JPH0139812B2 - - Google Patents
Info
- Publication number
- JPH0139812B2 JPH0139812B2 JP60089655A JP8965585A JPH0139812B2 JP H0139812 B2 JPH0139812 B2 JP H0139812B2 JP 60089655 A JP60089655 A JP 60089655A JP 8965585 A JP8965585 A JP 8965585A JP H0139812 B2 JPH0139812 B2 JP H0139812B2
- Authority
- JP
- Japan
- Prior art keywords
- line
- adsorption
- carbon dioxide
- adsorption tank
- adsorption tanks
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 238000001179 sorption measurement Methods 0.000 claims description 81
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 58
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 29
- 239000001569 carbon dioxide Substances 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 23
- 239000003507 refrigerant Substances 0.000 claims description 15
- 239000003463 adsorbent Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 12
- 238000011084 recovery Methods 0.000 description 9
- 238000003795 desorption Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、吸着剤を使用して空気中の二酸化炭
素（CO2〕を除去及び／又は回収する方法に係
り、特に宇宙ステーシヨン、潜水艦、ライフサイ
エンス実験室などの密閉空間におけるCO2の除
去、濃度コントロールに適した二酸化炭素の除去
装置に係る。Detailed Description of the Invention [Industrial Application Field] The present invention relates to a method for removing and/or recovering carbon dioxide (CO 2 ) from the air using an adsorbent, and is particularly applicable to space stations, submarines, Relates to a carbon dioxide removal device suitable for removing CO 2 and controlling concentration in closed spaces such as life science laboratories.
従来、吸着剤を使つて空気中の二酸化炭素（以
下、CO2という）を吸着し除去、回収する方法に
おいて、吸着剤を間接的に加熱して吸着された
CO2を脱着回収する場合、CO2を含む空気は、空
気フアンを介して吸着槽に入り、吸着剤でCO2が
吸着された後、熱媒により間接的に吸着槽が加熱
され除去、回収されるがCO2を吸着した吸着槽か
ら高純度のCO2を回収する場合には、初めに槽内
の空気を真空ポンプで吸引し、外部へ放出した
後、吸着槽が間接的に加熱され必要に応じて真空
を保たれてCO2を除去、回収する。その後、加熱
された吸着槽を冷媒により冷却した後、再びCO2
の吸着を開始し、吸着後再び加熱されてCO2を回
収するサイクルを繰返している。
Conventionally, in the method of adsorbing, removing, and recovering carbon dioxide (hereinafter referred to as CO2) in the air using an adsorbent, the adsorbent was indirectly heated to absorb carbon dioxide ( CO2 ).
When desorbing and recovering CO 2 , air containing CO 2 enters the adsorption tank via an air fan, and after the CO 2 is adsorbed by the adsorbent, the adsorption tank is indirectly heated by a heating medium to be removed and recovered. However, when recovering high-purity CO 2 from an adsorption tank that has adsorbed CO 2 , the air inside the tank is first sucked in with a vacuum pump and released to the outside, and then the adsorption tank is indirectly heated. If necessary, a vacuum is maintained to remove and recover CO2 . Then, after cooling the heated adsorption tank with a refrigerant, the CO 2
The cycle of CO 2 starts adsorption, and after adsorption, is heated again to recover CO 2 .
従来行なわれている空気中のCO2除去、回収ま
上記のように、吸着→加熱→回収→冷却→吸着の
サイクルを繰返しているが、吸着槽を加熱した熱
エネルギ（熱媒、冷媒）は全て排熱として系外へ
放出されており、複数の吸着槽を有する処理装置
においても上記サイクルの切換えが行なわれるの
みで、熱エネルギは全て系外に放出され熱回収は
行なわれていなかつた。
Conventionally, the removal and recovery of CO2 from the air involves repeating the cycle of adsorption → heating → recovery → cooling → adsorption, as described above, but the thermal energy (heating medium, refrigerant) used to heat the adsorption tank is All of the heat is released to the outside of the system as waste heat, and even in processing equipment having multiple adsorption tanks, the above cycle is simply switched, and all thermal energy is released to the outside of the system and no heat recovery is performed.
本発明は上記の問題点を解決するとともに宇宙
ステーシヨン等の密閉空間における生命維持系と
して好適な二酸化炭素除去装置を提供することを
目的とする。 It is an object of the present invention to solve the above-mentioned problems and to provide a carbon dioxide removal device suitable as a life support system in a closed space such as a space station.
本発明では上記問題点を解決するために、密閉
空間内の二酸化炭素を含有する空気を導入し複数
の吸着槽に弁を介して供給する導入ラインと、空
気を導入するよう導入ラインを連通しかつ内部に
設けられた熱交換器構造に接して二酸化炭素の吸
着剤が設けられている複数の吸着槽と、前記複数
の吸着槽から弁を介して連通する空気排出ライン
と、前記複数の吸着槽から弁を介して連通する二
酸化炭素処理ラインと、前記複数の吸着槽内に設
けられた熱交換器に連通し吸着槽相互間に冷熱を
輸送する回路をそれぞれ形成する冷媒ライン及び
熱媒ラインと、弁を介して冷媒ライン及び熱媒ラ
インの回路に並列にそれぞれ連通するクーラ及び
ヒータとを有する二酸化炭素の除去装置とした。
In order to solve the above problems, in the present invention, an introduction line for introducing air containing carbon dioxide in a closed space and supplying it to a plurality of adsorption tanks via valves is connected to an introduction line for introducing air. and a plurality of adsorption tanks in which a carbon dioxide adsorbent is provided in contact with a heat exchanger structure provided inside, an air discharge line communicating from the plurality of adsorption tanks via a valve, and a plurality of adsorption tanks. A carbon dioxide processing line that communicates from the tank via a valve, and a refrigerant line and a heat medium line that communicate with the heat exchanger provided in the plurality of adsorption tanks and form a circuit that transports cold heat between the adsorption tanks. The carbon dioxide removal device has a cooler and a heater that communicate in parallel with the refrigerant line and the heat medium line circuits through valves.
本発明では上記構成としたので次の作用効果を
奏する。吸着槽の加熱冷却が熱交換器を通して
行われるので特に二酸化炭素の脱着に際し他の熱
媒が混入せず二酸化炭素を高純度に保てる。二
酸化炭素処理ラインを空気排出ラインと別系統に
設けて、高純度の二酸化炭素を次工程へ移送でき
る。熱媒ラインと冷媒ラインとを１つの吸着槽
内に別系統で設けたので、加熱冷却の応答が早
く、二酸化炭素の吸脱着効率が良い。複数の吸
着槽間に冷熱を輸送する冷媒ラインと熱媒ライン
とを設けて熱媒ラインにより脱着を終了した吸着
槽から脱着を開始しようとする吸着槽に熱を移送
して加熱するとともに、冷媒ラインにより吸着を
終了した吸着槽から吸着を開始しようとする吸着
槽に冷たさを移送して冷却するので、加熱冷却の
応答が早いとともに、この過程の間はヒータやク
ーラを使わずに加熱冷却ができるのでエネルギー
消費が小さい。冷媒ラインと並列にクーラを、
熱媒ラインに並列にヒータをそれぞれ設けたの
で、クーラとヒータとがそれぞれ１個ずつで済
み、装置が軽量コンパクトとなる。吸着槽の加
熱と冷却は吸着槽ごとに順次交代で行えばよいの
で、クーラとヒータの能力を特にあげる必要がな
く、エネルギー消費が小さくてすむ。
Since the present invention has the above configuration, the following effects are achieved. Since the adsorption tank is heated and cooled through a heat exchanger, other heating mediums are not mixed in especially when carbon dioxide is desorbed, and carbon dioxide can be kept at a high purity. The carbon dioxide treatment line is installed in a separate system from the air discharge line, allowing highly purified carbon dioxide to be transferred to the next process. Since the heating medium line and the refrigerant line are provided as separate systems within one adsorption tank, the heating/cooling response is quick and the adsorption/desorption efficiency of carbon dioxide is high. A refrigerant line and a heating medium line are provided to transport cold heat between a plurality of adsorption tanks. Because the line transfers cold water from the adsorption tank that has finished adsorption to the adsorption tank that is about to start adsorption, the response to heating and cooling is quick, and during this process, heating and cooling are not required without using a heater or cooler. , so energy consumption is low. A cooler in parallel with the refrigerant line,
Since the heaters are provided in parallel with the heating medium lines, only one cooler and one heater are required, making the device lightweight and compact. Since heating and cooling of the adsorption tanks can be performed in turn for each adsorption tank, there is no need to particularly increase the capacity of the cooler and heater, and energy consumption can be reduced.
第１図〜第３図に本発明の実施例を示すが、第
１吸着槽と第２吸着槽の２槽を有する処理システ
ムを例示している。
Embodiments of the present invention are shown in FIGS. 1 to 3, which illustrate a processing system having two tanks, a first adsorption tank and a second adsorption tank.
図において、１は第１吸着槽、２は第２吸着槽
である。（以下吸着槽１、吸着槽２という）この
吸着槽１および２は、導入ライン３、および空気
排出ライン４を介して連通されており、更に、熱
媒ライン５および冷媒ライン６とも相互に連通さ
れている。 In the figure, 1 is a first adsorption tank, and 2 is a second adsorption tank. These adsorption tanks 1 and 2 (hereinafter referred to as adsorption tank 1 and adsorption tank 2) are communicated with each other via an introduction line 3 and an air discharge line 4, and are also communicated with each other with a heat medium line 5 and a refrigerant line 6. has been done.
導入ライン３には、CO2を含有する空気Ｊを吸
着槽１に導びく切換弁３−１と吸着槽２に導びく
切換弁３−２が設けられており、空気排出ライン
４には、吸着槽１，２の空気抜きを行なうための
切換弁４−１，４−２と、吸着槽１と二酸化炭素
処理ライン７を連通する連結ライン８および吸着
槽２と二酸化炭素処理ライン７を連通する連結ラ
イン９が切換弁８−１，９−１を介して設けられ
ている。 The introduction line 3 is provided with a switching valve 3-1 that guides air J containing CO 2 to the adsorption tank 1 and a switching valve 3-2 that leads it to the adsorption tank 2. Switching valves 4-1 and 4-2 for venting air from the adsorption tanks 1 and 2, a connection line 8 that communicates the adsorption tank 1 and the carbon dioxide treatment line 7, and a connection line 8 that communicates the adsorption tank 2 and the carbon dioxide treatment line 7. A connection line 9 is provided via switching valves 8-1 and 9-1.
二酸化炭素処理ライン７には、吸着槽１又は２
内の熱交換器に設けられた吸着剤で吸着され、脱
着処理で加熱されたCO2を冷却するためのクーラ
１０と必要に応じて真空引きを行なう真空ポンプ
１１と、空気抜き弁１２が設けられており、吸着
されたCO2を回収するようになつている。 The carbon dioxide treatment line 7 includes an adsorption tank 1 or 2.
A cooler 10 for cooling the CO 2 adsorbed by the adsorbent provided in the heat exchanger inside and heated in the desorption process, a vacuum pump 11 for evacuation if necessary, and an air vent valve 12 are provided. The system is designed to recover adsorbed CO2 .
吸着槽１，２におけるCO2の吸着と脱着の処理
は、第２図に示すように冷媒ライン６、熱媒ライ
ン５を介して行なわれるが、冷媒ライン６は脱着
時熱媒ライン５を介して加熱された一方の吸着槽
（例えば１）の熱を他方の吸着槽（例えば２）に
循環移動させる熱源循環ライン２１と、CO2を吸
着のため一方の吸着槽（１又は２）の冷却を行な
う冷却ライン２２，２３で構成されており、循環
ポンプ２４、クーラ２５、切換弁２６，２７，２
８，２９，３０，３１が設けられている。又、熱
媒ライン５はCO2の脱着時に一方の吸着槽（１又
は２）の加熱を行なう加熱ライン３２，３３で構
成されており、循環ポンプ３４、加熱装置（例え
ば蒸気）３５、切換弁３６，３７，３８，３９，
４０，４１が設けられている。 The adsorption and desorption of CO 2 in the adsorption tanks 1 and 2 is carried out via a refrigerant line 6 and a heating medium line 5 as shown in FIG. A heat source circulation line 21 that circulates and transfers the heat from one adsorption tank (e.g. 1) heated by water to the other adsorption tank (e.g. 2), and cooling of one adsorption tank (1 or 2) for adsorbing CO2 . It is composed of cooling lines 22 and 23 that carry out the
8, 29, 30, and 31 are provided. The heating medium line 5 is composed of heating lines 32 and 33 that heat one adsorption tank (1 or 2) during CO 2 desorption, and includes a circulation pump 34, a heating device (for example, steam) 35, and a switching valve. 36, 37, 38, 39,
40 and 41 are provided.
なお、第１図において１３は空気フアンであ
る。 In addition, in FIG. 1, 13 is an air fan.
次に第１図〜第３図にもとづき実施例の作用を
説明する。 Next, the operation of the embodiment will be explained based on FIGS. 1 to 3.
いま、CO2を含有する空気Ｊは、空気フアン１
３を介して導入ライン３から吸着槽１導びかれて
おり、吸着槽１は吸着工程、吸着槽２はCO2回収
工程にあるものとする。 Now, the air J containing CO 2 is
It is assumed that the adsorption tank 1 is led from the introduction line 3 via the inlet line 3, and the adsorption tank 1 is in the adsorption process and the adsorption tank 2 is in the CO 2 recovery process.
この時、第１図の切換弁３−１，９−１は開、
切換弁３−２，４−１，４−２，８−１は閉であ
る。 At this time, the switching valves 3-1 and 9-1 in Fig. 1 are opened.
The switching valves 3-2, 4-1, 4-2, and 8-1 are closed.
第２図の冷媒ライン６の切換弁２６〜３１は全
開、熱媒ライン５の切換弁３６，３９は閉、切換
弁３７，３８，４０，４１は開の状態にある。 In FIG. 2, the switching valves 26 to 31 of the refrigerant line 6 are fully open, the switching valves 36 and 39 of the heating medium line 5 are closed, and the switching valves 37, 38, 40, and 41 are open.
吸着槽１では、槽内に設けられた吸着剤により
空気中のCO2が吸着され、吸着槽２では、吸着剤
のCO2が加熱ライン３３の熱媒を介して加熱さ
れ、脱着が進むと切換弁９−１が開となり、連結
ライン９を経て、二酸化炭素処理ライン７にポン
プ１１を介して導入されてクーラ１０により冷却
された後、弁１２で空気抜きが行なわれCO2が回
収される。この時吸着槽１は低温槽、吸着槽２は
高温槽となつている。 In the adsorption tank 1, CO 2 in the air is adsorbed by the adsorbent provided in the tank, and in the adsorption tank 2, the CO 2 in the adsorbent is heated through the heating medium in the heating line 33, and as desorption progresses. The switching valve 9-1 is opened, and after passing through the connection line 9 and being introduced into the carbon dioxide processing line 7 via the pump 11 and being cooled by the cooler 10, air is vented through the valve 12 and CO 2 is recovered. . At this time, adsorption tank 1 is a low temperature tank, and adsorption tank 2 is a high temperature tank.
この、吸着工程、回収工程が完了すると次に吸
着槽１はCO2脱着のため加熱され、吸着槽２は
CO2吸着のため所定温度まで冷却されるが、その
前工程として、熱媒体を間接的、又は直接的（通
常は間接的）に循環させて両槽間の熱交換が行な
われる。 After the adsorption process and recovery process are completed, adsorption tank 1 is heated for CO 2 desorption, and adsorption tank 2 is
The tank is cooled to a predetermined temperature for CO 2 adsorption, but as a pre-process, a heat medium is circulated indirectly or directly (usually indirectly) to exchange heat between the two tanks.
まず、切換弁３−１，３−２，４−１，４−
２，９−１が全開、熱媒ライン５の切換弁３６〜
41全開、冷媒ライン６の切換弁３０，３１閉とな
り、熱源循環ライン２１を切換弁２６〜２９が開
となつて、循環ポンプ２４が作動し、高温状態に
ある吸着槽２の熱が低温の吸着槽１に移される。
この熱源移動は、吸着槽２が例えば100℃、吸着
槽１が例えば０℃とした場合、両槽が例えば50℃
前後のほぼ同温度になればよい。 First, the switching valves 3-1, 3-2, 4-1, 4-
2, 9-1 is fully open, switching valve 36 of heat medium line 5 ~
41 is fully opened, the switching valves 30 and 31 of the refrigerant line 6 are closed, and the switching valves 26 to 29 of the heat source circulation line 21 are opened, the circulation pump 24 is activated, and the heat in the adsorption tank 2, which is in a high temperature state, is transferred to a low temperature one. Transferred to adsorption tank 1.
This heat source movement is such that when adsorption tank 2 is set to, for example, 100°C and adsorption tank 1 is set to, for example, 0°C, both tanks are set to, for example, 50°C.
The temperature at the front and rear should be approximately the same.
両槽がほぼ同温度になると冷媒ライン６の切換
弁２６，２９が閉、切換弁２７，２８，３０，３
１が開となり（冷却ライン２３のみ作動）循環ポ
ンプ２４、クーラ２５を介して吸着槽２が吸着の
ための所定温度まで冷却される。 When both tanks reach approximately the same temperature, the switching valves 26 and 29 of the refrigerant line 6 close, and the switching valves 27, 28, 30, 3 close.
1 is opened (only the cooling line 23 is activated), and the adsorption tank 2 is cooled to a predetermined temperature for adsorption via the circulation pump 24 and cooler 25.
冷却が完了すると吸着槽２が吸着工程に入り、
吸着槽１は空気抜きが行なわれた後、加熱により
CO2回収が行なわれる。 When cooling is completed, adsorption tank 2 enters the adsorption process.
After air is removed from adsorption tank 1, it is heated to
CO 2 capture is performed.
すなわち、切換弁を所定の開閉状態にした後、
吸着槽２にはCO2を含有する空気Ｊが、空気フア
ン１３を介して導入されCO2の吸着が行なわれ、
一方、吸着槽１は、熱媒ライン５の加熱ライン３
２により加熱され、吸着済のCO2の脱着と回収が
行なわれるもので、上記操作が完了すると吸着槽
１，２の熱交換が行なわれ、吸着槽１が吸着工
程、吸着槽２が回収工程となるサイクルを繰返す
ものである。 In other words, after setting the switching valve to the predetermined open/close state,
Air J containing CO 2 is introduced into the adsorption tank 2 via an air fan 13 to adsorb CO 2 .
On the other hand, the adsorption tank 1 is connected to the heating line 3 of the heat medium line 5.
When the above operations are completed, heat exchange between adsorption tanks 1 and 2 takes place, with adsorption tank 1 performing the adsorption process and adsorption tank 2 performing the recovery process. This cycle is repeated.
なお、上記実施例における熱回収率は約50％を
相当量の熱回収が行なえることを発明者らは確認
している。 The inventors have confirmed that the heat recovery rate in the above embodiment is about 50%, which is a considerable amount of heat recovery.
又、上記実施例における切換弁の制御は、温度
検知器やタイマー等を制御器に連動させることに
より自動操縦が容易に行なえるものである。 Further, the control of the switching valve in the above embodiment can be easily performed automatically by interlocking a temperature sensor, a timer, etc. with the controller.
上記したように本発明によれば、高温槽と低温
槽を熱移動させることにより熱エネルギーの回収
が効率よく行なえ、特に宇宙空間等では貴重なエ
ネルギーを節約する上で重要な役割を果すことに
なる。
As described above, according to the present invention, thermal energy can be efficiently recovered by transferring heat between a high temperature chamber and a low temperature chamber, and this plays an important role in saving precious energy, especially in outer space. Become.
第１図は、本発明法におけるCO2の回収装置の
概略図、第２図は複数の吸着槽間の熱交換を説明
する概略図、第３図は、本発明法の処理工程を示
すチヤート図、である。
１……第１吸着槽、２……第２吸着槽、３……
導入ライン、４……空気排出ライン、５……熱媒
ライン、６……冷媒ライン、７……二酸化炭素処
理ライン、１０……クーラ、１１……真空ポン
プ、２１……循環ライン、２２，２３……冷却ラ
イン、２４……循環ポンプ、２５……クーラ、３
２，３３……加熱ライン、３４……循環ポンプ、
３５……加熱装置。
Figure 1 is a schematic diagram of a CO 2 recovery device in the method of the present invention, Figure 2 is a schematic diagram illustrating heat exchange between multiple adsorption tanks, and Figure 3 is a chart showing the processing steps of the method of the present invention. Figure. 1...First adsorption tank, 2...Second adsorption tank, 3...
Introduction line, 4... Air discharge line, 5... Heat medium line, 6... Refrigerant line, 7... Carbon dioxide processing line, 10... Cooler, 11... Vacuum pump, 21... Circulation line, 22, 23...Cooling line, 24...Circulation pump, 25...Cooler, 3
2, 33...Heating line, 34...Circulation pump,
35... Heating device.
Claims (1)
入し複数の吸着槽に弁を介して供給する導入ライ
ンと、空気を導入するよう導入ラインを連通しか
つ内部に設けられた熱交換器構造に接して二酸化
炭素の吸着剤が設けられている複数の吸着槽と、
前記複数の吸着槽から弁を介して連通する空気排
出ラインと、前記複数の吸着槽から弁を介して連
通する二酸化炭素処理ラインと、前記複数の吸着
槽内に設けられた熱交換器に連通し吸着槽相互間
に冷熱を輸送する回路をそれぞれ形成する冷媒ラ
イン及び熱媒ラインと、弁を介して冷媒ライン及
び熱媒ラインの回路に並列にそれぞれ連通するク
ーラ及びヒータとを有する二酸化炭素の除去装
置。1. An introduction line that introduces air containing carbon dioxide in a closed space and supplies it to multiple adsorption tanks via valves, and a heat exchanger structure that communicates the introduction line to introduce air and that is provided inside. a plurality of adsorption tanks in which carbon dioxide adsorbents are provided in contact with each other;
An air discharge line communicating from the plurality of adsorption tanks via valves, a carbon dioxide processing line communicating from the plurality of adsorption tanks via valves, and a heat exchanger provided in the plurality of adsorption tanks. A carbon dioxide absorbing system comprising a refrigerant line and a heating medium line each forming a circuit for transporting cold heat between the adsorption tanks, and a cooler and a heater respectively communicating in parallel with the circuit of the refrigerant line and the heating medium line via a valve. removal device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60089655A JPS61245818A (en) | 1985-04-25 | 1985-04-25 | Removal of carbon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60089655A JPS61245818A (en) | 1985-04-25 | 1985-04-25 | Removal of carbon dioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS61245818A JPS61245818A (en) | 1986-11-01 |
| JPH0139812B2 true JPH0139812B2 (en) | 1989-08-23 |
Family
ID=13976771
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60089655A Granted JPS61245818A (en) | 1985-04-25 | 1985-04-25 | Removal of carbon dioxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS61245818A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6369526A (en) * | 1986-09-10 | 1988-03-29 | Sumitomo Heavy Ind Ltd | Recovering method for regenerating heat in carbon dioxide remover by ion exchange resin |
| JP5319476B2 (en) * | 2009-09-28 | 2013-10-16 | エネルギープロダクト 株式会社 | Separation and recovery system |
| US9028592B2 (en) * | 2010-04-30 | 2015-05-12 | Peter Eisenberger | System and method for carbon dioxide capture and sequestration from relatively high concentration CO2 mixtures |
| JP5579630B2 (en) * | 2011-01-12 | 2014-08-27 | 株式会社日立製作所 | Carbon dioxide recovery system |
| JP7356885B2 (en) * | 2019-12-06 | 2023-10-05 | 株式会社豊田中央研究所 | Gas separation device and control method for gas separation device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5442840A (en) * | 1977-09-10 | 1979-04-05 | Baanaa Intaanashiyonaru Kk | Rotary dry moisture removing machine |
| JPS5551611A (en) * | 1978-10-06 | 1980-04-15 | Lucas Industries Ltd | Suspension system for car |
| JPS5738924A (en) * | 1980-08-20 | 1982-03-03 | Mitsubishi Electric Corp | Water producer |
-
1985
- 1985-04-25 JP JP60089655A patent/JPS61245818A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5442840A (en) * | 1977-09-10 | 1979-04-05 | Baanaa Intaanashiyonaru Kk | Rotary dry moisture removing machine |
| JPS5551611A (en) * | 1978-10-06 | 1980-04-15 | Lucas Industries Ltd | Suspension system for car |
| JPS5738924A (en) * | 1980-08-20 | 1982-03-03 | Mitsubishi Electric Corp | Water producer |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS61245818A (en) | 1986-11-01 |
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