JPH03229611A - Method for recovering co2 from gas containing thin co2 by psa process - Google Patents
Method for recovering co2 from gas containing thin co2 by psa processInfo
- Publication number
- JPH03229611A JPH03229611A JP2024972A JP2497290A JPH03229611A JP H03229611 A JPH03229611 A JP H03229611A JP 2024972 A JP2024972 A JP 2024972A JP 2497290 A JP2497290 A JP 2497290A JP H03229611 A JPH03229611 A JP H03229611A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- adsorption
- adsorbed
- adsorbent
- tank
- 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
- 238000000034 method Methods 0.000 title claims description 30
- 238000001179 sorption measurement Methods 0.000 claims abstract description 34
- 239000003463 adsorbent Substances 0.000 claims abstract description 20
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 5
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000010457 zeolite Substances 0.000 claims abstract description 5
- 238000010926 purge Methods 0.000 abstract description 20
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 abstract 3
- 239000000567 combustion gas Substances 0.000 abstract 2
- 238000002485 combustion reaction Methods 0.000 description 10
- 238000003795 desorption Methods 0.000 description 9
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 101150096839 Fcmr gene Proteins 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 238000010792 warming Methods 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
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Carbon And Carbon Compounds (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、稀薄ＣＯ２源からプレッシャースイングアド
ソープション法（以下ＰＳＡ法という）によりＣＯ□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 CO□ from a dilute CO2 source by pressure swing adsorption (hereinafter referred to as PSA method).
従来技術とその問題点
従来からも、燃焼排ガスなどの稀薄ＣＯ２源（ＣＯ２Ｏ
２濃度８〜冗０
りＣＯ２を回収する試みがなされている。しかしながら
、この方法には、以下の様な問題点があり、未だ実用化
されるには至っていない。Conventional technology and its problems Conventionally, dilute CO2 sources such as combustion exhaust gas (CO2O
Attempts have been made to capture CO2 at concentrations 8 to 0. However, this method has the following problems and has not yet been put into practical use.
（１）吸着剤のＣＯ２吸着容量が小さいため、大量の吸
着剤を必要とする。(1) Since the adsorbent has a small CO2 adsorption capacity, a large amount of adsorbent is required.
（２）吸着容量を大きくするためには吸着圧力を高めれ
ば良いが、この場合には、原料ガス中のＣＯ２濃度がも
ともと低いので、過剰の動力が必要となる。(2) In order to increase the adsorption capacity, it is sufficient to increase the adsorption pressure, but in this case, excessive power is required because the CO2 concentration in the raw material gas is originally low.
（３）動力費を減少させるために、吸着圧力を低下させ
るとともに真空脱着を行なう場合に、吸着剤として例え
ば合成ゼオライトを使用すると、原料ガス中のＣＯ２濃
度が低いため、大量のパージ用ＣＯ２を使用する必要が
あり、非効率的なプロセスとなる。(3) When lowering the adsorption pressure and performing vacuum desorption in order to reduce power costs, for example, if synthetic zeolite is used as the adsorbent, the CO2 concentration in the raw gas is low, so a large amount of purge CO2 is required. It is an inefficient process.
（４）また、吸着容量を増大させるためには、パージ工
程後に吸着剤層温度を高めることにより脱着時の再生度
を高める昇温工程を行なう、いわゆるブレッシャーサー
マルスイングアドソーブション法（ＰＴＳＡ法）の採用
も考えられる。しかしながら、この方法は、昇温工程に
長時間を要するので、サイクルタイムが長くなり、さら
に設置スペースの増大に伴って、イニシャルコストの増
加を招くという問題点がある。(4) In addition, in order to increase the adsorption capacity, a temperature raising process is performed after the purge process to increase the degree of regeneration during desorption by increasing the temperature of the adsorbent layer. ) may also be considered. However, this method requires a long period of time for the temperature raising process, resulting in a longer cycle time and an increase in the installation space, resulting in an increase in initial cost.
上記（１）〜（４）の様な問題点が存在するので、ＣＯ
２含有排ガスからＰＳＡ法またはＰＴＳＡ法によりＣＯ
２を回収する技術は、比較的高濃度（２５〜３０％程度
）のＣＯ２を含有する製鉄排ガス（高炉ガス）などに適
用されているのみであり、ＣＯ２濃度の低い燃焼排ガス
については実用化されるには至っていない。Since problems such as (1) to (4) above exist, CO
2-containing exhaust gas using the PSA method or PTSA method.
The technology to recover CO2 has only been applied to steelmaking exhaust gas (blast furnace gas), etc., which contains a relatively high concentration of CO2 (approximately 25 to 30%), and has not been put into practical use for combustion exhaust gas with a low CO2 concentration. It has not yet been reached.
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を背景として、燃焼
排ガスなどの稀薄ＣＯ２源から効率良く回収する方法を
見出すべく種々研究を重ねた結果、予め４０〜６０℃に
予熱しておいたＣＯ２をパージ工程で使用する場合には
、パージ用ＣＯ２の使用量を低減し得ること、また、パ
ージ終了時の吸着剤層温度を高めることができるので、
脱着時の回収製品量当たりのの動力削減と吸着剤の再生
度の向上（延いては吸着容量の増大）とが可能となるこ
とを見出した。Means for Solving the Problems Against the backdrop of the current state of technology as described above, the present inventor has conducted various studies in order to find a method for efficiently recovering CO2 from a dilute CO2 source such as combustion exhaust gas. When CO2 preheated to ℃ is used in the purge step, the amount of CO2 used for purging can be reduced, and the temperature of the adsorbent layer at the end of purging can be increased.
We have discovered that it is possible to reduce the power per unit of recovered product during desorption and improve the regeneration degree of the adsorbent (and thus increase the adsorption capacity).
すなわち、本発明は、下記のＣＯ２回収方法を提供する
ものである：
「稀薄ＣＯ２源ガスからプレッシャースイングアドソー
ブション法によりＣＯ２を回収する方法において、吸着
剤として合成セオライトを使用するとともに、４０〜６
０℃に予熱したＣＯ２により吸着ＣＯ２のパージを行な
うことを特徴とするＣＯ２を回収する方法。」
以下に図面を参照しつつ、本発明を各工程毎にさらに詳
細に説明する。That is, the present invention provides the following CO2 recovery method: "In a method of recovering CO2 from a dilute CO2 source gas by a pressure swing adsorption method, synthetic theolite is used as an adsorbent, and 6
A method for recovering CO2, characterized in that adsorbed CO2 is purged with CO2 preheated to 0°C. ” The present invention will be explained in more detail for each step with reference to the drawings.
第１図は、本発明方法の実施の一例を示すフローチャー
トである。FIG. 1 is a flowchart showing an example of implementing the method of the present invention.
１、吸着工程
まず、ボイラー（１）などのＣＯ２発生源で発生した稀
薄ＣＯ２源ガス（以下燃焼排ガスをもって代表させる）
の一部は、ライン（３）を経てパージガス予熱器（５）
で熱交換（冷却）された後、クツションタンク（７）に
収容される。次いで、クツションタンク（７）からの燃
焼排ガスは、エアフィンクーラー（９）および脱湿器（
１１）において順次冷却および脱湿され、昇圧ブロワ（
１３）で所定の吸着圧力（通常０． １ ｋｇ／ｃｌＩ
ｉ−Ｇ程度）まで昇圧された後、バルブ（１５）を経て
吸着剤（１７）を充填された第１．の吸着塔（１９）に
送入される。ここで燃焼排ガス中のＣＯ２の大部分と少
世のＮ２および０２が吸着剤に共吸着される。吸着剤と
しては、吸着能力などの観点から、合成ゼオライトが特
に好適である。1. Adsorption process First, diluted CO2 source gas generated from a CO2 source such as a boiler (1) (hereinafter referred to as combustion exhaust gas)
A part of the gas passes through the line (3) to the purge gas preheater (5).
After being subjected to heat exchange (cooling) at , it is stored in a cushion tank (7). Next, the combustion exhaust gas from the cushion tank (7) is passed through the air fin cooler (9) and the dehumidifier (
11), it is sequentially cooled and dehumidified, and then the booster blower (
13) at a predetermined adsorption pressure (usually 0.1 kg/clI
After the pressure is increased to about i-G), the first pipe is filled with adsorbent (17) through a valve (15). adsorption tower (19). Here, most of the CO2 and small amounts of N2 and 02 in the combustion exhaust gas are co-adsorbed by the adsorbent. As the adsorbent, synthetic zeolite is particularly suitable from the viewpoint of adsorption capacity.
■、加熱ＣＯ□によるパージ工程
次いで、製品タンク（３７）内の高純度ＣＯ２（通常９
９．７％程度）が、パージブロワ（２７）で昇圧（通常
０．．１ｋｇ／ｃｄ・Ｇ程度まで）され、ライン（２９
）を経てパージガス予熱器（５）に送られ、ライン（３
）を通る燃焼排ガスとの熱交換により予熱された後、バ
ルブ（３１）を経て、吸着工程を終えた第１の吸着塔（
１９）に送入される。■Purge process with heated CO□ Next, high-purity CO2 in the product tank (37) (usually 9
9.7%) is boosted by the purge blower (27) (usually to about 0.1 kg/cd・G), and the line (29
) to the purge gas preheater (5), and then to the line (3
) After being preheated by heat exchange with the combustion exhaust gas passing through the valve (31), the first adsorption tower (
19).
ここでＣＯ２分圧の差によって吸着平衡が上昇するので
、ＣＯ２がさらに吸着されて、バルクのＮ２および０２
ならびに共吸着されたＮ２および０２と置換する。置換
されたガスは、バルブ（３９）を経てオフガスとして排
出される。その結果、吸着塔（１９）内の吸着剤（１７
）は実質的にすべてＣＯ２を吸着した状態となる。Here, the adsorption equilibrium increases due to the difference in CO2 partial pressure, so more CO2 is adsorbed, and the bulk N2 and 02
and co-adsorbed N2 and 02. The displaced gas is discharged as off-gas through the valve (39). As a result, the adsorbent (17
) is in a state where substantially all CO2 is adsorbed.
パージに使用する高純度ＣＯ２の予熱は、他の排熱源に
より行なっても良いが、上記の様に燃焼排ガスとの熱交
換により行なうことが、コスト削減のために、最も好ま
しい。The high-purity CO2 used for purging may be preheated by other exhaust heat sources, but it is most preferable to preheat by exchanging heat with the combustion exhaust gas as described above in order to reduce costs.
■、真空脱着工程
次いで、吸着塔（１９）内の吸着剤（１７）に吸着され
たＣＯ２は、バルブ（３３）を経て真空ポンプ（３５）
により通常４０〜６０ト一ル程度で真空脱着され、製品
タンク（３７）に送入される。(2) Vacuum desorption process Next, the CO2 adsorbed by the adsorbent (17) in the adsorption tower (19) is transferred to the vacuum pump (35) via the valve (33).
The product is desorbed under vacuum, usually at a pressure of about 40 to 60 torr, and then sent to the product tank (37).
第１図に示す装置においては、３つの吸着塔（１９）、
（２１）および（２３）を使用するので、それぞれの吸
着塔でのサイクルを下表に示すように、順次切り替える
ことにより、装置全体として一ヒ記■〜■の工程を連続
的に行うことができる。In the apparatus shown in FIG. 1, three adsorption towers (19),
Since (21) and (23) are used, by sequentially switching the cycles in each adsorption tower as shown in the table below, it is possible to continuously perform steps ① to ① for the entire device. can.
第１の吸着塔（１９）・・・Ｉ−ＩＩ−ｍ第２の吸着塔
（２１）・・・ｍ−■−ｎ第３の吸着塔（２３）・・・
ｎ−ｍ−ｒなお、第１図においては、３つの吸着塔を使
用する装置の概要を示したか、本発明方法は、４つ以上
の吸着塔を使用しても実施することが出来る。First adsorption tower (19)...I-II-m Second adsorption tower (21)...m-■-n Third adsorption tower (23)...
Although FIG. 1 schematically shows an apparatus using three adsorption towers, the method of the present invention can also be carried out using four or more adsorption towers.
実用的には、３〜４個の吸着塔を使用する場合か最も有
利である。Practically, it is most advantageous to use 3 to 4 adsorption towers.
本発明によれば、公知のＰＳＡ法或いはＰＴＳＡ法に比
して、下記の様な顕著な効果が達成される。According to the present invention, the following remarkable effects can be achieved compared to the known PSA method or PTSA method.
（イ）パージ用ＣＯ□使用量が削減される。(a) The amount of CO□ used for purging is reduced.
（ロ）ＣＯ□パージ工程終了時の吸着剤層温度の全体的
上昇により、ＣＯ２脱着工程時の回収製品歯当たりの動
力が削減される。(b) Due to the overall increase in the temperature of the adsorbent bed at the end of the CO□ purge step, the power applied to the teeth of the recovered product during the CO2 desorption step is reduced.
（ハ）吸着剤の再生度が向上するので、ＣＯ２吸着容貴
が増大して吸着剤必要量が減少するとともに、ＣＯ２回
収率が向上する。(c) Since the degree of regeneration of the adsorbent is improved, the CO2 adsorption capacity is increased, the required amount of adsorbent is reduced, and the CO2 recovery rate is improved.
（ハ）上記（イ）乃至（ハ）の総合的な結果として、従
来実用化されていなかった稀薄ＣＯ２源からのＣＯ２回
収が可能となった。(c) As a comprehensive result of the above (a) to (c), it has become possible to recover CO2 from a dilute CO2 source, which has not been put to practical use in the past.
（ニ）したがって、本発明方法は、地球温暖化抑制のた
めに現在検討されつつあるＣＯ２の排出量規制に対処す
る手段としても、有用である。(d) Therefore, the method of the present invention is also useful as a means for dealing with CO2 emission regulations that are currently being considered in order to suppress global warming.
実施例
以下に実施例および比較例を示し、本発明の特徴とする
ところをより一層明確にする。EXAMPLES Examples and comparative examples are shown below to further clarify the features of the present invention.
実施例１
第１図に示す形式の装置を使用し、合成ゼオライト（商
標“ＭＳ１３Ｘ” トーソー（株）製）を吸着剤とし
て、燃焼排ガス（ＣＣｈ濃度１１．８％）からＣＯ２を
回収した。Example 1 Using a device of the type shown in FIG. 1, CO2 was recovered from combustion exhaust gas (CCh concentration 11.8%) using synthetic zeolite (trademark "MS13X" manufactured by Toso Corporation) as an adsorbent.
吸着工程、パージ工程および脱着工程における操作条件
並びに結果は、下記第１表に示す通りである。The operating conditions and results in the adsorption step, purge step and desorption step are shown in Table 1 below.
比較例Ｉ
ＣＯ□濃度１２．８％の燃焼排ガスを原料とし、且つパ
ージガス温度を２０℃とする以外は実施例１と同様にし
てＣＯ２を回収した。Comparative Example I CO2 was recovered in the same manner as in Example 1, except that combustion exhaust gas with a CO□ concentration of 12.8% was used as a raw material and the purge gas temperature was set to 20°C.
吸着工程、パージ工程および脱着工程における操作条件
並びに結果は、下記第１表に併せて示す通りである。The operating conditions and results in the adsorption step, purge step and desorption step are also shown in Table 1 below.
第１表
実施例１
！着！匣（’Ｃ） ２０１！圧力 （ｋ
ｇ／ｃＪＧ） ０．０８吸着時Ｓ
Ｖ （ｈ−’） ６７０ 〜７
００吸着時ＬＶ （ｃｍ／ｓｅｅ ）
９．３ 〜９．７パージ時ＳＶ （ｈ −’）
１１０ 〜１２０バージ時ＬＶ （
ｃｍ／ｓｅｅ ） １．６ 〜１．７バー
ジガス温度 （℃） ４０
脱着時圧力 （Ｔｏｒｒ）
４ ０脱着時回収率 （％）
７５．８比１着量 （ｗｔ％）
２． ７比較例１
０
０．０８
６７０〜７００
９．３〜９．７
１１０〜１２０
１．６〜１．７
０
０
６８．３
２．４
第１表に示す結果から、本発明方法の優れたＣＯ２回収
効果が明らかである。Table 1 Example 1! Arrived! Box ('C) 201! Pressure (k
g/cJG) 0.08 S at adsorption
V (h-') 670 ~7
00 adsorption LV (cm/see)
9.3 to 9.7 SV at purge (h -')
LV at 110-120 barge (
cm/see) 1.6 ~1.7 Barge gas temperature (℃) 40
Pressure during attachment/desorption (Torr)
4 Recovery rate at 0 desorption (%)
75.8 ratio (wt%)
2. 7 Comparative Example 1 0 0.08 670-700 9.3-9.7 110-120 1.6-1.7 0 0 68.3 2.4 From the results shown in Table 1, the method of the present invention was superior. The CO2 recovery effect is clear.
第１図は、本発明方法の実施の一例を示すフローチャー
トである。
（１）・・・ＣＯ２源（例えばボイラー）（５）・・・
パージガス予熱器
（７）・・・クツションタンク
（９）・・・エアフィンクーラー
（１１）・・・脱湿器
（１３）・・・昇圧ブロワ
（１５）・・・バルブ
（１７）・・・吸着剤
（１９）・・・吸着塔
（２１）・・・吸着塔
（２３）・・・吸着塔
（２７）・・・パージブロワ
（３１）・・・バルブ
（３３）・・・バルブ
（３５）・・・真空ポンプ
（３７）・・・製品タンク
（以 上）FIG. 1 is a flowchart showing an example of implementing the method of the present invention. (1)...CO2 source (e.g. boiler) (5)...
Purge gas preheater (7)...Cushion tank (9)...Air fin cooler (11)...Dehumidifier (13)...Boosting blower (15)...Valve (17)...・Adsorbent (19)...Adsorption tower (21)...Adsorption tower (23)...Adsorption tower (27)...Purge blower (31)...Valve (33)...Valve (35 )...Vacuum pump (37)...Product tank (and above)
Claims (1)
ドソープション法によりＣＯ＿２を回収する方法におい
て、吸着剤として合成ゼオライトを使用するとともに、
４０〜６０℃に予熱したＣＯ＿２により吸着ＣＯ＿２の
パージを行なうことを特徴とするＣＯ＿２を回収する方
法。(1) In the method of recovering CO_2 from dilute CO_2 source gas by pressure swing adsorption method, synthetic zeolite is used as an adsorbent, and
A method for recovering CO_2, characterized in that adsorbed CO_2 is purged with CO_2 preheated to 40 to 60°C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2024972A JPH03229611A (en) | 1990-02-02 | 1990-02-02 | Method for recovering co2 from gas containing thin co2 by psa process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2024972A JPH03229611A (en) | 1990-02-02 | 1990-02-02 | Method for recovering co2 from gas containing thin co2 by psa process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH03229611A true JPH03229611A (en) | 1991-10-11 |
Family
ID=12152887
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2024972A Pending JPH03229611A (en) | 1990-02-02 | 1990-02-02 | Method for recovering co2 from gas containing thin co2 by psa process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH03229611A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5531808A (en) * | 1994-12-23 | 1996-07-02 | The Boc Group, Inc. | Removal of carbon dioxide from gas streams |
| JP2004202393A (en) * | 2002-12-25 | 2004-07-22 | Tokyo Electric Power Co Inc:The | Carbon dioxide desorption method |
-
1990
- 1990-02-02 JP JP2024972A patent/JPH03229611A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5531808A (en) * | 1994-12-23 | 1996-07-02 | The Boc Group, Inc. | Removal of carbon dioxide from gas streams |
| JP2004202393A (en) * | 2002-12-25 | 2004-07-22 | Tokyo Electric Power Co Inc:The | Carbon dioxide desorption method |
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