the filler 21a.
- a reboiler is attached as an external heating means for actively heating the absorption liquid using externally supplied energy. That is, a steam heater 25 provided outside the regenerator 20 and a circulation path 26 for circulating the absorbent A2 stored in the tower bottom through the steam heater 25 are attached, and a part of the absorbent A2 at the tower bottom is attached.
- the flow is divided by the circulation path 26, supplied to the steam heater 25, continuously heated by heat exchange with the high-temperature steam, and returned to the tower. Accordingly, the absorption liquid A2 at the bottom is positively heated by the external heating means to sufficiently release carbon dioxide, and the filler 21a is also indirectly heated to emit carbon dioxide due to gas-liquid contact on the filler 21a. Carbon release is promoted.
- the high-temperature gas containing carbon dioxide and water vapor released from the absorbing liquid rises and passes through the filler 21a of the first regeneration unit 22a, and then passes through the tubular wall inner hole of the partition member 23 to form the second regeneration unit 22b. Passes through the filler 21b. During this time, the absorbing liquid A2 'flowing down the filler 21a and the absorbing liquid A1 flowing down the filler 21b are heated, and the carbon dioxide in the absorbing liquids A1 and A2' is released.
- the absorbing liquid A1 supplied to the second regeneration unit 22b is not positively heated by the external heating means and is heated only by the heat of the gas released from the first regeneration unit 22a.
- the temperature of the absorbing liquid A1 ′ is lower than that of the absorbing liquid A2. Accordingly, the regeneration degree of the absorbing liquid A1 'is lower than the regeneration degree of the absorbing liquid A2 at the bottom of the column, and becomes a semi-lean liquid.
- the absorbing liquid A1 'from which carbon dioxide has been released by the second regeneration unit 22b flows down from the liquid pool in the partition member 23 to the tank 24 through the flow path L5.
- the bottom of the tank 24 is connected to the flow path L2 by the flow path L6, and the absorbing liquid A1 ′ in the tank 24 is supplied to the flow path L2 by the pump 27 provided in the flow path L6 and supplied from the tank 14.
- a vent pipe V2 communicating with the second regeneration unit 22b is connected to the top of the tank 24 in order to eliminate pressure fluctuations in the tank 24 (indicated by a two-dot chain line in the figure).
- Absorbing liquid A2 (lean liquid) that is stored at the bottom of the regenerator 20 and sufficiently releases carbon dioxide is pumped through the flow path L7 that connects the top of the absorber 10 and the bottom of the regenerator 20 by the pump 28. 2 is refluxed to the upper part of the absorber 12b.
- a circulation system is formed in which the absorption liquids A2 and A2 'reciprocate between the second absorption part 12b and the first regeneration part 22a through the flow paths L1, L2 and L7.
- a part of the absorption liquid A2 ′ in the circulation system is divided by the flow paths L3 to L6 to obtain the absorption liquids A1 and A1 ′ through the first absorption part 12a and the second regeneration part 22b in order.
- a tributary system is formed that joins the system absorption liquid A2 ′. That is, the flow paths L1, L2, and L7 form a circulation path between the second absorption section and the first regeneration section, and the flow paths L3 to L6 are branched from the circulation path to form the second absorption section 12b. From the first through the first absorption unit 12a and the second regeneration unit 22b, a branch channel that is reconnected to the circulation system is formed before reaching the first regeneration unit 22a. The gas containing carbon dioxide released from the absorbing solution in the regenerator 20 is discharged as the recovered gas C from the top of the regenerator 20.
- the absorbing liquid A1 ′ from which carbon dioxide has been released by the second regeneration unit 22b passes through the first heat exchanger 29 while flowing through the flow paths L5 and L6.
- the absorbing liquid in the flow path L4 Heat exchange is performed between A1 and the absorption liquid A1 ′ of the flow path L6. Therefore, the absorption liquid A1 'is cooled by the absorption liquid A1 in the flow path L4 and merges with the absorption liquid A2' in the flow path L2.
- the absorbing liquid A2 from which carbon dioxide has been released by the first regeneration unit 22a passes through the second heat exchanger 30 while flowing through the flow path L7, and in the second heat exchanger 30, the absorbing liquid A2 in the flow path L7.
- the absorption liquid (A1 ′ + A2 ′) in the flow path L2 is cooled by the absorption liquid (A1 ′ + A2 ′) in the flow path L2, and further sufficiently cooled by the cooler 33 using cooling water, and then introduced into the upper part of the second absorption part 12b.
- the heat exchangers such as spiral type, plate type, double pipe type, multiple cylinder type, multiple circular pipe type, spiral tube type, spiral plate type, tank coil type, tank jacket type, direct contact liquid-liquid type, etc.
- any type may be used as the heat exchanger between the absorbing liquids, but the plate type is superior in terms of simplification of the apparatus and ease of cleaning and disassembly.
- the recovered gas C containing carbon dioxide released from the absorbing liquid by heating in the regenerator 20 passes through a condensing part 37 provided at the top of the regenerator 20 in order to suppress discharge of water vapor and absorbent, and then exhausted from the top. It is discharged through the tube 38.
- it has the heat recovery system comprised using the compressor and heat exchanger for collect
- the recovered gas C discharged from the regenerator 20 is compressed as it is without being subjected to condensation and separation of water vapor by cooling.
- Both the heat of gas compression generated by this compression and the heat of condensation of water are collected together by a heat exchanger and reused.
- Heat recovery and supply are performed using a heat exchanger that exchanges heat between the compressed recovered gas C and the absorbent introduced into the regenerator 20, and in the embodiment of FIG. 1, three heat exchangers are used. It is used to recover and supply heat at three locations, but may be omitted at one or two locations, omitting one or two.
- the recovery device 1 divides a part of the absorbing liquid A2 at the bottom of the regenerator 20 from the compressor 40 provided on the exhaust pipe 38 so as to directly communicate with the regenerator 20, and the outside of the regenerator.
- Heat exchangers 41a, 41b attached to the exhaust pipe 38 so as to exchange heat between the circulation path 50 for circulating between them and the recovered gas C compressed by the compressor 40 and the absorbent introduced into the regenerator 20.
- 41c, and the recovered gas C compressed by the compressor 40 sequentially passes through the heat exchanger 41a, the heat exchanger 41b, and the heat exchanger 41c.
- the heat exchanger 41a is provided on the circulation path 50, and performs heat exchange between the recovered gas C and the absorption liquid A2 in the circulation path 50.
- the heat exchanger 41b is disposed between the second heat exchanger 30 and the first regeneration unit 22a in the flow path L2, and performs heat exchange between the recovered gas C and the absorbing liquid (A1 '+ A2').
- the heat exchanger 41c is disposed between the first heat exchanger 29 and the second regeneration unit 22b in the flow path L4, and performs heat exchange between the recovered gas C and the absorbing liquid A1.
- the temperature of the recovered gas C decreases every time it passes through the heat exchanger, and the water vapor contained in the recovered gas C cools and condenses, so that the heat of condensation is released. Therefore, in the heat exchangers 41a to 41c, Condensation heat is also recovered and supplied to the absorbent.
- various heat exchangers generally used for gas-liquid heat exchange can be appropriately selected and used.
- direct contact type, fin tube type, plate A heat exchanger such as an equation is mentioned.
- the regenerator 20 of the present invention the regenerator is configured in two stages, and the tower top temperature of the regenerator 20 is lower than that in the single-stage structure. This configuration is suitable for preventing corrosion of the compressor 40.
- the absorption liquid A2 in the circulation path 50 heated by the heat exchanger 41a is refluxed to the bottom of the regenerator 20, and the absorption liquid (A1 ′ + A2 ′) in the flow path L2 heated by the heat exchanger 41b is the first.
- the absorption liquid A1 of the flow path L4 introduced into the upper part of the regeneration unit 22a and heated by the heat exchanger 41c is introduced into the upper part of the second regeneration unit 22b. Therefore, in any case, the heat recovered from the recovered gas C is supplied to the regenerator 20.
- the absorption liquid A2 after heat exchange in the heat exchanger 41a is directly returned to the regenerator 20, but the circulation path 50 may be connected so as to return through the steam heater 25. Good.
- the recovered gas C of the exhaust pipe 38 that has undergone heat recovery by the heat recovery system is sufficiently cooled by the cooler 42 using cooling water to condense the water vapor as much as possible, and then condensed by the gas-liquid separator 43. It is collected after removing.
- Carbon dioxide in the recovered gas C can be fixed and reorganized in the ground by, for example, injecting it into the ground or an oil field.
- the pressure of the recovered gas C by the compressor 40 can be effectively used, for example, as a working pressure such as an injection pressure in the processing of recovered carbon dioxide.
- the bottom of the gas-liquid separator 43 is connected to the downstream side of the second heat exchanger 30 of the flow path L7 by the water supply path 45, and the pressure reducing means for releasing the applied pressure on the water supply path 45.
- a pressure reducing valve 44 is provided.
- the condensed water separated in the gas-liquid separator 43 is depressurized and adjusted to a pressure suitable for introduction into the absorber 10 by the pressure reducing valve 44, and added from the water supply path 45 to the absorbing liquid A2 in the flow path L7.
- the absorption liquid A2 in the flow path L7 is returned to the upper part of the second absorption portion 12b of the absorption device 10 after being cooled by the cooler 33.
- the condensed water generated from the recovered gas C is used to compensate for the composition variation of the absorbing liquid A2 supplied to the absorber 10.
- the pressure reducing valve 44 for example, what is generally used as a pressure adjusting valve or a back pressure valve may be used.
- a pressure gauge 46 is connected to the exhaust pipe 38 in order to detect the pressure in the regenerator 20, and the output of the motor 40M of the compressor 40 is controlled according to the detected pressure value.
- the operation of the compressor 40 is adjusted so that the pressure is maintained constant (in the figure, the connection indicated by the alternate long and short dash line indicates an electrical connection).
- output efficiency using an inverter or the like is used, so that energy efficiency is good.
- the pressure release and adjustment of the condensed water can be changed by using an expander instead of the pressure reducing valve 44.
- the expander and the compressor 40 are coaxial rotors. If it is configured as a heat pump that cooperates to drive, the operating efficiency is improved.
- the above-described embodiment can be modified so that a plurality of compressors arranged in series are used as the compressor 40, and the amount of recovered heat by heat exchange can be increased.
- the compressor is connected so that the compressor is located between the heat exchanger 41a and the heat exchanger 41b and between the heat exchanger 41b and the heat exchanger 41c. If the recovery gas C that has passed through 41a is configured such that compression and heat exchange are alternately repeated, the compression heat recovery efficiency is good.
- each heat exchanger can be modified to repeat multi-stage heat exchange by a plurality of heat exchangers, or the exhaust pipe 38 and the circulation path 50 (or the flow paths L2 and L4) can be respectively changed.
- the plurality of heat exchangers may be arranged so as to be branched into a plurality of parallel paths and to exchange heat between them.
- the temperature of the absorbent A2 heated at the bottom of the first regenerator 22a is T1
- the absorbent (A1 ′ + A2 ′) introduced from the second heat exchanger 30 to the top of the first regenerator 22a If T2 is T2, then T1> T2.
- the temperature of the liquid absorption liquid A1 ′ in the pool heated by the second regeneration unit 22b by the gas released from the first regeneration unit 22a is T3, and is introduced from the first heat exchanger 29 to the second regeneration unit 22b.
- T1> T3 where T4 is the temperature of the absorbing liquid A1 and T2 is the temperature of the gas released from the first regeneration unit 22a to the second regeneration unit 22b and t2 is the temperature of the gas released from the second regeneration unit 22b.
- the absorbing liquid in the regenerator is heated near the boiling point of the absorbing liquid in order to increase the degree of regeneration.
- the heat recovery rate is increased by using a heat exchanger having high heat exchange performance and the temperature difference (T1-T2) is reduced, the temperature t1 of the gas released from the first regeneration unit 22a is also increased. If discharged, it not only releases sensible heat energy, but also releases a large amount of latent heat energy together with water vapor.
- the amount of heat of the gas released from the first regeneration unit 22a is recovered in the second regeneration unit 22b and used for regeneration of the absorption liquid, and the sensible heat is released by lowering the gas temperature from t1 to t2. Reduce the amount.
- the condensation of water vapor also proceeds, so the water vapor and latent heat contained in the recovered gas C released from the second regeneration unit 22b also decrease.
- the condensed water vapor evaporated from the absorption liquid is absorbed into the absorption liquid A2 ′ of the second absorption section 12b in the absorption apparatus 10, and the absorption liquid A1 of the second reproduction section 22b in the regeneration apparatus 20. Supplied to '. Therefore, in the circulation system, even if the vaporized portion from the absorbing liquid A2 in the first regeneration unit 22a exceeds the condensed moisture supplemented in the second absorbing unit 12b, a part of the absorbing liquid is divided and flows through the branch channel.
- the concentration fluctuation of the absorbing solution is reduced. Further, since the amount of condensed water increases by recovering heat from the recovered gas C using the compressor 40 and the heat exchangers 41a to 41c, the amount of water vapor and latent heat discharged from the regenerator 20 decreases. Further, since the temperature of the condensed water in the gas-liquid separator 43 is lowered by releasing the pressure in the pressure reducing valve 44, it is suitable for addition to the absorbing liquid A2 to be refluxed to the absorbing device 10, and is necessary for the cooler 33. It is also useful for reducing the amount of cooling heat.
- a gas G containing carbon dioxide such as combustion exhaust gas and process exhaust gas is supplied from the bottom, and the pumps 16 to 18, 27 and 28 are driven, and the absorption liquids A2 ′ and A2 are supplied to the first and second liquids. If each is supplied from the upper part of absorption part 12a, 12b, gas G and absorption liquid A2 ', A2 will carry out gas-liquid contact on filler 11a, 11b, and the 1st absorption process and 2nd absorption in the 1st absorption part 12a will be carried out.
- the absorption process which consists of the 2nd absorption process in the part 12b is performed, and a carbon dioxide is absorbed by absorption liquid A2 ', A2.
- the liquid temperature of the absorbing liquids A2 ′ and A2 or the absorption device 10 is generally set to about 50 ° C. or lower, preferably 40 ° C. or lower. Adjust the temperature. Since the absorbing liquid generates heat due to absorption of carbon dioxide, it is desirable to take into account the rise in liquid temperature caused by this, so that the liquid temperature does not exceed 60 ° C.
- the gas G supplied to the absorption device 10 may be adjusted to an appropriate temperature in advance using a cooling tower if necessary in consideration of the above.
- An aqueous liquid containing a compound having affinity for carbon dioxide as an absorbent is used as the absorbent.
- Examples of the absorbent include alkanolamines and hindered amines having an alcoholic hydroxyl group.
- alkanolamine examples include monoethanolamine, diethanolamine, triethanolamine, N-methyldiethanolamine (MDEA),
- MDEA N-methyldiethanolamine
- examples of the hindered amine having an alcoholic hydroxyl group examples include 2-amino-2-methyl-1-propanol (AMP), 2- (ethylamino) ethanol (EAE), and the like.
- Examples include 2- (methylamino) ethanol (MAE), 2- (isopropylamino) ethanol (IPAE), and a plurality of the above compounds may be used in combination.
- Piperidine, piperazine, pyridine, pyrimidine, pyrazine, 3-methylpyridine, 2-methylpyrazine, 2- (methylamino) piperidine (2AMPD), 2-methylpiperazine, 2- (aminomethyl) piperazine, 2,6- A cyclic amine such as dimethylpiperazine, 2,5-dimethylpiperazine, 2- ( ⁇ -hydroxyethyl) piperazine and the like may be added and mixed.
- Monoethanolamine (MEA) which is generally preferred for use, is an absorbent having high absorbability, and examples of the absorbent having good regenerative properties include AMP and MDEA. Frequently, MEA is mixed to improve the absorption of AMP and MDEA, and the absorption liquid is composed.
- the absorption and regeneration can be adjusted to some extent depending on the mixing ratio, so that the regeneration energy can be reduced.
- the absorbent concentration of the absorbent can be appropriately set according to the amount of carbon dioxide contained in the gas to be treated, the treatment speed, the fluidity of the absorbent and the suppression of consumption loss, and is generally 10 to 50% by mass. For example, for the treatment of the gas G having a carbon dioxide content of about 20%, an absorbing solution having a concentration of about 30% by mass is preferably used.
- the supply rate of the gas G and the circulation rate of the absorption liquid are determined so that the absorption proceeds well in consideration of the amount of carbon dioxide contained in the gas G, the carbon dioxide absorption capacity of the absorption liquid, the gas-liquid contact efficiency in the filler, and the like. Is set as appropriate.
- the absorption process and the regeneration process are repeatedly executed by the circulation of each absorption liquid.
- the regeneration process of the absorbent in the regenerator 20 uses the first regeneration process in which the absorbent is heated by external heating in the first regeneration unit 22a and the heat of the gas released from the first regeneration process in the second regeneration unit 22b. And a second regeneration step of heating. Part of the absorption liquid A2 '(semi-rich liquid) that has absorbed carbon dioxide in the second absorption process is supplied from the tank 14 to the first regeneration process in the first regeneration unit 22a through the flow path L2.
- the remaining portion flows from the tank 14 through the flow paths L3 and L4, and after performing the first absorption step in the first absorption portion 12a and the second regeneration step in the second regeneration portion 22b, the semi-regenerated absorption liquid A1 ′ ( As the semi-liquid), the fluid merges with the absorption liquid A2 ′ of the flow path L2 through the flow paths L5 and L6 and travels toward the first regeneration unit 22a.
- the absorption liquid A1 ′ of the flow path L5 merges with the absorption liquid A2 ′ of the flow path L2, the flow path before being supplied to the second regeneration process in the first heat exchange process by the first heat exchanger 29. Heat exchange with the L4 absorbent A1.
- the absorption liquid (A2 ′ + A1 ′) merged at the connection between the flow path L2 and the flow path L6 is supplied by the second heat exchanger 30 before being supplied to the first regeneration process in the first regeneration section 22a.
- the heat is exchanged with the absorbing liquid A2 that is refluxed through the first regenerating step in the regenerator 20.
- the temperature T1 of the absorbent A2 heated by external heat in the first regeneration step in the first regeneration unit 22a varies depending on the composition of the absorbent used and the regeneration conditions, but is generally set to about 100 to 130 ° C. (near the boiling point). Based on this, the temperature of the absorption liquid (A2 ′ + A1 ′) after the second heat exchange step is about 90 to 125 ° C., and the introduction temperature T2 to the first regeneration unit 22a is the heat exchanger 41b. Depending on the temperature.
- the temperature t1 of the recovered gas C released from the first regeneration unit 22a to the second regeneration unit 22b is about 90 to 120 ° C., and is heated by the second regeneration unit 22b by the gas released from the first regeneration unit 22a.
- the temperature T3 of the absorbed liquid A1 ′ is about 85 to 120 ° C.
- the first heat with the absorption liquid A1 supplied from the absorption device 10 to the regeneration device 20 is obtained. Cooled by heat exchange by the exchanger 29, the temperature of the absorbing liquid A1 rises to about 80 to 110 ° C., and the temperature T4 of the absorbing liquid A1 introduced into the second regeneration unit 22b is the temperature in the heat exchanger 41c. It can be set to about 85 to 115 ° C. by heating.
- the temperature t2 of the recovered gas C released from the second regeneration unit 22b is about 65 to 100 ° C.
- S be the flow rate of the absorption liquid flowing through the flow path before and after the diversion in the circulation process in which the absorption liquid circulates through the circulation system formed by the flow paths L1, L2, and L7 (for example, the flow rate of the absorption liquid A2 in the flow path L7).
- the flow rate in the tributary process after branching that is, the flow rate of the absorption liquids A1 and A1 ′ flowing through the tributary flow paths L3 to L6 is ⁇ S
- the ratio of the flow rate ⁇ S to the flow rate S: ⁇ S / S is the gas G
- it is generally set appropriately to about 1/10 to 9/10, and in consideration of heat recovery and regeneration efficiency in the second regeneration unit 22b, It is preferable to set it to about 4/10 to 8/10.
- This ratio ⁇ S / S is substantially equal to the ratio of the filling volume of the filling material 11a of the first absorbent portion 12a to the filling volume of the filling material 11 in the absorption device 10, and the filling material 21 in the regeneration device 20 It is good to design so that it may become substantially equal to the ratio of the filling volume of the filler 21b of the 2nd reproduction
- the difference in carbon dioxide content between the absorption liquid A2 ′ (semi-rich liquid) supplied from the tank 14 to the first regeneration unit 22a and the absorption liquid A1 ′ (semi-lean liquid) that merges from the tank 24 to the flow path L2 is the flow rate.
- the ratio ⁇ S / S also changes.
- the flow rates S and ⁇ S can be adjusted by controlling the driving of the pumps 16 to 18, 27 and 28. At this time, the liquid level in the tanks 14 and 24 is detected, and the pumps are adjusted according to the fluctuations. An appropriate flow rate in a steady state can be set by balancing the driving. Therefore, when the driving conditions of the pump for circulating the absorbing liquid at an appropriate flow rate are known in advance, the tanks 14 and 24 can be omitted.
- the temperature of the upper part of the regeneration device 20 ( ⁇ the temperature t2 of the recovered gas C) is close to the temperature T4 of the absorbing liquid A1 to be charged (T2 ⁇ t1, T4 ⁇ T3 ⁇ t1). Therefore, the absorbent contained in the recovered gas C passing through the condensing unit 37 is reduced, and corrosion due to the absorbent such as equipment provided in the exhaust pipe 38 is prevented.
- the second regeneration unit 22b is suitable for performing regeneration using exhaust heat of gas.
- the absorbing liquid A2 stored at the bottom of the regenerator 20 is heated to the vicinity of the boiling point by partial circulation heating.
- the boiling point of the absorbing liquid depends on the composition (absorbent concentration) and the pressure in the regenerator 20.
- heating it is necessary to supply the latent heat of vaporization of water lost from the absorbing liquid and the sensible heat of the absorbing liquid.
- the sensible heat increases due to the rise in boiling point. Therefore, in consideration of these balances, it is preferable in terms of energy efficiency to use a condition setting in which the inside of the regenerator 20 is pressurized to about 100 kPaG and the absorbent is heated to 120 to 130 ° C.
- the operation of the compressor 40 has the effect of lowering the internal pressure of the regenerator 20. Therefore, in order to pressurize the regenerator 20, the exhaust pressure from the exhaust pipe 38 is controlled by using an on-off valve or the like to increase the pressure in the tower. Thereafter, the internal pressure of the regenerator 20 and the outlet pressure of the compressor 40 may be adjusted while controlling the operation of the compressor 40.
- the recovered gas C containing carbon dioxide released from the absorbing liquid is directly compressed by the compressor 40, the gas temperature rises due to an increase in pressure, and it becomes easy to recover heat by heat exchange.
- the heat recovery process in the heat exchanger 41a the water vapor contained in the recovered gas C is condensed and the heat of condensation of the water is also released.
- the compression rate by the compressor 40 may be adjusted so that the gas temperature after compression is about 120 to 500 ° C., preferably about 5 ° C. higher than the boiling point of the absorbent.
- the pressure of the recovered gas C is set to about 0.3 to 2.0 MPaG by the compression process.
- the pressure in the first stage compression process is 0.
- about 3 to 1.0 MPaG, about 0.5 to 1.5 MPaG in the second stage compression stroke, and about 1.0 to 2.0 MPaG in the third stage compression stroke may be set.
- the compression heat generated by the compression and the heat of condensation of the water are recovered by a part of the absorbing liquid A2 circulated from the regenerator 20 by the heat exchange process in the heat exchanger 41a, and this is returned to the bottom of the regenerator 20,
- the recovered heat is supplied to the absorbent of the regenerator 20.
- the residual heat of the recovered gas C that has passed through the heat exchanger 41a is sequentially recovered by heat exchange between the absorption liquid (A1 ′ + A2 ′) in the flow path L2 and the absorption liquid A1 in the flow path L4 in the heat exchangers 41b and 41c.
- the recovered liquid is supplied to the regenerator 20 by introducing the absorption liquid in the flow paths L2 and L4 into the first regenerator 22a and the second regenerator 22b.
- the temperature of the recovered gas C flowing through the exhaust pipe 38 decreases every time it passes through the heat exchangers 41a to 41c, and is about 100 to 140 ° C. at the outlet of the heat exchanger 41a and 80 to 130 ° C. at the outlet of the heat exchanger 41b. About 70 to 120 ° C. at the outlet of the heat exchanger 41c.
- the condensed water condensed from the recovered gas C after the heat recovery step is subjected to the separation step by the gas-liquid separator 43, and then the pressure is released by the pressure reducing valve 44 and added to the absorbing liquid A2 flowing through the flow path L7. Then, it is refluxed to the second absorption part 12b of the absorption device 10.
- the temperature of the condensed water in the gas-liquid separator 43 is about 40 to 50 ° C., and the water temperature is further lowered by vaporization due to the pressure reduction in the pressure reducing valve 44, which is convenient for introduction into the absorption device 10. It is effective in reducing the amount of cooling heat.
- the absorption liquid circulates between the second absorption unit 12b of the absorption device 10 and the first regeneration unit 22a of the regeneration device 20, while part of the first absorption unit 12a and the first absorption unit 12a in the tributary system.
- the second regeneration unit 22b By passing through the second regeneration unit 22b, carbon dioxide absorbed at a higher concentration is released at a lower temperature.
- the energy efficiency of the regeneration device is improved by the heat utilization in the second regeneration unit 22b that performs regeneration at a temperature lower than that of the first regeneration unit 22a.
- a circulation system that performs main absorption-regeneration is configured, and heat energy in the regenerator is recovered and reused in the branch flow paths by the flow paths L3 to L6.
- a tributary system is formed that is also effective in reducing the absorption load that the gas G having a high carbon dioxide concentration gives to the absorbent.
- the release of the pressure applied using the compressor 40 in the heat recovery from the recovered gas C cools the condensed water generated from the recovered gas C, so that it is added as a correction of the concentration of the absorbing liquid returning to the absorber 10.
- Condensed water is also convenient in terms of temperature control. Therefore, the apparatus configuration in FIG. 1 is effective in improving the heat adaptability of the recovery apparatus by improving the efficiency of use of the thermal energy in the regenerator by recovering and reusing the thermal energy.
- any of the three heat exchangers 41a to 41c can be used to recover and reuse heat from the recovered gas C, and a recovered heat regeneration apparatus 20 using a plurality of heat exchangers.
- the effect of reducing the regenerative energy is increased by repeating the supply to.
- the form using the heat exchangers 41a and 41c has less regeneration energy than the form using the heat exchangers 41a and 41b.
- One reason for this is that the heat exchange performance cannot be satisfactorily exhibited because the difference between the inlet temperature of the recovered gas C and the inlet temperature of the absorbing liquid (A1 '+ A2') in the heat exchanger 41b is small. That is, when the heat exchanger 41c is used, the temperature difference between the recovered gas C and the absorbing liquid A1 at the heat exchanger inlet is such that the heat exchange performance is suitably exhibited. Even if the amount of water vapor and latent heat to be increased are recovered again, as a result, the efficiency becomes higher than using the heat exchanger 41b.
- FIG. 2 shows a second embodiment of the recovery apparatus for implementing the carbon dioxide recovery method of the present invention.
- a branch flow path L2 ′ branched from the flow path L2 and a third heat exchanger 34 are provided, and the absorption liquid (A2 ′ + A1 ′) supplied from the tanks 14 and 24 to the flow path L2 is provided.
- a part of the steam is supplied to the third heat exchanger 34 without being introduced into the second heat exchanger 30, and the third heat exchanger 34 uses the remaining heat of the steam condensate discharged from the steam heater 25. Heat. Since the high-temperature steam of the steam heater 25 is sufficiently high-temperature steam condensed water of about 120 ° C.
- the absorption liquid heated by the third heat exchanger 34 merges with the absorption liquid in the flow path L2 on the downstream side of the second heat exchanger 30 in the flow path L2, passes through the heat exchanger 41b, and then enters the first regeneration unit 22a. Supplied.
- Heat recovery from the compressed recovered gas C in the exhaust pipe 38 is performed by the heat exchangers 41a to 41c as in the embodiment of FIG. 1, and the first recovery is performed from the absorption liquid A2 and the flow path L2 at the bottom of the regenerator 20. Recovery heat is supplied to each of the absorption liquid (A2 ′ + A1 ′) supplied to the regeneration unit 22a and the absorption liquid A1 supplied from the flow path L4 to the second regeneration unit 22b.
- the temperature of the absorbing liquid supplied to the first regeneration unit 22a can be set higher than that in the embodiment of FIG. 1 by the heat supplied in the third heat exchanger 34.
- the heat exchanger 41c can easily recover the amount.
- the heating temperature of the absorption liquid A1 in the flow path L4 can be higher than that in the embodiment of FIG. That is, heat recovery from the compressed recovered gas C in the exhaust pipe 38 can be suitably performed by the heat exchangers 41a and 41c.
- the third heat exchanger 34 can share the role of the second heat exchanger 30 that heats the absorbent supplied from the flow path L2 to the first regeneration unit 22a. Therefore, it is possible to use a smaller one as the second heat exchanger 30.
- any of the three heat exchangers 41a to 41c can recover and reuse heat from the recovered gas C, and one or two of these can be arbitrarily omitted. It is also possible to do.
- FIG. 3 shows a third embodiment of a recovery apparatus that implements the carbon dioxide recovery method of the present invention.
- the configuration is simplified by reducing the number of pumps and tanks. That is, the recovery device 3 in FIG. 3 includes a tank 14 ′ corresponding to the tank 24 of the recovery device 1 in FIG. 1 integrated with the tank 14, and is configured to omit the tank 24 in FIG. 1. As a result, the pump 27 of FIG. Also, the pump 17 of the flow path L3 in FIG. 1 is configured to be omitted.
- a branching point that divides the absorption liquid A2 ′ of the flow path L1 led out of the absorption device 10 from the liquid reservoir of the second absorption portion 12b into two is provided on the flow path L1 instead of the tank.
- a junction where the tributary system passing from the branch point through the first absorption unit 12a and the second regeneration unit 22b is integrated into the circulation system is not the flow path L2 but the tank 14 ′.
- the absorption liquid A2 'flowing out from the second absorption part 12b through the flow path L1 is divided into two at the three-way valve 47 provided at the branch point on the flow path L1. Part of the absorption liquid A2 'flows down the flow path L1 and is stored in the tank 14', and the other part is supplied to the first absorption part 12a through the flow path L3 ', and is cooled by the cooler 15 therebetween. Since the supply of the absorption liquid A2 ′ from the second absorption unit 12b to the tank 14 ′ and the first absorption unit 12a can be performed using a gravity drop, a pump can be omitted in the flow paths L1 ′ and L3 ′.
- the distribution ratio of the absorbing liquid A2 ′ can be adjusted by setting the three-way valve 47. Furthermore, the absorbing liquid A1 ′ led out of the regenerator 20 from the second regeneration unit 22b through the flow path L6 ′ also flows down due to the gravity drop and is stored in the tank 14 ′, where it is supplied from the flow path L1. It merges with a part of the absorbing liquid A2 ′. That is, the tank 14 ′ functions as both the tank 14 and the tank 24 in FIG. 1, and the absorbing liquid A2 ′ and the absorbing liquid A1 ′ merge in the tank 14 ′.
- the pump 27 that supplies the absorbing liquid A1 ′ to L2 is not necessary in the embodiment of FIG.
- the absorption liquid (A1 ′ + A2 ′) in the tank 14 ′ is supplied to the first regeneration unit 22a through the flow path L2 by the pump 16, and in the meantime, in the second heat exchanger 30, the second absorption from the first regeneration unit 22a. Heat exchange with the absorbing liquid A2 refluxed to the portion 12b through the flow path L7. Further, the absorption liquid A1 'flowing out from the second regeneration unit 22b through the flow path L6' exchanges heat with the absorption liquid A1 flowing out from the bottom of the absorption device 10 through the flow path L4 in the first heat exchanger 29.
- a vent pipe V ⁇ b> 1 ′ communicating with the second absorption portion 12 b is connected to the top in order to eliminate the internal pressure fluctuation (indicated by a two-dot chain line in the drawing).
- Absorbing liquid A2 (lean liquid) that is stored at the bottom of the regenerator 20 and sufficiently releases carbon dioxide is pumped through the flow path L7 that connects the top of the absorber 10 and the bottom of the regenerator 20 by the pump 28. 2 is refluxed to the upper part of the absorber 12b.
- the flow paths L1, L2, and L7 form a circulation path between the second absorption section 12b and the first regeneration section 22a, and the absorption liquids A2 and A2 ′ are second through the flow paths L1, L2, and L7.
- a circulation system that reciprocates between the absorption unit 12b and the first reproduction unit 22a is configured.
- the flow paths L3 ′, L4, L6 ′ are branched from the circulation path so as to reach the first regeneration section 22a from the second absorption section 12b through the first absorption section 12a and the second regeneration section 22b.
- a branch flow path connected to the circulation system is formed, and the absorption liquid A2 ′ is diverted from the circulation system through the flow paths L3 ′, L4, and L6 ′, and the first absorption portion 12a and the second regeneration are formed as absorption liquids A1 and A1 ′.
- a tributary system that merges with the circulation system via the portion 22b is configured.
- the absorption liquid A1 ′ from which carbon dioxide has been released by the second regeneration unit 22b passes through the first heat exchanger 29 while flowing through the flow path L6 ′, and performs heat exchange between the flow path L4 and the flow path L6 ′. Is done. Therefore, the absorption liquid A1 'is cooled by the absorption liquid A1 in the flow path L4, and merges with the absorption liquid A2' in the flow path L1 and the tank 14 '.
- the absorption liquid A2 from which carbon dioxide has been released by the first regeneration unit 22a passes through the second heat exchanger 30 while flowing through the flow path L7, and in the second heat exchanger 30, the flow paths L7 and L2 Heat exchange with the Accordingly, the absorption liquid A2 is cooled by the absorption liquid (A1 ′ + A2 ′) in the flow path L2, and further sufficiently cooled by the cooler 33 using cooling water, and then introduced into the upper part of the second absorption part 12b.
- the heat recovery from the compressed recovered gas C in the exhaust pipe 38 is performed by the heat exchangers 41a to 41c as in the embodiment of FIG. 1, and the first regeneration is performed from the absorbing liquid A2 and the flow path L2 at the bottom of the regenerator 20.
- the recovery device 3 of FIG. 3 is the same as the recovery apparatus 1 of FIG. 1 except for the points described above, and therefore the description thereof is omitted.
- the recovery device 3 of FIG. 3 can also be modified like the recovery device 2 of FIG. That is, the absorption liquid supplied from the tank 14 ′ to the first regeneration unit 22 a through the flow path L 2 is diverted before being supplied to the second heat exchanger 30, and a part thereof is exhausted from the steam heater 25. If the branch flow path and the heat exchanger are provided so as to join the flow path L2 downstream from the second heat exchanger 30 after heating, the second heat exchanger 30 can be downsized as in the embodiment of FIG. Even if the heat exchanger 41b is omitted, it is easy to efficiently recover the heat from the recovered gas C. Further, as in the embodiment of FIG. 1, any of the three heat exchangers 41a to 41c can recover and reuse heat from the recovered gas C, and thus one or two of these can be arbitrarily omitted. It is also possible to carry out.
- FIG. 4 shows a fourth embodiment of a recovery apparatus that implements the carbon dioxide recovery method of the present invention.
- This embodiment is a configuration for improving the heat exchange of the absorbing liquid A1 'supplied from the tank 24 to the flow path L2 in the recovery apparatus of FIG.
- the absorption liquid A1 ′ supplied from the tank 24 to the flow path L2 is once cooled in the first heat exchanger 29, and then merged with the absorption liquid in the flow path L2 and heated again in the second heat exchanger 30.
- the branch flow path L7 ′ is branched from the flow path L7 for refluxing the absorption liquid from the first regeneration section 22a to the second absorption section 12b and connected in parallel, and two heat exchanges are performed instead of the first heat exchanger 29.
- Containers 35a and 35b are provided in the branch flow path L7 ′.
- the absorption liquid A1 'in the tank 24 is heated using heat exchange with the branch flow path L7' and then merged with the flow path L2.
- two heat exchangers 35a and 35b are provided in a branch flow path L7 ′ branched from and parallel to the flow path L7 extending from the first regeneration section 22a to the second absorption section 12b.
- heat exchange is performed between the absorption liquid A1 ′ in the flow path L6 ′′ that joins from the tank 24 to the flow path L2 and the absorption liquid A2 that returns from the regenerating apparatus 20 to the absorption apparatus 10.
- the temperature of the absorbing liquid A2 flowing through the branch flow path L7 ′ is The heat exchange in the heat exchanger 35a decreases to a temperature close to the absorption liquid A1 ′ in the tank 24, so that heat is exchanged with the absorption liquid A1 in the flow path L4 in the downstream heat exchanger 35b.
- the exchange conditions are the same as those of the first heat exchanger 29 in Fig. 1. Therefore, the temperature condition of the absorbing liquid introduced into the regenerator 20 is the same as in the embodiment of Fig. 1, and the exhaust pipe 38 is compressed.
- Heat recovery from the recovered gas C is performed by the heat exchangers 41a to 41c in the same manner as in the embodiment of FIG. 1, and the absorption liquid A2 at the bottom of the regenerator 20 and the absorption supplied from the flow path L2 to the first regenerator 22a. Liquid (A2 '+ A1') and flow path The recovered heat is supplied to each of the absorption liquids A1 supplied to the second regeneration unit 22b from 4.
- the heat recovery effect in the embodiment of Fig. 4 is the same as that of the embodiment of Fig. 1, and is used for recovering carbon dioxide.
- the required regeneration energy is the same as in Table 1.
- the recovery device 4 of FIG. 4 is the same as the recovery device 1 of FIG. 1 except for the points described above, and therefore the description thereof is omitted.
- the recovery device 4 of FIG. 4 can also be modified like the recovery device 2 of FIG. That is, a part of the absorption liquid A2 ′ supplied from the tank 14 to the first regeneration unit 22a through the flow path L2 is diverted before being supplied to the second heat exchanger 30, and the exhaust heat from the steam heater 25 is used. If a branch flow path and a heat exchanger are provided so as to join the flow path L2 downstream from the second heat exchanger 30 after heating, the second heat exchanger 30 can be reduced in size and the heat exchanger 41b is omitted. Even so, it is easy to efficiently recover the heat from the recovered gas C. Further, as in the embodiment of FIG. 1, any of the three heat exchangers 41a to 41c can recover and reuse heat from the recovered gas C, and thus one or two of these can be arbitrarily omitted. It is also possible to carry out.
- FIG. 5 shows a fifth embodiment of a recovery apparatus for implementing the carbon dioxide recovery method of the present invention.
- This embodiment is an embodiment that can be configured by combining two sets of recovery devices.
- the absorption device 10 in the recovery device 1 of FIG. 1 is configured by two independent absorption devices, and the first and the first The two absorption units are distributed to the respective absorption devices, and the reproduction device 20 is configured by two independent reproduction devices, and the first and second reproduction units are distributed to the respective reproduction devices.
- These are connected by piping so that they function in the same manner as the recovery device of FIG. In other words, it is a useful form that can add additional absorbers and regenerators to the existing collection device, or improve the processing efficiency by using the existing two collection devices.
- Carbon dioxide can be recovered by connecting the system and another set of recovery devices so as to constitute a tributary system.
- the absorption device 10A has substantially the same configuration as the configuration in which the first absorption portion 12a and the partition member 13 are removed from the absorption device 10 in FIG. 1, and the reproduction device 20A is the reproduction device in FIG. It is comprised only by the lower part from 20 1st reproduction
- the absorbing device 10B is configured only by a portion below the first absorbing portion 12a in the absorbing device 10 of FIG. 1, and the reproducing device 20B is changed from the reproducing device 20 of FIG. 1 to the first reproducing portion 22a and the partition member 23.
- the configuration is substantially the same as the configuration without the reboiler.
- the top of the absorber 10B is connected to the lower part of the absorber 10A by a pipe 48.
- the gas G By supplying the gas G to the lower part of the absorber 10B, the gas G is supplied to the first absorber 12a and the absorber 10A of the absorber 10B.
- the gas G ′ from which carbon dioxide has been removed through the second absorber 12b is discharged from the top of the absorber 10A.
- the top of the regenerator 20A and the lower part of the regenerator 20B are connected by a pipe 49, and the recovered gas C containing carbon dioxide generated in the regenerator 20A by heating of the steam heater 25 is regenerated through the pipe 49.
- the flow paths L8 and L9 form a circulation path between the absorption device 10A and the regeneration device 20A, and the absorption liquid A2 ′ at the bottom of the absorption device 10A and the absorption liquid A2 at the bottom of the regeneration device 20A are second through the flow paths L8 and L9.
- a circulation system that circulates between the absorption unit 12b and the first regeneration unit 22a is configured.
- Pumps 16 and 28 are provided in the flow paths L8 and L9, respectively.
- the flow paths L10, L11, and L12 branch from the flow path L8 to form a branch path that connects to the flow path L8 via the absorption device 10B and the regeneration device 20B, and the flow paths L10, L11, and L12 include Pumps 17, 18 and 27 are respectively arranged.
- a part of the absorption liquid A2 ′ (semi-rich liquid) at the bottom of the absorption device 10A is supplied to the absorption device 10B through the flow path L10 branched from the flow path L8, and absorbs carbon dioxide at the first absorption section 12a. It is stored in.
- Absorbing liquid A1 (rich liquid) at the bottom of the absorber 10B is supplied to the regenerator 20B through the flow path L11, regenerated to some extent by the second regenerator 22b, and stored at the bottom. Thereafter, the semi-lean absorbing liquid A1 'is joined from the bottom of the regenerator 20B to the absorbent A2' of the flow path L8 from the flow path L12 and supplied to the first regenerator 22a of the regenerator 20A.
- a tributary system is configured.
- heat exchange between the flow path L11 and the flow path L12 is performed by the first heat exchanger 29, and in the circulation system, the flow path L8 and the flow path L9 are exchanged by the second heat exchanger 30. Heat exchange takes place between.
- the heat exchangers 41a to 41c provided on the exhaust pipe 38 through which the recovered gas C compressed by the compressor 40 sequentially performs heat exchange with the absorption liquid in the circulation path 50, the flow path L8, and the flow path L11. Are arranged as follows.
- the heat exchanger 41a a part of the absorption liquid A2 at the bottom of the regenerator 20A is heated by the recovered gas C, and then in the heat exchanger 41b, the absorption liquid (A2 ′) in the flow path L8 in the circulation system. + A1 ′) is heated on the downstream side of the second heat exchanger 30 by heat exchange with the recovered gas C. Further, in the heat exchanger 41 c, the absorbing liquid A ⁇ b> 1 in the flow path L ⁇ b> 11 in the tributary system is heated by heat exchange with the recovered gas C on the downstream side of the first heat exchanger 29.
- the heat recovery from the compressed recovered gas C in the exhaust pipe 38 is performed by the heat exchangers 41a to 41c as in the embodiment of FIG. 1, and the second liquid is absorbed from the absorbing liquid A2 and the flow path L8 at the bottom of the regenerator 20A.
- Recovery heat is supplied to each of the absorption liquid (A2 ′ + A1 ′) supplied to the first regeneration unit 22a and the absorption liquid A1 supplied from the flow path L11 to the second regeneration unit 22b.
- the heat recovery effect in the embodiment of FIG. 5 is the same as that of the embodiment of FIG. 1, and the regenerative energy required for recovering carbon dioxide is the same as in Table 1.
- the absorbing liquid is stored at the bottoms of the absorption device 10 ⁇ / b> A and the regeneration device 20 ⁇ / b> B, so that the storage capacity can serve as the tanks 14 and 24 of FIG. 1.
- the tanks 14 and 24 in FIG. 1 are not necessary.
- the conventional recovery device is used to configure the recovery device of FIG. 5, for example, the conventional recovery device is used as the tributary absorption device 10B and the regeneration device 20B, and the absorption device 10A and the regeneration device 20A are added. It is advisable to connect the flow path of the absorbing liquid and the gas distribution pipe so as to constitute a circulation system.
- the recovery device 5 of FIG. 5 is the same as the collection device 1 in FIG. 1 except for the points described above, and therefore the description thereof is omitted.
- the recovery device 5 of FIG. 5 can also be modified like the recovery device 2 of FIG. That is, the absorption liquid (A1 ′ + A2 ′) supplied to the first regeneration unit 22a through the flow path L8 is diverted before being supplied to the second heat exchanger 30, and a part of the remaining heat is supplied from the steam heater 25.
- the branch flow path and the heat exchanger are provided so as to merge with the flow path L8 on the downstream side of the second heat exchanger 30 after being heated by the first heat exchanger 30, the temperature rise of the absorption liquid introduced into the first regeneration unit 22a or the second heat
- the exchanger 30 can be reduced in size, and even if the heat exchanger 41b is omitted, it is easy to efficiently perform heat exchange from the recovered gas C.
- a heat exchanger for heating the absorption liquid A1 ′ before being merged with the flow path L8 by the residual heat from the steam heater 25 is provided, and the junction with the flow path L8 is subjected to the second heat exchange. You may change to the downstream from the container 30.
- a branch channel that branches from the channel L9 through which the absorption liquid A2 circulates from the first regeneration unit 22a to the second absorption unit 12b is provided, and the channels L12 and L11 are sequentially heated. It changes so that it may replace
- the modification in FIG. 2 and the modification in FIG. 4 may be used in combination.
- the absorption liquid A1 ′ of the flow path L12 and Heat exchange is performed to exchange heat with the absorbing liquid A1 in the flow path L11 in the downstream (low temperature side) heat exchanger, and the downstream flow path L12 of the upstream (high temperature side) heat exchanger is connected to the flow path L8.
- the second heat exchanger 30 is connected downstream.
- the absorbing liquid A1 'of the regenerator 20B is heated as it is without being cooled and supplied to the regenerator 20A, and the exhaust heat is used for the heat energy consumed in the tributary system.
- any of the three heat exchangers 41a to 41c can recover and reuse heat from the recovered gas C, and thus one or two of these can be arbitrarily omitted. It is also possible to carry out.
- the present invention is useful for reducing the amount of carbon dioxide released and its impact on the environment by using it for the treatment of carbon dioxide-containing gas discharged from facilities such as thermal power plants, steelworks, and boilers.
- the cost required for the carbon dioxide recovery process can be reduced, and a carbon dioxide recovery device that can contribute to energy saving and environmental protection can be provided.
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Abstract
Description
又、吸収液から二酸化炭素を回収する際に必要なエネルギーの削減を目的とした燃焼排ガスやプロセス排ガスの処理プロセスが、下記特許文献6或いは特許文献7に記載されている。
使用熱交換器の符号 再生エネルギーの割合
- 85.8%
41a 74.4%
41b 78.0%
41c 81.9%
41a+41b 72.3%
41a+41c 65.8%
41b+41c 74.2%
41a+41b+41c 65.3%
基本構造 100%
Claims (26)
- ガスを吸収液に接触させて前記ガスに含まれる二酸化炭素を吸収液に吸収させる吸収装置であって、第1吸収部及び第2吸収部を有し、前記ガスが前記第1吸収部を経て前記第2吸収部に供給されるように配設される前記吸収装置と、
前記吸収装置で二酸化炭素を吸収した前記吸収液を加熱し二酸化炭素を放出させて前記吸収液を再生する再生装置であって、第1再生部及び第2再生部を有し、前記第1再生部は外部加熱手段を有し、前記第2再生部は前記第1再生部から放出されるガスの熱によって加熱されるように配設される前記再生装置と、
前記第2吸収部と前記第1再生部との間で吸収液を循環させる循環系と、前記循環系を循環する吸収液の一部が前記第2吸収部から前記第1吸収部及び前記第2再生部を順次経由して第1再生部に向かうように前記循環系から分岐する支流系とを有する循環機構と、
前記再生装置から排出される水蒸気及び二酸化炭素を含んだ回収ガスをそのまま圧縮する圧縮器と、
前記圧縮器によって圧縮された前記回収ガスの熱を回収して前記再生装置へ供給する熱回収システムと
を有する二酸化炭素の回収装置。 - 更に、前記熱回収システムによって熱を回収した回収ガスから凝縮する水を分離する気液分離器と、前記循環系において前記第1再生部から前記第2吸収部へ還流する吸収液に、前記気液分離器において分離した水を供給する水供給路とを有する請求項1記載の二酸化炭素の回収装置。
- 前記第2再生部は外部加熱手段を有さず、前記支流系において前記第2再生部へ供給される吸収液の温度は、前記循環系において前記第1再生部へ供給される吸収液の温度より低い請求項1又は2に記載の二酸化炭素の回収装置。
- 前記支流系は、前記循環系から分岐して前記第2吸収部から前記第1吸収部へ吸収液を供給する第1流路と、前記第1吸収部から前記第2再生部へ吸収液を供給する第2流路と、第2再生部から前記循環系へ合流する第3流路とを有し、
前記支流系の第1流路は、第1吸収部へ供給する吸収液を冷却する冷却器を有する請求項1~3の何れか1項に記載の二酸化炭素の回収装置。 - 前記循環系は、前記第2吸収部から前記第1再生部へ吸収液を供給する供給路と、前記第1再生部から前記第2吸収部へ吸収液を還流する還流路とを有し、前記循環機構は、第1熱交換器及び第2熱交換器を有し、前記第1熱交換器は、前記支流系における前記第2流路と前記第3流路との間で熱交換を行い、前記第2熱交換器は、前記循環系における前記供給路と前記還流路との間で熱交換を行うように各々配置される請求項4に記載の二酸化炭素の回収装置。
- 前記循環系における前記供給路の吸収液は、前記第2熱交換器より上流側で、前記支流系の第3流路の吸収液と合流するように、前記循環系と前記支流系とが接続される請求項5に記載の二酸化炭素の回収装置。
- 前記循環系は、前記第2吸収部から前記第1再生部へ供給される吸収液を前記第2熱交換器の上流側で貯留するタンクを前記供給路上に有し、前記タンクにおいて前記供給路の吸収液と前記支流系の第3流路の吸収液が合流するように前記循環系と前記支流系とが接続される請求項6に記載の二酸化炭素の回収装置。
- 前記循環系は、前記第2吸収部から前記第1再生部へ吸収液を供給する供給路と、前記第1再生部から前記第2吸収部へ吸収液を還流するための分岐した第1還流路及び第2還流路とを有し、前記循環機構は、前記循環系の前記第1還流路と前記支流系の前記第3流路との間で熱交換を行う第1熱交換器と、前記循環系において前記供給路と前記第2還流路との間で熱交換を行う第2熱交換器と、前記循環系の前記第1還流路における前記第1熱交換器より下流側で、前記第1還流路と前記支流系の前記第2流路との間の熱交換を行う第3熱交換器とを有する請求項4に記載の二酸化炭素の回収装置。
- 前記熱回収システムは、
前記支流系の前記第2流路における前記第1熱交換器と前記第2再生部との間の吸収液と、前記圧縮器によって圧縮した回収ガスとの熱交換を行う熱交換器を有し、これにより、回収ガスの熱が前記支流系の吸収液を介して前記第2再生部へ供給される請求項5~7の何れか1項に記載の二酸化炭素の回収装置。 - 前記熱回収システムは、
前記支流系の前記第2流路における前記第3熱交換器と前記第2再生部との間の吸収液と、前記圧縮器によって圧縮した回収ガスとの熱交換を行う熱交換器を有し、これにより、回収ガスの熱が前記支流系の吸収液を介して前記第2再生部へ供給される請求項8記載の二酸化炭素の回収装置。 - 前記熱回収システムは、
前記循環系の前記供給路における前記第2熱交換器と前記第1再生部との間の吸収液と、前記圧縮器によって圧縮した回収ガスとの熱交換を行う熱交換器を有し、これにより、回収ガスの熱が前記循環系の吸収液を介して前記第1再生部へ供給される請求項5~10の何れか1項に記載の二酸化炭素の回収装置。 - 前記熱回収システムは、
前記第1再生部の吸収液を再生装置外との間で循環させる循環路と、
前記循環路の吸収液と前記圧縮器によって圧縮した回収ガスとの熱交換を行う熱交換器と
を有し、これにより、回収ガスの熱が前記循環路の吸収液を介して前記第1再生部へ供給される請求項1~11の何れか1項に記載の二酸化炭素の回収装置。 - 前記循環系は、更に、前記第2吸収部から前記第1再生部へ供給される吸収液の一部を、前記再生装置の外部加熱手段における余熱を利用して加熱するための流路及び熱交換器を有する請求項1~12の何れか1項に記載の二酸化炭素の回収装置。
- 前記吸収装置は、前記第1吸収部及び前記第2吸収部が各々分配される2つの独立した塔を有し、前記再生装置は、第1再生部及び第2再生部が各々分配される2つの独立した塔を有する請求項1~13の何れか1項に記載の二酸化炭素の回収装置。
- ガスを吸収液に接触させてガスに含まれる二酸化炭素を吸収液に吸収させる吸収処理であって、第1吸収工程及び第2吸収工程を有し、ガスは前記第1吸収工程を経て前記第2吸収工程に供給される前記吸収処理と、
前記吸収処理で二酸化炭素を吸収した吸収液を加熱し二酸化炭素を放出させて吸収液を再生する再生処理であって、第1再生工程及び第2再生工程を有し、前記第1再生工程では外部加熱手段を利用して加熱し、前記第2再生工程は前記第1再生工程において放出されるガスの熱によって加熱する前記再生処理と、
前記第2吸収工程と前記第1再生工程との間で吸収液を循環させる循環工程と、前記循環工程で循環する前記吸収液の一部を、前記第2吸収工程から前記第1吸収工程及び前記第2再生工程を順次経由して前記第1再生工程に向かうように分流する支流工程とを有する循環処理と、
前記再生処理から排出される水蒸気及び二酸化炭素を含んだ回収ガスをそのまま圧縮する圧縮工程と、
前記圧縮工程によって圧縮された回収ガスの熱を回収して前記再生処理へ供給する熱回収工程と
を有する二酸化炭素の回収方法。 - 更に、前記熱回収工程によって熱を回収した回収ガスから凝縮する水を分離する分離工程と、
前記循環工程において前記第1再生工程から前記第2吸収工程へ還流する吸収液に、前記分離工程において分離した水を供給する水供給工程と
を有する請求項15に記載の二酸化炭素の回収方法。 - 前記第2再生工程は外部加熱手段を用いず、前記支流工程の吸収液が前記第2再生工程へ供給される際の温度は、前記循環工程で循環する吸収液が前記第1再生工程へ供給される際の温度より低い請求項15又は16に記載の二酸化炭素の回収方法。
- 前記支流工程は、前記第2吸収工程から前記第1吸収工程へ吸収液を供給する第1工程と、前記第1吸収工程から前記第2再生工程へ吸収液を供給する第2工程と、第2再生工程から前記循環工程へ供給する第3工程とを有し、
前記支流工程の第1工程は、第1吸収工程へ供給する吸収液を冷却する冷却工程を有する請求項15~17の何れか1項に記載の二酸化炭素の回収方法。 - 前記循環工程は、前記第2吸収工程から前記第1再生工程へ吸収液を供給する供給工程と、前記第1再生工程から前記第2吸収工程へ吸収液を還流する還流工程とを有し、前記循環処理は、更に、前記支流工程における前記第2工程の吸収液と前記第3工程の吸収液との熱交換を行う第1熱交換工程と、前記循環工程における前記供給工程の吸収液と前記還流工程の吸収液との熱交換を行う第2熱交換工程とを有する請求項18に記載の二酸化炭素の回収方法。
- 前記循環処理において、前記供給工程の吸収液は、前記第2熱交換工程の前に、前記支流工程の第3工程の吸収液と合流させる請求項19に記載の二酸化炭素の回収方法。
- 前記循環工程は、前記第2吸収工程から前記第1再生工程へ吸収液を供給する供給工程と、前記第1再生工程から前記第2吸収工程へ吸収液を還流する並行した第1還流工程及び第2還流工程を有し、
前記循環処理は、更に、第1熱交換工程、第2熱交換工程及び第3熱交換工程を有し、前記第1熱交換工程では、前記第1還流工程の吸収液と前記支流工程における前記第3工程の吸収液との熱交換を行い、前記第2熱交換工程では、前記循環工程における前記供給工程の吸収液と前記第2還流工程の吸収液との熱交換を行い、前記第3熱交換工程では、前記第1還流工程における前記第1熱交換工程の後の吸収液と前記支流工程における前記第2工程の吸収液との熱交換を行う請求項18に記載の二酸化炭素の回収方法。 - 前記熱回収工程は、
前記支流工程の前記第2工程において前記第1熱交換工程を経て前記第2再生工程へ供給される前の吸収液と、前記圧縮工程によって圧縮した回収ガスとの熱交換を行う熱交換処理を有し、これにより、回収ガスの熱が前記支流工程の吸収液を介して前記第2再生工程へ供給される請求項19又は20に記載の二酸化炭素の回収方法。 - 前記熱回収工程は、
前記支流工程の前記第2工程において前記第3熱交換工程を経て前記第2再生工程へ供給される前の吸収液と、前記圧縮工程によって圧縮した回収ガスとの熱交換を行う熱交換処理を有し、これにより、回収ガスの熱が前記支流工程の吸収液を介して前記第2再生工程へ供給される請求項21に記載の二酸化炭素の回収方法。 - 前記熱回収工程は、
前記循環工程の前記供給工程において前記第2熱交換工程を経て前記第1再生工程へ供給される前の吸収液と、前記圧縮工程によって圧縮した回収ガスとの熱交換を行う熱交換処理を有し、これにより、回収ガスの熱が前記循環工程の吸収液を介して前記第1再生工程へ供給される請求項19~23の何れか1項に記載の二酸化炭素の回収方法。 - 前記熱回収工程は、
前記第1再生工程における吸収液と、前記圧縮工程によって圧縮した回収ガスとの熱交換を行う熱交換処理を有し、これにより、回収ガスの熱が前記第1再生工程へ供給される請求項15~24の何れか1項に記載の二酸化炭素の回収方法。 - 前記循環処理は、更に、前記第2吸収工程から前記第1再生工程へ供給される吸収液の一部を、前記再生処理で用いた外部加熱手段の余熱を利用して加熱するための熱交換工程を有する請求項15~25の何れか1項に記載の二酸化炭素の回収方法。
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