WO2013088731A1 - 蒸気再圧縮設備を設置した二酸化炭素化学吸収システム - Google Patents
蒸気再圧縮設備を設置した二酸化炭素化学吸収システム Download PDFInfo
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- WO2013088731A1 WO2013088731A1 PCT/JP2012/007997 JP2012007997W WO2013088731A1 WO 2013088731 A1 WO2013088731 A1 WO 2013088731A1 JP 2012007997 W JP2012007997 W JP 2012007997W WO 2013088731 A1 WO2013088731 A1 WO 2013088731A1
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- steam
- absorption
- regeneration tower
- control device
- temperature control
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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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
- B01D2252/20478—Alkanolamines
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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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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 (CO 2 ) chemical absorption system equipped with a vapor recompression facility.
- the present invention uses the steam formed by flash evaporation of a part of the absorption liquid extracted from the regeneration tower as a heat source of the regeneration tower by recompressing the steam, and sets the temperature of the steam within a predetermined range (for example,
- the present invention relates to a carbon dioxide (CO 2 ) chemical absorption system equipped with a vapor recompression facility, which can be adjusted to 110 to 120 ° C. to suppress deterioration due to overheating of an absorbent, and an exhaust gas treatment system having the same.
- FIG. 1 An example of a power plant including a conventional CO 2 chemical absorption system is shown in FIG.
- the power plant includes a boiler 1, a denitration device 2, an air heater 3, an electrostatic precipitator 4, a wet desulfurization device 5, a press clubber 10, a CO 2 absorption tower 20, a regeneration tower 40, a reboiler 60, and the like.
- Nitrogen oxides are removed from the combustion exhaust gas discharged from the boiler 1 by burning fossil fuel such as coal by the denitration device 2. Thereafter, heat exchange is performed by the air heater 3 and the temperature is cooled to 120 to 170 ° C., for example.
- the exhaust gas that has passed through the air heater 3 is removed by the electric dust collector 4 in the exhaust gas.
- the pressure is increased by an induction fan, and the sulfur oxide (SO 2 ) is removed by the wet desulfurization apparatus 5. Since there are cases where SO 2 of several tens of ppm remains in the outlet gas of the wet desulfurization device 5, the residual SO 2 is reduced as much as possible (for example, to 10 ppm or less) with the press clubber 10 installed in front of the CO 2 chemical absorption facility. Thus, deterioration of the absorbing solution circulating in the CO 2 absorption tower 20 due to residual SO 2 is prevented.
- the CO 2 absorption tower 20 includes a packed bed 21, an absorbing liquid spray unit 22, a water washing unit 24, a water washing spray unit 25, a demister 26, a water washing water storage unit 27, a cooler 28, a water washing pump 29, and the like.
- the CO 2 contained in the exhaust gas is absorbed into the absorbing liquid by gas-liquid contact with the absorbing liquid supplied from the absorbing liquid spraying section above the CO 2 absorption tower 20 in the packed bed 21.
- the exhaust gas from which CO 2 has been removed (de-CO 2 gas) has a high temperature due to the heat generated during the absorption reaction, and is accompanied by mist.
- the mist is further removed in the demister 26 installed in the upper part of the water washing section 24, and is released as a processing gas 37 (de-CO 2 gas).
- the flush water cooled by the cooler 28 is circulated by the flush water pump 29.
- the absorption liquid (rich liquid) that has absorbed CO 2 is extracted from the liquid reservoir at the lower part of the absorption tower 20 by the absorption tower extraction pump 33, heated by the heat exchanger 34, and then sent to the regeneration tower 40.
- a rich liquid is sprayed from the spray section 42 in the regeneration tower 40 and supplied to the packed bed 41.
- steam generated in the reboiler 60 installed at the lower part of the regeneration tower 40 is supplied to the packed bed 41.
- the rich liquid and the vapor are brought into gas-liquid contact to desorb the CO 2 gas from the rich liquid.
- the mist is removed in the rinsing unit 43 and the demister 45 installed on the upper part of the rinsing unit 43, and is discharged as CO 2 gas 46 from the upper part of the regeneration tower 40.
- the CO 2 gas is cooled to about 40 ° C. by the cooler 47, separated into gas and drain water by the CO 2 separator 48, and the CO 2 gas is introduced into a CO 2 liquefaction facility (not shown),
- the drain water is supplied to the washing spray section by the drain pump 50.
- the absorption liquid from which CO 2 has been desorbed (lean liquid) is stored in the regeneration tower liquid reservoir 51 and then sent to the reboiler 60 through the reboiler liquid supply pipe 52.
- a heat transfer tube or the like is installed inside the reboiler 60, and the lean liquid is heated by the water vapor 62 supplied to the heat transfer tube through the water vapor supply pipe.
- Steam is generated inside the reboiler 60, and the steam is supplied to the regeneration tower 40 through the steam supply pipe 65.
- the steam 62 used in the reboiler 60 is recovered as water in the heat transfer tube.
- the absorption liquid stored in the liquid reservoir at the lower part of the regeneration tower 40 is supplied to the flash tank 91 through the regeneration tower liquid extraction pipe 66.
- the absorbing liquid is converted into vapor by flash evaporation.
- This steam is recompressed by the compressor 92, supplied to the regeneration tower 40, and reused as a heat source.
- the liquid phase side of the flash tank 91 is pressurized by a pump 93, the temperature is lowered by a heat exchanger 34 and a cooler 29, and then supplied to the CO 2 absorption tower 20.
- the above-described conventional technique has an advantage that the steam recompressed by the compressor 92 is supplied to the regeneration tower 40 and reused as a heat source.
- the temperature in the regeneration tower is reduced by the steam supplied to the regeneration tower.
- the absorption liquid was overheated, and the absorption liquid deteriorated and lost.
- One method of controlling the temperature in the regeneration tower 40 is a method of controlling the supply amount itself of steam generated from a steam recompression facility having a compressor or the like to the regeneration tower 40.
- the amount depends on the gas phase / liquid phase ratio of the absorbing liquid in the flash tank 91. Since the absorption liquid (liquid phase) collected at the bottom of the flash tank must be continuously supplied to the CO 2 absorption tower 20 in a constant amount, changing the gas phase / liquid phase ratio to change the amount of steam generated The material balance in the flash tank 91 collapses, the supply of the absorption liquid (liquid phase) to the CO 2 absorption tower 20 becomes unstable, or surplus steam is generated. Is hard to say.
- An object of the present invention is to use as a heat source for a regeneration tower by recompressing a vapor obtained by flash evaporation of a part of the absorbing liquid extracted from the regeneration tower, and to set the temperature of the steam within a predetermined range (for example, 110 to 110).
- An object of the present invention is to provide a carbon dioxide (CO 2 ) chemical absorption system having a vapor recompression facility and an exhaust gas treatment system having the same, which can be adjusted to 120 ° C. to suppress deterioration due to overheating of the absorbent.
- CO 2 carbon dioxide
- the present inventors have adjusted the temperature of the steam recompressed by the compressor 92 to a predetermined range by the temperature control device before supplying it to the regeneration tower 40.
- a steam recompression facility for controlling the steam
- a temperature control device for adjusting the steam compressed by the steam recompression facility to a predetermined temperature
- an exhaust gas treatment system for controlling the steam, a temperature control device for adjusting the steam compressed by the steam recompression facility to a predetermined temperature, and supplying steam adjusted to a predetermined temperature by the temperature control device to the regeneration tower
- an exhaust gas treatment system for controlling the steam, a temperature control device for adjusting the steam compressed by the steam
- the temperature control device is a cooler capable of directly spraying the refrigerant onto the vapor compressed by the vapor recompression facility to cool the vapor, or the vapor compressed by the vapor recompression facility and the refrigerant.
- absorption liquid CO 2 desorbs the absorption tower and CO 2 from the absorbent by absorption liquid for absorbing carbon dioxide (CO 2) of carbon dioxide-containing gases by absorbing solution mainly composed of an amine compound CO 2 chemical absorption facility having a regeneration tower for regeneration, a flash tank for depressurizing and evaporating the absorption liquid extracted from the lower part of the regeneration tower, and steam for compressing the steam generated in the flash tank A recompression facility; a temperature control device for adjusting the steam compressed by the steam recompression facility to a predetermined temperature; and a pipe for supplying the steam adjusted to the predetermined temperature by the temperature control device to the regeneration tower. It has a carbon dioxide chemical absorption system.
- the carbon dioxide (CO 2 ) chemical absorption system and the exhaust gas treatment system having the same having the vapor recompression facility of the present invention recompress the vapor formed by flash evaporation of a part of the absorption liquid extracted from the regeneration tower.
- CO 2 carbon dioxide
- the carbon dioxide (CO 2 ) chemical absorption system and the exhaust gas treatment system having the same having the vapor recompression facility of the present invention recompress the vapor formed by flash evaporation of a part of the absorption liquid extracted from the regeneration tower.
- it can be used as a heat source for the regeneration tower, so that the amount of water vapor supplied to the reboiler 60 can be reduced and the plant thermal efficiency can be improved.
- the temperature of the recompressed steam is adjusted to a predetermined value (for example, 110 to 120 ° C) by the temperature control device, so that deterioration of the absorbent due to overheating is suppressed without disrupting the material balance in the flash tank. be able to.
- the temperature control device In order to avoid loss due to deterioration of the absorbing solution in the regeneration tower 40, it is necessary to maintain the interior of the regeneration tower 40 (mainly at the bottom of the packed bed) at a predetermined temperature (eg, 110 to 120 ° C.). Then, it is possible to prevent the temperature in the regeneration tower 40 from rising (including locally) by controlling the steam generated in the steam recompression facility within a predetermined temperature range by the temperature control device.
- a refrigerant is used in the temperature control device.
- the refrigerant a part of the liquid circulating in the CO 2 chemical absorption facility is preferably used. Examples of the liquid circulating in the CO 2 chemical absorption facility include plant water (cooling water) and absorption liquid.
- the temperature control device is not particularly limited.
- a refrigerant is sprayed onto the steam pipe 97 using a spray nozzle or the like and directly contacted with the steam, or a refrigerant is contacted with the steam indirectly using a heat exchanger or the like.
- the thermal energy used to reduce the temperature of the steam generated in the vapor recompression facility only shifts to the absorption liquid side. Therefore, in principle, there is no loss of thermal energy due to the temperature reduction of the steam. That is, by controlling the temperature of the steam before supplying the regeneration tower 40, the amount of heat used to reduce the temperature of the steam can be efficiently returned into the regeneration tower 40 via the absorbing liquid.
- Embodiment 1 according to the present invention is shown in FIG. 1, and the present invention will be described in more detail.
- the difference between the first embodiment according to the present invention and the embodiment according to the prior art shown in FIG. 8 is that a part of the absorbing liquid extracted from the regeneration tower 40 is generated in the flash tank 91 and the compressor 92 and the like.
- the recompressed steam is used as a refrigerant for cooling, and the steam supplied to the regeneration tower 40 is controlled to an optimum temperature (for example, 110 to 120 ° C.). That is, as shown in FIG. 1, a branch pipe 98 for extracting a part of the absorbing liquid from the absorbing liquid extracting pipe 66 from the regeneration tower 40 to the flash tank 91 is installed.
- a cooler 94 a is installed in the compressed steam pipe 97.
- the absorbing liquid is sprayed using a spray nozzle 98 or the like, and is directly brought into contact with the recompressed steam to reduce the temperature of the steam.
- the amount of absorbed liquid supplied to the cooler 94a is controlled using a control valve 99 based on a temperature signal from a temperature detector 95 installed in the compressed steam pipe 97, and the temperature of the steam supplied to the regeneration tower 40 is within a predetermined range. To be inside.
- the absorbing liquid supplied from the flash tank 91 to the CO 2 absorption tower 20 by the absorbing liquid supply pump 93 needs to be supplied continuously in order to maintain the CO 2 absorption performance. For this reason, the amount of absorption liquid supplied into the flash tank 91 is made constant by the control valve 100, and the pressure in the flash tank 91 is controlled to be constant. As a result, the gas-liquid balance in the flash tank 91 is kept constant, and a certain amount of steam can be supplied to the regeneration tower and a certain amount of absorption liquid to the absorption tower.
- FIG. 7 illustrates the basic principle of the present invention with an HS diagram.
- A shows the internal conditions of the regeneration tower 40
- B shows the internal conditions of the flash tank 91
- C shows the steam conditions before supplying the regeneration tower 40.
- the inside of the regeneration tower 40 (A in FIG. 7) is slightly pressurized due to CO 2 desorption from the absorbing solution and heating through the reboiler 60.
- the process of A ⁇ B represents a decompression flash operation in the flash tank 91, where steam is generated.
- the process of B ⁇ C represents the pressurization (adiabatic compression) of the steam generated in the flash tank 91.
- a compressor 92 is used, where steam is pressurized and heated.
- the process of C ⁇ A represents a process in which steam is used as a heat source in the regeneration tower 40.
- the steam temperature is controlled and supplied to the regeneration tower 40 during the process.
- Embodiments 2 to 6 according to the present invention are shown in FIGS. 2 to 6, respectively.
- the second embodiment shown in FIG. 2 is the same as the first embodiment except that the cooler 94a installed in the compressed steam pipe 97 is changed to a heat exchanger 94b.
- the absorbent supplied to the heat exchanger 94b from the pipe 98 branched from the CO 2 extraction pipe 66 is used as a refrigerant for cooling the steam in the compressed steam pipe 97.
- steam contact indirectly through the heat exchanger tube for heat exchange.
- the amount of absorption liquid supplied to the heat exchanger 94b is controlled by using the control valve 99 based on the temperature signal from the temperature detector 95 installed in the compressed steam pipe 97, as in the control method according to the first embodiment shown in FIG.
- the temperature of the steam supplied to the regeneration tower 40 is set within a predetermined range (for example, 110 to 120 ° C.).
- the absorbing liquid used as a refrigerant for cooling the steam is returned to the regeneration tower 40.
- the use of the absorbing liquid is advantageous because the amount of heat can be returned to the regeneration tower 40 without loss.
- Embodiment 3 shown in FIG. 3 is carried out except that the absorption liquid after the flash operation in the flash tank 91 is used as a refrigerant to be supplied to the compressed steam pipe 97 instead of the absorption liquid extracted from the regeneration tower 40. It is the same as Form 1. That is, a pipe 98 branched from the pipe 96 for supplying the absorbing liquid to the CO 2 absorption tower 20 is installed, and the absorbing liquid is sprayed using a spray nozzle 98 or the like in the cooler 94a installed in the compressed steam pipe 97 and compressed. Used for cooling by direct contact with steam.
- the amount of the absorption liquid supplied to the cooler 94a is controlled using the control valve 99 based on the temperature signal from the temperature detector 95 installed in the compressed steam pipe 97, and the temperature of the steam supplied to the regeneration tower 40 is predetermined. Within the range (for example, 110 to 120 ° C.).
- using an absorbent that circulates in the CO 2 chemical absorption facility can reduce the heat quantity of all the outlets of the compressor 92 without breaking the water balance of the entire system. This is advantageous because it can be returned to the regeneration tower 40.
- the fourth embodiment shown in FIG. 4 is the same as the third embodiment except that the cooler 94a installed in the compressed steam pipe 97 is changed to a heat exchanger 94b.
- the absorption liquid supplied through the pipe 98 branched from the absorption liquid supply pipe 96 to the CO 2 absorption tower 20 is indirectly contacted with the refrigerant in the heat exchanger 94b.
- the amount of absorbed liquid supplied to the heat exchanger 94b is controlled using the control valve 99 based on the temperature signal from the temperature detector 95 installed in the compressed steam pipe 97 as described above, and supplied to the regeneration tower 40.
- the temperature of the steam is set within a predetermined range (for example, 110 to 120 ° C.).
- the absorbing liquid used as a refrigerant for cooling the steam is returned to the regeneration tower 40.
- the use of the absorbing liquid is advantageous because the amount of heat can be returned to the regeneration tower 40 without loss.
- an absorption liquid (drain water) supplied to the washing spray section of the regeneration tower is used as a refrigerant to be supplied to the compressed steam pipe 97. It is the same as Embodiment 1 except having used.
- a pipe 98 partially branched from the drain pipe is installed, and drain water is sprayed directly into the cooler 94a installed in the compressed steam pipe 97 using a spray nozzle 98 or the like. Since the drain water of the CO 2 separator 48 has a low amine concentration, when it is sprayed directly as a refrigerant to the steam pipe 97 using the spray nozzle 98 or the like, it is more easily vaporized than the absorbent extracted from the regeneration tower 40.
- Embodiment 6 shown in FIG. 6 is the same as Embodiment 5 except that the cooler 94a installed in the compressed steam pipe 97 is changed to a heat exchanger 94b.
- the absorption liquid supplied through the pipe 98 branched from the absorption liquid supply pipe 96 to the CO 2 absorption tower 20 is indirectly contacted with the refrigerant in the heat exchanger 94b.
- the amount of absorbed liquid supplied to the heat exchanger 94b is controlled using the control valve 99 based on the temperature signal from the temperature detector 95 installed in the compressed steam pipe 97 as described above, and supplied to the regeneration tower 40.
- the steam temperature is set within a predetermined range (for example, 110 to 120 ° C.).
- the absorbing liquid used as a refrigerant for cooling the steam is returned to the regeneration tower 40.
- the use of the absorbing liquid is advantageous because the amount of heat can be returned to the regeneration tower 40 without loss.
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Abstract
Description
を有する、排ガス処理システム。
〔3〕温度制御装置は、蒸気再圧縮設備で圧縮された蒸気に冷媒を直接噴霧して該蒸気を冷却することができる冷却器、または蒸気再圧縮設備で圧縮された蒸気と、冷媒との間での熱交換によって該蒸気を冷却することができる熱交換器を有する、〔1〕または〔2〕に記載の排ガス処理システム。
〔4〕CO2化学吸収設備内を循環する吸収液の一部を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
〔6〕吸収塔へ供給する吸収液の一部を冷媒として温度制御装置に供給する配管を有する、〔1〕~〔3〕のいずれかひとつに記載の排ガス処理システム。
〔7〕再生塔の水洗スプレ部に供給する吸収液(ドレン水)の一部を冷媒として温度制御装置に供給する配管を有する、〔1〕~〔3〕のいずれかひとつに記載の排ガス処理システム。
〔8〕プロセス水を冷媒として温度制御装置に供給する配管を有する、〔1〕~〔3〕のいずれかひとつに記載の排ガス処理システム。
本発明に係る実施形態1と図8に示す従来技術に係る実施形態との相違点は、再生塔40から抜き出された吸収液の一部を、フラッシュタンク91で発生させ且つ圧縮機92等で再圧縮してなる蒸気を冷やすための冷媒として使用し、再生塔40に供給される蒸気を最適な温度(例えば110~120℃)に制御するようにしたことである。すなわち、図1に示すように、再生塔40からフラッシュタンク91への吸収液抜き出し配管66から吸収液を一部抜き出すための分岐配管98を設置する。圧縮蒸気配管97に冷却器94aを設置する。該冷却器94aで吸収液をスプレノズル98等を用いて噴霧し、再圧縮された蒸気に直接接触させて該蒸気の減温に用いる。さらに冷却器94aに供給する吸収液量を圧縮蒸気配管97に設置した温度検知器95からの温度信号に基づいて制御弁99を用いて制御し再生塔40へ供給する蒸気の温度が所定の範囲内となるようにする。
2 脱硝装置
3 エアヒータ
4 乾式電気集塵装置
5 湿式脱硫装置
6 脱硫出口排ガス
10 プレスクラバー
11 吸収剤
12 液溜め
14 循環ポンプ
15 冷却器
16 スプレ部
17 冷却水
18 プレスクラバー出口ガス
20 吸収塔
21 充填層(CO2吸収部)
22 吸収液スプレ部
23 脱CO2ガス
24 水洗部
25 水洗スプレ部
26 デミスタ
27 吸収塔水洗水溜め部
28 冷却器
29 水洗水ポンプ
30 冷却水
31 冷却器
32 ボイラ水
33 吸収塔抜出しポンプ
34 熱交換器
35 再生塔液供給配管
36 水洗水抜出し配管
37 処理ガス
40 再生塔
41 充填層(CO2脱離部)
42 スプレ部
43 水洗部
44 水洗スプレ部
45 デミスタ
46 CO2ガス
47 冷却器
48 CO2分離器
49 ドレン管
50 ドレンポンプ
51 再生塔液溜め部
52 リボイラ液供給配管
53 冷却水
60 リボイラ
61 水蒸気供給配管
62 水蒸気
63 リボイラ液溜め部
64 リボイラ液抜出し配管
65 蒸気供給配管
66 再生塔液抜出し配管
91 フラッシュタンク
92 圧縮機
93 ポンプ
94a 冷却器
94b 熱交換器
95 温度検出器
96 吸収液供給配管
97 蒸気配管
98 配管
99 制御弁
100 制御弁
101 圧力計
Claims (9)
- 燃焼装置から排出される燃焼排ガス中の二酸化炭素(CO2)をアミン化合物を主成分とする吸収液によって吸収するための吸収塔およびCO2を吸収した吸収液からCO2を脱離して吸収液を再生するための再生塔を有するCO2化学吸収設備と、
再生塔の下部から抜き出される吸収液を減圧してフラッシュ蒸発させるためのフラッシュタンクと、
フラッシュタンクで発生した蒸気を圧縮するための蒸気再圧縮設備と、
蒸気再圧縮設備で圧縮された蒸気を所定温度に調節するための温度制御装置と、
温度制御装置にて所定温度に調節された蒸気を再生塔に供給するための配管と
を有する、排ガス処理システム。 - 温度制御装置は、CO2化学吸収設備内を循環する液の一部を冷媒として用いて、圧縮された蒸気の温度を調節する、請求項1に記載の排ガス処理システム。
- 温度制御装置は、蒸気再圧縮設備で圧縮された蒸気に冷媒を直接噴霧して該蒸気を冷却することができる冷却器、または蒸気再圧縮設備で圧縮された蒸気と、冷媒との間での熱交換によって該蒸気を冷却することができる熱交換器を有する、請求項1または2に記載の排ガス処理システム。
- CO2化学吸収設備内を循環する吸収液の一部を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
- 再生塔の下部から抜き出される吸収液の一部を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
- 吸収塔へ供給する吸収液の一部を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
- 再生塔の水洗スプレ部に供給する吸収液の一部を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
- プロセス水を冷媒として温度制御装置に供給する配管を有する、請求項1~3のいずれかひとつに記載の排ガス処理システム。
- 二酸化炭素含有ガス中の二酸化炭素(CO2)をアミン化合物を主成分とする吸収液によって吸収するための吸収塔およびCO2を吸収した吸収液からCO2を脱離して吸収液を再生するための再生塔を有するCO2化学吸収設備と、
再生塔の下部から抜き出される吸収液を減圧してフラッシュ蒸発させるためのフラッシュタンクと、
フラッシュタンクで発生した蒸気を圧縮するための蒸気再圧縮設備と、
蒸気再圧縮設備で圧縮された蒸気を所定温度に調節するための温度制御装置と、
温度制御装置にて所定温度に調節された蒸気を再生塔に供給するための配管と
を有する二酸化炭素化学吸収システム。
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CA 2858803 CA2858803A1 (en) | 2011-12-14 | 2012-12-14 | Carbon dioxide chemical absorption system installed with vapor recompression equipment |
EP12858675.7A EP2792399A4 (en) | 2011-12-14 | 2012-12-14 | CHEMICAL CARBON DIOXIDE ABSORPTION SYSTEM INSTALLED WITH A STEAM REPRESSION DEVICE |
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2015024398A (ja) * | 2013-07-29 | 2015-02-05 | 株式会社東芝 | 二酸化炭素分離回収システム及びその運転方法 |
KR20150015885A (ko) * | 2013-08-02 | 2015-02-11 | 한국전력공사 | 산성 가스 처리 장치 |
JP2015077581A (ja) * | 2013-10-18 | 2015-04-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
JP2015089528A (ja) * | 2013-11-05 | 2015-05-11 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
JP7062509B2 (ja) | 2017-09-22 | 2022-05-06 | チアンナン エンバイロメンタル プロテクション グループ インコーポレイティド | 炭素捕捉 |
JP7510479B2 (ja) | 2022-11-21 | 2024-07-03 | 株式会社大気社 | 回収システム |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104535723B (zh) * | 2014-12-25 | 2017-02-22 | 华能国际电力股份有限公司 | 一种变工况稠浆型二氧化碳捕集工艺测试*** |
WO2016123386A1 (en) | 2015-01-28 | 2016-08-04 | Fluor Technologies Corporation | Methods and systems for improving the energy efficiency of carbon dioxide capture |
US10376829B2 (en) | 2017-06-13 | 2019-08-13 | Fluor Technologies Corporation | Methods and systems for improving the energy efficiency of carbon dioxide capture |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011506081A (ja) * | 2007-12-13 | 2011-03-03 | アルストム テクノロジー リミテッド | 吸収剤溶液の再生システム及び方法 |
JP2011062700A (ja) * | 2011-01-04 | 2011-03-31 | Mitsubishi Heavy Ind Ltd | Co2回収装置及び方法 |
JP2012115779A (ja) * | 2010-12-01 | 2012-06-21 | Mitsubishi Heavy Ind Ltd | Co2回収システム |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6689332B1 (en) * | 1992-09-16 | 2004-02-10 | The Kansai Electric Power Co, Inc. | Process for removing carbon dioxide from combustion gases |
NO20092229L (no) | 2009-06-09 | 2010-12-10 | Aker Clean Carbon As | Reclaimer for absorbent |
JP2011115779A (ja) | 2009-10-29 | 2011-06-16 | Hymo Corp | パルプ製造排水の処理方法 |
WO2011162869A1 (en) * | 2010-06-22 | 2011-12-29 | Powerspan Corp. | Process and apparatus for capturing co2 from a gas stream with controlled water vapor content |
JP5655593B2 (ja) * | 2011-01-27 | 2015-01-21 | 株式会社Ihi | 二酸化炭素の回収方法及び回収装置 |
-
2012
- 2012-12-14 CA CA 2858803 patent/CA2858803A1/en not_active Abandoned
- 2012-12-14 US US14/364,205 patent/US9463411B2/en active Active
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- 2012-12-14 WO PCT/JP2012/007997 patent/WO2013088731A1/ja active Application Filing
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Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2011506081A (ja) * | 2007-12-13 | 2011-03-03 | アルストム テクノロジー リミテッド | 吸収剤溶液の再生システム及び方法 |
JP2012115779A (ja) * | 2010-12-01 | 2012-06-21 | Mitsubishi Heavy Ind Ltd | Co2回収システム |
JP2011062700A (ja) * | 2011-01-04 | 2011-03-31 | Mitsubishi Heavy Ind Ltd | Co2回収装置及び方法 |
Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2832420A3 (en) * | 2013-07-29 | 2015-06-10 | Kabushiki Kaisha Toshiba | Carbon dioxide separating and capturing system and method of operating same |
JP2015024398A (ja) * | 2013-07-29 | 2015-02-05 | 株式会社東芝 | 二酸化炭素分離回収システム及びその運転方法 |
US9464842B2 (en) | 2013-07-29 | 2016-10-11 | Kabushiki Kaisha Toshiba | Carbon dioxide separating and capturing system and method of operating same |
KR20150015885A (ko) * | 2013-08-02 | 2015-02-11 | 한국전력공사 | 산성 가스 처리 장치 |
KR102075463B1 (ko) * | 2013-08-02 | 2020-02-10 | 한국전력공사 | 산성 가스 처리 장치 |
WO2015056677A1 (ja) * | 2013-10-18 | 2015-04-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
US9901875B2 (en) | 2013-10-18 | 2018-02-27 | Mitsubishi Heavy Industries, Ltd. | Reclaiming device, method, and recovery unit of CO2, H2S, or both of CO2 and H2S |
JP2015077581A (ja) * | 2013-10-18 | 2015-04-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
WO2015068576A1 (ja) * | 2013-11-05 | 2015-05-14 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
JP2015089528A (ja) * | 2013-11-05 | 2015-05-11 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
US10137415B2 (en) | 2013-11-05 | 2018-11-27 | Mitsubishi Heavy Industries Engineering, Ltd. | Reclaiming device, method, and recovery unit of CO2, H2S, or both of CO2 and H2S |
JP7062509B2 (ja) | 2017-09-22 | 2022-05-06 | チアンナン エンバイロメンタル プロテクション グループ インコーポレイティド | 炭素捕捉 |
JP7510479B2 (ja) | 2022-11-21 | 2024-07-03 | 株式会社大気社 | 回収システム |
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