WO2015141158A1 - 二酸化炭素分離回収システム - Google Patents
二酸化炭素分離回収システム Download PDFInfo
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- WO2015141158A1 WO2015141158A1 PCT/JP2015/001103 JP2015001103W WO2015141158A1 WO 2015141158 A1 WO2015141158 A1 WO 2015141158A1 JP 2015001103 W JP2015001103 W JP 2015001103W WO 2015141158 A1 WO2015141158 A1 WO 2015141158A1
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0446—Means for feeding or distributing gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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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
Definitions
- the present invention relates to a carbon dioxide separation and recovery system that separates and recovers carbon dioxide in a target gas using a solid adsorbent.
- Patent Document 1 discloses a carbon dioxide separation and recovery system 100 as shown in FIG.
- the adsorbent is transferred in the order of the hopper 110, the adsorption tower 120, the regeneration tower 130, the drying tower 140, and the cooling tower 150. Further, the adsorbent is returned from the cooling tower 150 to the hopper 110 by the conveyor 160.
- the target gas is brought into contact with the adsorbent, and carbon dioxide in the target gas is adsorbed by the adsorbent.
- Water vapor is supplied to the regeneration tower 130 from the drying tower 140, and the water vapor is condensed into the adsorbent after carbon dioxide adsorption, whereby carbon dioxide is released from the adsorbent.
- the released carbon dioxide is sucked into the recovery pump 170 through the carbon dioxide recovery path 135, compressed by the recovery pump 170, and then stored in the carbon dioxide holder 180.
- the drying tower 140 evaporates the condensed water adhering to the adsorbent by indirect heating.
- the water vapor derived from the evaporation of the condensed water is supplied to the regeneration tower 130 as water vapor for regeneration.
- the drying tower 140 is supplied with saturated water vapor (eg, 60 ° C.) having a negative pressure (about 20 kPa in absolute pressure) as a heat medium.
- the drying tower 140 and the regeneration tower 130 are constituted by continuous tanks, the inside of the drying tower 140 and the regeneration tower 130 has a pressure (for example, about 20 kPa) at which condensed water can be evaporated by the heat medium by suction of the recovery pump 170. ) Is adjusted. Therefore, a differential pressure holding device (for example, a lock hopper) for maintaining a pressure difference with respect to the atmospheric pressure is provided between the adsorption tower 120 and the regeneration tower 130 and between the drying tower 140 and the cooling tower 150.
- a differential pressure holding device for example, a lock hopper
- the reason why the negative pressure saturated steam is used as a drying heat medium in the carbon dioxide separation and recovery system 100 shown in FIG. 3 is that the adsorbent is used with a small amount of energy (for example, waste heat of less than 100 ° C. from various facilities). This is to generate steam for regeneration.
- a differential pressure holding device is required as described above.
- the present invention provides a carbon dioxide separation and recovery system that can regenerate an adsorbent using low-temperature (less than 100 ° C.) and negative-pressure steam that can be generated with less energy and that does not require a differential pressure holding device. For the purpose.
- a carbon dioxide separation and recovery system is a carbon dioxide separation and recovery system that separates and recovers carbon dioxide in a target gas using a solid adsorbent, and the target gas is From the compressor, an adsorption tower for contacting the adsorbent and adsorbing the carbon dioxide in the target gas to the adsorbent and discharging the target gas from which carbon dioxide has been removed, a compressor for compressing carbon dioxide, and the compressor
- the ejected carbon dioxide is expanded while sucking negative-pressure water vapor to generate atmospheric pressure wet gas, and the wet gas flowing out from the ejector is brought into contact with the adsorbent after carbon dioxide adsorption.
- the carbon dioxide is released from the adsorbent, the regeneration tower for discharging the released carbon dioxide, and the adsorbent after contact with the wet gas are dried.
- drying tower characterized in that it comprises a.
- normal pressure wet gas refers to a wet gas having a pressure substantially equal to the atmospheric pressure (for example, a pressure within a range of ⁇ 5% from the atmospheric pressure).
- a differential pressure maintaining device for atmospheric pressure is not necessary.
- the wet gas is generated by the ejector. Since the ejector sucks negative-pressure water vapor, it is possible to generate wet gas for adsorbent regeneration using low-temperature, negative-pressure water vapor that can be generated with less energy.
- the high-temperature carbon dioxide compressed by the compressor is mixed with the water vapor, so that a wet gas of 100 ° C. or higher can be easily generated. it can.
- components other than water vapor in the wet gas are carbon dioxide, high concentration carbon dioxide can be recovered from the regeneration tower.
- the carbon dioxide separation and recovery system may further include a reflux path that guides a part of the carbon dioxide discharged from the regeneration tower to the compressor. According to this configuration, waste heat from the regeneration tower can be rationally used for generating wet gas.
- FIG. 1 is a schematic configuration diagram of a carbon dioxide separation and recovery system according to a first embodiment of the present invention. It is a schematic block diagram of the carbon dioxide separation-and-recovery system which concerns on 2nd Embodiment of this invention. It is a schematic block diagram of the conventional carbon dioxide separation and recovery system.
- the carbon dioxide separation and recovery system of the present invention separates and recovers carbon dioxide in the target gas using a solid adsorbent.
- the target gas is, for example, combustion exhaust gas.
- the adsorbent is, for example, a granular porous material that supports an amine compound.
- As the porous material activated carbon, activated alumina, or the like can be used.
- FIG. 1 shows a carbon dioxide separation and recovery system 1A according to the first embodiment of the present invention.
- This carbon dioxide separation and recovery system 1A is a moving bed system in which an adsorbent is transferred in the order of an adsorption tower 2, a regeneration tower 3, and a drying tower 4.
- the adsorbent is returned from the drying tower 4 to the adsorption tower 2 by an unillustrated conveyor or the like. In other words, the adsorbent is circulated through the adsorption tower 2, the regeneration tower 3 and the drying tower 4.
- the adsorption tower 2, the regeneration tower 3, and the drying tower 4 are arranged in this order from top to bottom.
- each of the adsorption tower 2, the regeneration tower 3, and the drying tower 4 is constituted by a single tank.
- the transfer of the adsorbent from the adsorption tower 2 to the regeneration tower 3 and the transfer of the adsorbent from the regeneration tower 3 to the drying tower 4 are continuously performed by, for example, gravity.
- the configurations of the adsorption tower 2, the regeneration tower 3, and the drying tower 4 can be changed as appropriate.
- two or all of the adsorption tower 2, the regeneration tower 3, and the drying tower 4 may be constituted by continuous tanks.
- the adsorption tower 2, the regeneration tower 3, and the drying tower 4 are arranged in the horizontal direction independently, and the adsorbent may be transferred by the conveyor in the order of the adsorption tower 2, the regeneration tower 3, and the drying tower 4.
- the adsorption tower 2 brings the target gas into contact with the adsorbent. Specifically, a target gas supply path 21 is connected to the lower part of the adsorption tower 2, and a target gas discharge path 22 is connected to the upper part of the adsorption tower 2.
- the target gas is supplied to the adsorption tower 2 through the target gas supply path 21. Thereby, the carbon dioxide in target gas is adsorbed by the adsorbent.
- the target gas from which carbon dioxide has been removed is discharged through the target gas discharge path 22.
- the adsorbent after carbon dioxide adsorption is transferred to the regeneration tower 3.
- the temperature of the adsorbent when introduced into the adsorption tower 2 is about 40 ° C., and the temperature of the target gas supplied to the adsorption tower 2 is about 35 ° C.
- the temperature of the adsorbent is slightly increased (for example, about 60 ° C.) as the adsorbent adsorbs carbon dioxide.
- the regeneration tower 3 is for bringing the wet gas into contact with the adsorbent. Specifically, a wet gas supply path 31 is connected to the lower part of the regeneration tower 3, and a carbon dioxide recovery path 32 is connected to the upper part of the regeneration tower 3.
- the regeneration tower 3 is supplied with a wet gas of 100 ° C. or higher at normal pressure through a wet gas supply path 31.
- the wet gas is a mixed gas of carbon dioxide and water vapor.
- water vapor in the wet gas is condensed into the adsorbent, and carbon dioxide is released from the adsorbent.
- the amount of water vapor in the wet gas is such that almost all of the water vapor in the wet gas is condensed into the adsorbent.
- Carbon dioxide released from the adsorbent and carbon dioxide in the wet gas are discharged through the carbon dioxide recovery path 32.
- the concentration of carbon dioxide discharged through the carbon dioxide recovery path 32 is almost 100%.
- the adsorbent with the condensed water attached is transferred to the drying tower 4.
- the temperature of the wet gas supplied to the regeneration tower 3 is 100 ° C.
- the temperature of the adsorbent rises to about 100 ° C. due to contact between the adsorbent and the wet gas and condensation of water vapor in the wet gas onto the adsorbent. Carbon dioxide is released from the adsorbent by sensible heat and condensation heat applied to the adsorbent.
- the drying tower 4 is for drying the adsorbent after contact with the wet gas.
- the adsorbent is dried by direct heating in which a drying gas is brought into contact with the adsorbent.
- drying of the adsorbent may be performed by indirect heating in which a heat medium is passed through a pipe passed through the drying tower 4.
- the heat medium for indirect heating carbon dioxide discharged from the regeneration tower 3, carbon dioxide compressed by the compressor 51 described later, wet gas before being supplied to the regeneration tower 3, or the like may be used. .
- a drying gas supply path 41 is connected to the lower part of the drying tower 4, and a drying gas discharge path 42 is connected to the upper part of the drying tower 4.
- a drying gas is supplied to the drying tower 4 through a drying gas supply path 41.
- the condensed water adhering to the adsorbent is evaporated.
- the water vapor derived from the evaporation of the condensed water is discharged through the drying gas discharge path 42 together with the drying gas.
- the adsorbent after drying is returned to the adsorption tower 2.
- the temperature of the drying gas supplied to the drying tower 4 is about 80 ° C.
- the temperature of the adsorbent gradually decreases to the wet bulb temperature of the drying gas due to evaporation of the condensed water adhering to the adsorbent. Thereafter, the temperature of the adsorbent is maintained at the wet bulb temperature of the drying gas during the evaporation of the condensed water.
- the above “adsorbent after drying” is an adsorbent immediately before the condensed water completely evaporates, that is, an adsorbent maintained at a low temperature.
- a cooling tower may be provided between the drying tower 4 and the adsorption tower 2. .
- the upstream end of the above-described wet gas supply path 31 is connected to the ejector 53. Further, the ejector 53 is connected to the compressor 51 by a relay path 52. Further, the reflux path 6 branched from the carbon dioxide recovery path 32 is connected to the compressor 51.
- the reflux path 6 guides a part of the carbon dioxide discharged from the regeneration tower 3 to the compressor 51.
- the compressor 51 compresses and discharges the carbon dioxide. Carbon dioxide discharged from the compressor 51 is guided to the ejector 53 through the relay path 52.
- the ejector 53 is connected to a water vapor supply source by a water vapor supply path 54.
- the steam supply source is, for example, a turbine or a boiler that discharges negative-pressure steam.
- the water vapor supply source may be a sealed container that stores water.
- the ejector 53 expands the compressed carbon dioxide while sucking negative-pressure steam (saturated steam or superheated steam). Thereby, the above-mentioned normal-pressure wet gas is generated.
- the wet gas flowing out from the ejector 53 is guided to the regeneration tower 3 by the wet gas supply path 31.
- carbon dioxide discharged from the compressor 51 has a pressure of about 410 kPa and a temperature of about 265 ° C., and the water vapor sucked into the ejector 53 is saturated water vapor (about 40 ° C.) of about 7 kPa.
- the wet gas at normal pressure is supplied to the regeneration tower 3, a differential pressure maintaining device for atmospheric pressure is unnecessary. Moreover, the wet gas is generated by the ejector 53. Since the ejector 53 sucks negative-pressure water vapor, it is possible to generate wet gas for adsorbent regeneration using low-temperature, negative-pressure water vapor that can be generated with less energy. For example, when the ejector 53 is connected to an airtight container that stores water, wet gas can be generated only by the power of the compressor 51.
- the high-temperature carbon dioxide compressed by the compressor 51 is mixed with the water vapor, so that a wet gas of 100 ° C. or higher is easily generated. be able to.
- the components other than water vapor in the wet gas are carbon dioxide, a high concentration of carbon dioxide can be recovered from the regeneration tower 3.
- the configurations of the adsorption tower 2, the regeneration tower 3, and the drying tower 4 can be changed as appropriate.
- the adsorption tower 2 may be arrange
- the lower part of one tank may be the adsorption tower 2 and the upper part may be the drying tower 4.
- the target gas supply path 21 is connected to the lower part of the tank and the target gas discharge path 22 is connected to the upper part of the tank, the adsorption with the condensed water attached using the target gas after carbon dioxide removal.
- the material can be dried.
- a single tank 7 filled with an adsorbent functions as an adsorption tower 2, a regeneration tower 3, and a drying tower 4 for each adsorption process, regeneration process, and drying process. It is a layer system.
- two tanks 7 are provided so that continuous processing is possible.
- the number of tanks 7 may be three or more. Or when performing an intermittent process, the tank 7 may be only one.
- one tank 7 is referred to as a first tank 7A, and the other tank 7 is referred to as a second tank 7B.
- a first common supply path 71, a first common discharge path 72, a first wet gas supply path 73, and a first carbon dioxide recovery path 74 are connected to the first tank 7A.
- a second common supply path 75, a second common discharge path 76, a second wet gas supply path 77, and a second carbon dioxide recovery path 78 are connected to the second tank 7B.
- Each of the flow paths 71 to 78 is provided with an open / close valve.
- These supply passages 81 and 82 are also provided with on-off valves, respectively. That is, either the target gas or the drying gas can be selectively passed through each of the first common supply path 71 and the second common supply path 75.
- the upstream portion of the reflux path 6 is branched into two lines, and these lines are downstream of the on-off valves in the first carbon dioxide recovery path 74 and the second carbon dioxide recovery path 78. It is connected to the side part. That is, the carbon dioxide led to the compressor 51 by the reflux path 6 can be switched between the carbon dioxide discharged from the first tank 7A and the carbon dioxide discharged from the second tank 7B.
- the adsorbent can be regenerated in one tank 7 and the carbon dioxide can be adsorbed by the adsorbent and dried by the other tank. Even in this configuration, the compressor 51 and the ejector 53 can provide the same effects as those of the first embodiment.
- the reflux path 6 can be omitted.
- the compressor 51 may be connected to a pressure vessel filled with carbon dioxide.
- the reflux path 6 is provided as in the first and second embodiments, the waste heat from the regeneration tower 3 can be rationally used for generating wet gas.
- the present invention is useful, for example, when treating combustion exhaust gas.
Abstract
Description
図1に、本発明の第1実施形態に係る二酸化炭素分離回収システム1Aを示す。この二酸化炭素分離回収システム1Aは、吸着材が、吸着塔2、再生塔3、乾燥塔4の順に移送される移動層方式のシステムである。吸着材は、図略のコンベヤなどにより乾燥塔4から吸着塔2へ戻される。換言すれば、吸着材は、吸着塔2、再生塔3および乾燥塔4を循環させられる。
上述したように、吸着塔2、再生塔3および乾燥塔4の構成は適宜変更可能である。例えば、吸着塔2が乾燥塔4の下方に配置され、それらが連続したタンクで構成されていてもよい。換言すれば、1つのタンクの下部が吸着塔2、上部が乾燥塔4となっていてもよい。この場合には、そのタンクの下部に対象ガス供給路21を接続し、タンクの上部に対象ガス排出路22を接続すれば、二酸化炭素除去後の対象ガスを利用して凝縮水が付着した吸着材を乾燥させることができる。
次に、図2を参照して本発明の第2実施形態に係る二酸化炭素分離回収システム1Bを説明する。なお、本実施形態において、第1実施形態と同一構成要素には同一符号を付し、重複した説明は省略する。
第1および第2実施形態では、還流路6によって再生塔3(第2実施形態ではどちらかのタンク7)から排出される二酸化炭素の一部が圧縮機51へ導かれていた。しかしながら、還流路6は省略可能である。例えば、圧縮機51は、二酸化炭素が充填された圧力容器に接続されていてもよい。ただし、第1および第2実施形態のように還流路6が設けられていれば、再生塔3からの廃熱をウエットガスの生成に合理的に利用することができる。
2 吸着塔
3 再生塔
4 乾燥塔
51 圧縮機
53 エジェクタ
6 還流路
Claims (2)
- 固体の吸着材を用いて対象ガス中の二酸化炭素を分離および回収する二酸化炭素分離回収システムであって、
前記対象ガスを前記吸着材に接触させて前記吸着材に前記対象ガス中の二酸化炭素を吸着させ、二酸化炭素が除去された前記対象ガスを排出する吸着塔と、
二酸化炭素を圧縮する圧縮機と、
前記圧縮機から吐出された二酸化炭素を、負圧の水蒸気を吸引しながら膨張させることによって常圧のウエットガスを生成するエジェクタと、
前記エジェクタから流出する前記ウエットガスを二酸化炭素吸着後の前記吸着材に接触させて前記吸着材から二酸化炭素を放出させ、放出された二酸化炭素を排出する再生塔と、
前記ウエットガスと接触後の前記吸着材を乾燥させる乾燥塔と、
を備える、二酸化炭素分離回収システム。 - 前記再生塔から排出される二酸化炭素の一部を前記圧縮機へ導く還流路をさらに備える、請求項1に記載の二酸化炭素分離回収システム。
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US15/127,592 US10010826B2 (en) | 2014-03-20 | 2015-03-03 | Carbon dioxide separation and recovery system |
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US11254028B2 (en) | 2019-05-20 | 2022-02-22 | Saudi Arabian Oil Company | Systems and processes for accelerated carbonation curing of pre-cast cementitious structures |
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US20170136404A1 (en) | 2017-05-18 |
JP2015181964A (ja) | 2015-10-22 |
CN105916568A (zh) | 2016-08-31 |
CN105916568B (zh) | 2018-05-11 |
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JP6302309B2 (ja) | 2018-03-28 |
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