JPH0397613A - Method for recovering gaseous carbon dioxide from waste combustion gas of cogeneration equipment - Google Patents
Method for recovering gaseous carbon dioxide from waste combustion gas of cogeneration equipmentInfo
- Publication number
- JPH0397613A JPH0397613A JP1234976A JP23497689A JPH0397613A JP H0397613 A JPH0397613 A JP H0397613A JP 1234976 A JP1234976 A JP 1234976A JP 23497689 A JP23497689 A JP 23497689A JP H0397613 A JPH0397613 A JP H0397613A
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- heat
- gas
- combustion gas
- waste combustion
- 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.)
- Pending
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 31
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims description 16
- 239000000567 combustion gas Substances 0.000 title abstract 3
- 239000002699 waste material Substances 0.000 title abstract 3
- 239000007789 gas Substances 0.000 claims abstract description 18
- 239000002912 waste gas Substances 0.000 claims description 12
- 238000002485 combustion reaction Methods 0.000 claims description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 5
- 238000006114 decarboxylation reaction Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 abstract description 21
- 238000011084 recovery Methods 0.000 abstract description 13
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 6
- 230000008929 regeneration Effects 0.000 abstract description 6
- 238000011069 regeneration method Methods 0.000 abstract description 6
- 230000002745 absorbent Effects 0.000 abstract description 4
- 239000002250 absorbent Substances 0.000 abstract description 4
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 abstract description 3
- 239000000446 fuel Substances 0.000 abstract description 3
- 239000003345 natural gas Substances 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 27
- 235000011089 carbon dioxide Nutrition 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、コジェネレーション設備の燃焼廃ガスから炭
酸ガスを回収する方法に関する。DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method for recovering carbon dioxide gas from combustion waste gas of a cogeneration facility.
従来技術とその問題点
近年、飲料用、冷却用などに使用される純度９９．９９
％程度の液体炭酸および固体炭酸（ドライアイス）に対
する需要の伸びは、著しい。現在、液体炭酸および固体
炭酸（以下液体炭酸をもって代表させる）の原料となる
炭酸ガスは、石油精製、アンモニア精製などのプロセス
において、従来は主に吸収式脱炭酸設備から放散されて
いた炭酸ガス（純度９７〜９９％程度）を回収すること
により、比較的安価に得られている。しかしながら、既
設の石油精製、アンモニア精製などのプラントに隣接し
て液体炭酸製造設備を新設乃至増設するには、立地的な
制約があり、また、石油精製装置の能力にも制限があっ
て、上記の需要増大に対応することが次第に困難となり
つつある。Conventional technology and its problems In recent years, purity of 99.99 is used for beverages, cooling, etc.
The growth in demand for liquid carbonic acid and solid carbonic acid (dry ice) on the order of % is remarkable. Currently, carbon dioxide, which is the raw material for liquid carbonic acid and solid carbonic acid (hereinafter referred to as liquid carbonic acid), is produced in processes such as petroleum refining and ammonia refining. It is obtained at a relatively low cost by recovering the purity (about 97-99% purity). However, there are locational constraints in constructing or expanding liquid carbon dioxide manufacturing equipment adjacent to existing oil refining, ammonia refining, etc. plants, and there are also limitations on the capacity of the oil refining equipment, which are mentioned above. It is becoming increasingly difficult to meet the increasing demand for
また、ボイラーなどの燃焼廃ガス（炭酸ガス濃度１０％
程度）から化学吸収式脱炭酸設備（吸収液として通常モ
ノエタノールアミン液、熱炭酸カリウム溶液などが使用
される）、吸着分離法であるプレッシャースイングアド
ソープション（ＰＳＡ）法、テンペラチャースイングア
ドソープション（Ｔ Ｓ Ａ）法などにより炭酸ガスを
分離し、これから液体炭酸ガスを製造することも考えら
れるが、これらの場合には、高い設備費および低い回収
効率のために製造コストが著しく高くなり、実用的では
ない。また、燃焼廃ガス中の酸素、ＳＯｘ，ＮＯｘなど
の除去が不十分であり、特にＳＯｘおよびＮＯｘは、液
体炭酸中に混入する危険性もある。In addition, combustion waste gas from boilers (carbon dioxide concentration 10%)
from chemical absorption decarboxylation equipment (usually monoethanolamine solution, hot potassium carbonate solution, etc. are used as the absorption liquid), pressure swing adsorption (PSA) method, which is an adsorption separation method, and temperature swing adsorption. It is also possible to separate carbon dioxide gas using the TSA method and produce liquid carbon dioxide gas from it, but in these cases, the production costs would be extremely high due to high equipment costs and low recovery efficiency. , not practical. Furthermore, removal of oxygen, SOx, NOx, etc. from the combustion waste gas is insufficient, and there is a danger that SOx and NOx in particular may be mixed into the liquid carbonic acid.
問題点を解決するための手段
本発明者は、上記の如き技術の現状に鑑みて、液体炭酸
製造に際しての新たな炭酸ガス源を見出すべく思索を重
ねた結果、エネルギーの高効率的利用手段として注目さ
れているコジェネレーション設備において発生する廃ガ
ス中の炭酸ガスに着目し、さらに研究を重ねて、遂に本
発明を完成するにいたった。Means for Solving the Problems In view of the current state of the technology as described above, the inventor of the present invention has repeatedly thought to find a new carbon dioxide source for producing liquid carbonic acid, and as a result, has developed a method for highly efficient use of energy. Focusing on carbon dioxide gas in the waste gas generated in cogeneration equipment, which is attracting attention, and conducting further research, the present invention was finally completed.
すなわち、本発明は、下記の炭酸ガス回収方法を提供す
るものである：
■コジェネレーション設備で得られる熱及び電気エネル
ギーを利用して、該コジェネレーション設備で発生する
燃焼廃ガスから炭酸ガスを回収する方法。That is, the present invention provides the following carbon dioxide recovery method: ■Using the heat and electrical energy obtained by the cogeneration facility, carbon dioxide is recovered from the combustion waste gas generated by the cogeneration facility. how to.
■脱炭酸後に放散されるガスから窒素を回収する上記項
のに記載の方法。(2) The method described in the above item for recovering nitrogen from the gas released after decarboxylation.
以下に添付図面を参照しつつ、本発明をより詳細に説明
する。The present invention will be explained in more detail below with reference to the accompanying drawings.
第１図において、天然ガスなどの燃料（Ｆ）を燃焼させ
るエンジン（１）は、発電機（２）を駆動し、発電を行
なう。エンジン（１）で発生した燃焼廃ガスは、熱回収
用ボイラー（３）およびクーラー（４）を経てブロワ（
５）から吸収塔（６）に入る。吸収塔（６）には、吸収
液が循環されている。吸収液としては、アルカノールア
ミン系のものが好ましい。吸収液としてモノエタノール
アミン系のものを使用する場合には、酸素と反応して熱
再生不能の塩を発生する、炭酸ガスの回収率が低い、分
離エネルギーコストが高いなどの問題を生ずるので、好
ましくない。吸収塔（６）では、燃焼廃ガスと吸収液と
が向流接触し、燃焼廃ガス中のＣＯ２が吸収液に吸収さ
れるとともに、微量のＳＯｘは、吸収液と反応して熱再
生可能な塩を形成する。吸収液の劣化防止のためには、
必要に応じて、少量の吸収液を補給する。塔頂からは、
Ｎ２を主成分とし、０２、ＮＯｘなどを含有するガスが
放出される。この放出ガスからは、常法にしたがって、
Ｎ２を収得することができる。In FIG. 1, an engine (1) that burns a fuel (F) such as natural gas drives a generator (2) to generate electricity. The combustion waste gas generated by the engine (1) passes through the heat recovery boiler (3) and cooler (4), and then passes through the blower (
5) and enters the absorption tower (6). Absorption liquid is circulated through the absorption tower (6). As the absorption liquid, an alkanolamine type absorption liquid is preferable. When using a monoethanolamine-based absorbent, there are problems such as it reacts with oxygen and generates salts that cannot be thermally regenerated, the recovery rate of carbon dioxide is low, and the separation energy cost is high. Undesirable. In the absorption tower (6), the combustion waste gas and the absorption liquid come into countercurrent contact, and the CO2 in the combustion waste gas is absorbed by the absorption liquid, and a small amount of SOx can be thermally regenerated by reacting with the absorption liquid. Forms salt. To prevent deterioration of the absorption liquid,
Add a small amount of absorbent liquid if necessary. From the top of the tower,
A gas containing N2 as a main component and 02, NOx, etc. is released. From this released gas, according to the usual method,
N2 can be obtained.
次いで、ＣＯ２分などを含む吸収液は、循環ポンプ（１
０）により熱回収熱交換器（８）を経て再生塔（７）に
送られる。再生塔（７）の頂部からは、ガス状のＣＯ２
が取り出され、これは、一次クーラー（１３） 、圧縮
機（１４） 、二次クーラー（１５）および脱湿及び脱
水機（ｔ６）を経て、例えばＬＮＧを冷却剤とする三次
クーラー（ｌ７）により液化されて、精留塔（ｌ８）で
高純度に精製され、需要に応じて、液体炭酸（Ｌ）とし
て取り出される。冷却剤としてのＬＮＧから生成する気
化天然ガスは、エンジン（１）における燃料（Ｆ）とし
て利用することができる。Next, the absorption liquid containing CO2 etc. is passed through a circulation pump (1
0) is sent to the regeneration tower (7) via the heat recovery heat exchanger (8). From the top of the regeneration tower (7), gaseous CO2
is taken out, which passes through a primary cooler (13), a compressor (14), a secondary cooler (15), and a dehumidifier and dehydrator (t6), and is then cooled by a tertiary cooler (l7) using LNG as a coolant, for example. It is liquefied, purified to high purity in a rectification column (18), and taken out as liquid carbonic acid (L) according to demand. Gasified natural gas produced from LNG as a coolant can be used as fuel (F) in the engine (1).
再生塔（７）では、ＣＯ２分などを含む吸収液が塔内を
下降し、リボイラー（１２）で発生した蒸気と向流接触
し、ＣＯ２ガスを放出するとともに、自らは再生される
。In the regeneration tower (7), the absorption liquid containing CO2 and the like descends in the tower, comes into countercurrent contact with the steam generated in the reboiler (12), releases CO2 gas, and is itself regenerated.
リボイラー（ｌ２）の熱源は、ライン（１９）から供給
される水が熱回収用ボイラー（３）で加熱されて形成さ
れる水蒸気である。再生された吸収液は、循環ポンプ（
１１）および熱回収熱交換器（８）およびクーラー（９
）を経て、吸収塔（６）に循環される。The heat source of the reboiler (12) is steam formed when water supplied from the line (19) is heated in the heat recovery boiler (3). The regenerated absorption liquid is sent to the circulation pump (
11) and heat recovery heat exchanger (8) and cooler (9)
) and then circulated to the absorption tower (6).
発明の効果 本発明によれば、下記の様な顕著な効果が達成される。Effect of the invention According to the present invention, the following remarkable effects are achieved.
コジェネレーション設備におけるエンジン排熱を有効に
利用することが出来る。すなわち、脱炭酸プロセスに必
要な熱エネルギーを外部から供給する必要はない。Engine exhaust heat in cogeneration equipment can be used effectively. That is, there is no need to externally supply the thermal energy required for the decarboxylation process.
また、必要な各種の設備で使用する電気エネルギーも、
十分に自給出来、余剰で安価な電気エネルギーは、後続
の液化炭酸製造設備などで利用され、設備投資の回収を
早めることができる。In addition, the electrical energy used in the various necessary equipment is
The surplus and inexpensive electric energy that is sufficiently self-sufficient can be used in subsequent liquefied carbon dioxide production facilities, etc., allowing for a faster return on capital investment.
炭酸ガスの回収率が高く、液体炭酸などの原料として有
用で安価な高純度の炭酸ガスが得られる。The recovery rate of carbon dioxide is high, and high-purity carbon dioxide that is useful and inexpensive as a raw material for liquid carbonic acid can be obtained.
窒素ガスの収得も可能である。It is also possible to obtain nitrogen gas.
実施例
以下に実施例を示し、本発明の特徴とするところをより
一層明確にする。EXAMPLES Examples will be shown below to further clarify the features of the present invention.
実施例１
第１図に示す設備を使用して、炭酸ガスの回収および液
体炭酸の製造を行なった。Example 1 Using the equipment shown in FIG. 1, carbon dioxide gas was recovered and liquid carbonic acid was produced.
まず、都市ガス４ １ ４ Ｎｍ３／ｈｒをガスエンジ
ン（１）において燃焼させることにより、電力１４７５
ＫＷＩ１ 、スチーム１．５トン／ｈｒおよびＣ０２含
有量約１０％の燃焼廃ガス５０００Ｎｍ３／ｈｒを生成
させた。First, by burning city gas 4 1 4 Nm3/hr in the gas engine (1), electric power 1475
KWI1 produced 1.5 tons/hr of steam and 5000 Nm3/hr of combustion waste gas with a CO2 content of about 10%.
得られた燃焼廃ガスを吸収塔（６）に送り、アルカノー
ルアミン系吸収液と接触させるとともに、Ｎ２を主成分
とするガスを塔頂から回収した。この回収ガスからは、
常法により純度９９％のＮ２４４Ｂ９Ｎｍ’ ／ｈｒを
収得することができた。The obtained combustion waste gas was sent to the absorption tower (6) and brought into contact with an alkanolamine-based absorption liquid, and a gas containing N2 as a main component was recovered from the top of the tower. From this recovered gas,
N244B9Nm'/hr with a purity of 99% could be obtained by a conventional method.
一方、上記のアルカノールアミン系吸収液を再生塔（７
）に送り、純度９９％のＣＯ２５３１Ｎｍ３／ｈｒを得
た。On the other hand, the above alkanolamine-based absorption liquid was transferred to a regeneration tower (7
) to obtain CO2531Nm3/hr with a purity of 99%.
このようにして得たＣ ０ ２ ５３１ Ｎ ｍ ３／
ｈｒを常法による液体炭酸製造装置に送り、純度９９
．９９％の液体炭酸約９５ｋｇ／ｈｒを得た。C 0 2 531 N m 3/ thus obtained
hr is sent to a liquid carbonic acid production device using a conventional method, and the purity is 99.
．． Approximately 95 kg/hr of 99% liquid carbonate was obtained.
なお、上記の脱炭酸工程で使用した電力は、８０ＫＷ１
１であり、余剰の電力は、１３９５ＫＷｌ１であった。The electricity used in the above decarboxylation process was 80KW1
1, and the surplus power was 1395KWl1.
第１図は、本発明方法による燃焼廃ガスからの炭酸ガス
回収工程とそれに引続く液体炭酸製造工程とを示すフロ
ーダイヤグラムである。
（１）・・・ガスエンジン
（２）・・・発電機
（３）・・・熱回収用ボイラー
（４）・・・クーラー
（５）・・・ブロワ
（６）・・・吸収塔
（７）・・・再生塔
（８）・・・熱回収熱交換器
（９）・・・クーラー
（１０）・・・循環ポンプ
（１１）・・・循環ポンプ
（１２）・・・リボイラー
（１３）・・・第一次クーラー
（１４）・・・圧縮機
（１５）・・・第二次クーラー
（１６）・・・脱湿脱水機
（ｌ７）・・・第三次クーラー
（１８）・・・精留塔
（以 上）FIG. 1 is a flow diagram showing the process of recovering carbon dioxide gas from combustion waste gas and the subsequent process of producing liquid carbon dioxide according to the method of the present invention. (1) Gas engine (2) Generator (3) Heat recovery boiler (4) Cooler (5) Blower (6) Absorption tower (7 )...Regeneration tower (8)...Heat recovery heat exchanger (9)...Cooler (10)...Circulation pump (11)...Circulation pump (12)...Reboiler (13) ...Primary cooler (14)...Compressor (15)...Second cooler (16)...Dehumidifier/dehydrator (l7)...Tertiary cooler (18)...・Rectification tower (and above)
Claims (2)
ネルギーを利用して、該コジェネレーション設備で発生
する燃焼廃ガスから炭酸ガスを回収する方法。(1) A method of recovering carbon dioxide gas from combustion waste gas generated by cogeneration equipment by using heat and electrical energy obtained by the cogeneration equipment.
求項（１）に記載の方法。(2) The method according to claim (1), wherein nitrogen is recovered from the gas released after decarboxylation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1234976A JPH0397613A (en) | 1989-09-11 | 1989-09-11 | Method for recovering gaseous carbon dioxide from waste combustion gas of cogeneration equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1234976A JPH0397613A (en) | 1989-09-11 | 1989-09-11 | Method for recovering gaseous carbon dioxide from waste combustion gas of cogeneration equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0397613A true JPH0397613A (en) | 1991-04-23 |
Family
ID=16979200
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1234976A Pending JPH0397613A (en) | 1989-09-11 | 1989-09-11 | Method for recovering gaseous carbon dioxide from waste combustion gas of cogeneration equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0397613A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1695756A1 (en) * | 2005-02-23 | 2006-08-30 | Mitsubishi Heavy Industries, Ltd. | Apparatus and method for CO2 recovery |
| JP2009264348A (en) * | 2008-04-30 | 2009-11-12 | Hitachi Ltd | Humid air gas turbine system |
| KR101375645B1 (en) * | 2012-06-12 | 2014-03-19 | 한국전력기술 주식회사 | CO2 Absorption Device using heat of reboiler steam condensate |
-
1989
- 1989-09-11 JP JP1234976A patent/JPH0397613A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1695756A1 (en) * | 2005-02-23 | 2006-08-30 | Mitsubishi Heavy Industries, Ltd. | Apparatus and method for CO2 recovery |
| US7485274B2 (en) | 2005-02-23 | 2009-02-03 | Mitsubishi Heavy Industries, Ltd. | Apparatus and method for CO2 recovery |
| JP2009264348A (en) * | 2008-04-30 | 2009-11-12 | Hitachi Ltd | Humid air gas turbine system |
| KR101375645B1 (en) * | 2012-06-12 | 2014-03-19 | 한국전력기술 주식회사 | CO2 Absorption Device using heat of reboiler steam condensate |
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