JPH0699015A - Pressure swing adsorption method - Google Patents
Pressure swing adsorption methodInfo
- Publication number
- JPH0699015A JPH0699015A JP4253283A JP25328392A JPH0699015A JP H0699015 A JPH0699015 A JP H0699015A JP 4253283 A JP4253283 A JP 4253283A JP 25328392 A JP25328392 A JP 25328392A JP H0699015 A JPH0699015 A JP H0699015A
- Authority
- JP
- Japan
- Prior art keywords
- concentration
- pressure swing
- gas
- adsorption
- raw material
- 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
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、例えば、発酵プロセス
やタバコプロセス等の排ガス中に含まれるＣＯ2 のよう
に操業に伴う含有濃度の変動が多い原料ガスから、ＣＯ
2 等の特定成分を回収する圧力スイング吸着装置の操業
方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention is applied to the production of CO 2 from a raw material gas whose concentration concentration varies with the operation, such as CO 2 contained in exhaust gas from fermentation processes, tobacco processes, etc.
The present invention relates to a method of operating a pressure swing adsorption device that recovers specific components such as 2 .
【０００２】[0002]
【従来技術】例えば、複数の吸着塔を配置して、それぞ
れの吸着塔に昇圧工程、吸着工程、洗浄工程、脱着工程
を交互にずらせて操作して、ボイラ等の燃焼排ガスから
ＣＯ、ＣＯ2 等の特定ガスを回収する方法は、例えば、
特開昭６３−７７５１５号公報、特開平１−２０３０１
８号公報に記載されているように、圧力スイング吸着法
（ＰＳＡ法）として公知である。2. Description of the Related Art For example, by arranging a plurality of adsorption towers and operating the pressure rising step, the adsorption step, the washing step, and the desorption step alternately in each of the adsorption towers, CO and CO 2 from combustion exhaust gas from a boiler or the like is operated. The method of recovering a specific gas such as
JP-A-63-77515, JP-A-1-20301
As described in JP-A-8, it is known as a pressure swing adsorption method (PSA method).
【０００３】この圧力スイング吸着法は、比較的小規模
の設備で、排ガス（原料ガス）中の回収対象であるＣ
Ｏ、ＣＯ2 等の特定ガスの含有量が少ない場合でも連続
的に回収できるという特長がある。This pressure swing adsorption method is a relatively small-scale facility, and is a target of recovery of C in exhaust gas (raw material gas).
It has a feature that it can be continuously recovered even when the content of a specific gas such as O or CO 2 is small.
【０００４】また、従来の圧力スイング吸着法が適用さ
れている原料ガス、例えば、ボイラ等の燃焼排ガス中の
特定ガスの濃度は、操業に伴って余り変動がなく、その
ため要求される回収ガスの製品濃度に合わせて吸着剤の
選定及びタイムサイクルの時間を一定に設定している。Further, the concentration of a specific gas in a raw material gas to which the conventional pressure swing adsorption method is applied, for example, a combustion exhaust gas of a boiler or the like does not change much with the operation, and therefore, the required recovery gas is The adsorbent is selected and the time cycle time is set to a constant value according to the product concentration.
【０００５】しかしながら、前記従来の圧力スイング吸
着法は、吸着・回収される製品のＣＯ2 純度確保のため
には、排ガス発生設備の操業に伴う排ガス変動幅の最も
低い含有ＣＯ2 濃度条件に合わせた操業しかできず、例
えば、図５に示すとおり、発酵プロセスやタバコプロセ
ス等から排出されるガスのように、ＣＯ2 濃度の変動が
大きい原料ガスからのＣＯ2 吸着・回収に際して、ＣＯ
2 濃度が９９％以上の場合のみを原料ガスとしてＣＯ2
液化設備により回収しているのが現状である。However, in order to secure the CO 2 purity of the product to be adsorbed / collected, the above-mentioned conventional pressure swing adsorption method is adjusted to the contained CO 2 concentration condition in which the exhaust gas fluctuation range accompanying the operation of the exhaust gas generation equipment is the lowest. However, as shown in FIG. 5, for example, as shown in FIG. 5, when CO 2 is adsorbed and recovered from a raw material gas such as a gas discharged from a fermentation process or a tobacco process, which has a large fluctuation in CO 2 concentration,
2 Only when the concentration is 99% or more, CO 2 is used as the source gas.
Currently, it is collected by liquefaction equipment.
【０００６】[0006]
【発明が解決しようとする課題】本発明の目的は、回収
対象である特定成分の含有量の変動が大きい原料ガスの
場合でも、常に、高い回収率で、しかも、経済的に特定
成分を回収できる圧力スイング吸着方法を提供すること
にある。SUMMARY OF THE INVENTION An object of the present invention is to recover a specific component economically at a high recovery rate, even in the case of a raw material gas in which the content of the specific component to be recovered varies greatly. It is to provide a pressure swing adsorption method that can be performed.
【０００７】[0007]
【課題を解決するための手段】本発明は、原料ガス中の
特定回収成分濃度が大きく変動する原料ガスから特定成
分を回収する圧力スイング吸着方法であって、吸着塔へ
流入させる特定回収成分の濃度と原料ガス流量に応じて
圧力スイング吸着装置のタイムサイクルを変化させ追従
させることを特徴とする。SUMMARY OF THE INVENTION The present invention is a pressure swing adsorption method for recovering a specific component from a source gas in which the concentration of the specific recovery component in the source gas fluctuates greatly. It is characterized in that the time cycle of the pressure swing adsorption device is changed and followed according to the concentration and the raw material gas flow rate.
【０００８】[0008]
【作用】吸着塔中の吸着剤による特定成分の回収は、原
料ガス中のＣＯ2 、ＣＯ等の特定成分の濃度と吸着塔に
出し入れするガス流量に左右される。一方、従来の圧力
スイング吸着装置における昇圧、吸着、洗浄、脱着の全
工程タイムサイクルは固定している。本発明は、このタ
イムサイクルの中で吸着工程と洗浄工程の時間の比率を
変えること、つまり、原料ガス中における吸着・回収す
るガス成分の濃度が低い時は、洗浄工程の比率を大きく
し、逆に吸着・回収するガス成分の濃度が高い場合に
は、吸着工程の比率を大きくすることで、吸着装置の吸
着能を最大限に発揮できる条件での操業が可能となる。The recovery of the specific component by the adsorbent in the adsorption tower depends on the concentration of the specific component such as CO 2 and CO in the raw material gas and the gas flow rate to and from the adsorption tower. On the other hand, in the conventional pressure swing adsorption device, the time cycle of all steps of pressurization, adsorption, cleaning and desorption is fixed. The present invention changes the ratio of the times of the adsorption process and the cleaning process in this time cycle, that is, when the concentration of the gas component to be adsorbed and recovered in the raw material gas is low, the ratio of the cleaning process is increased. On the contrary, when the concentration of the gas component to be adsorbed / collected is high, by increasing the ratio of the adsorption step, it becomes possible to operate under the condition that the adsorption capacity of the adsorption device can be maximized.
【０００９】[0009]
【実施例】本発明を、原料ガス中のＣＯ2 の濃度が図５
に示す３日間に３０〜９９％と変動するビール発酵排ガ
スを原料ガスとして図１に示す設備を利用してＣＯ2 を
回収する実施例について説明する。EXAMPLE The present invention shows that the concentration of CO 2 in the source gas is as shown in FIG.
An example will be described in which CO 2 is recovered using the equipment shown in FIG. 1 with beer fermentation exhaust gas that fluctuates from 30 to 99% in 3 days as a raw material gas.
【００１０】同図において、ビール発酵設備からの排ガ
スを、冷却塔１、脱湿器２、原ガスホールダー３を経
て、ブロアー４によって、その原料ガス中のＣＯ2 含有
濃度に応じて吸着塔に入る流量を調整して、それぞれ、
活性炭１．４ｋｇを装入した２基の吸着塔５Ａ、５Ｂの
それぞれに送入し、吸着・回収を行った。In the figure, the exhaust gas from the beer fermentation equipment is passed through a cooling tower 1, a dehumidifier 2 and a raw gas holder 3 and then a blower 4 to an adsorption tower according to the CO 2 content concentration in the raw material gas. Adjust the incoming flow rate,
Each of the two adsorption towers 5A and 5B charged with 1.4 kg of activated carbon was fed into each of the two adsorption towers 5A and 5B for adsorption / recovery.
【００１１】吸着塔５Ａ、５Ｂにおける操業工程は、図
２に示すように、一方の吸着塔において、昇圧、吸着、
洗浄の工程を経る間、他方の吸着塔においては脱着工程
にあるもので、それぞれのタイムサイクルを約１６０秒
に設定すると共に、原料ガス中のＣＯ2 含有濃度に応じ
て、図３のように流量条件を設定し、吸着と洗浄工程の
時間比率を吸着工程，洗浄工程の必要流量が流通可能な
ように変更した。The operation steps in the adsorption towers 5A and 5B are as shown in FIG.
While passing through the washing step, the other adsorption tower is in the desorption step, each time cycle is set to about 160 seconds, and according to the CO 2 content concentration in the raw material gas, as shown in FIG. The flow rate conditions were set, and the time ratio between the adsorption and cleaning processes was changed so that the required flow rates for the adsorption and cleaning processes could flow.
【００１２】図３は、到達真空度５０〜５５Ｔｏｒｒの
もとで製品ＣＯ2 の純度９８．５％を確保しようとした
場合の、供給原料ガス中のＣＯ2 含有濃度に対応して、
吸着塔に供給したＣＯ2 の流量を示す。FIG. 3 shows the concentration of CO 2 contained in the feed gas when the purity of product CO 2 is 98.5% under the ultimate vacuum of 50 to 55 Torr.
The flow rate of CO 2 supplied to the adsorption tower is shown.
【００１３】同図において、曲線ａは図２に示す洗浄工
程当たり供給するＣＯ2 量を示し、曲線ｂは図２に示す
吸着工程当たり供給するＣＯ2 量を示す。In the figure, a curve a shows the amount of CO 2 supplied per washing step shown in FIG. 2, and a curve b shows the amount of CO 2 supplied per adsorption step shown in FIG.
【００１４】曲線ａの場合、原料ガス中のＣＯ2 含有濃
度が３０％のときには、ＣＯ2 のガス流量は略２２リッ
トル／ｓｔｅｐとし、９５％のときには、ＣＯ2 のガス
流量を略７リットル／ｓｔｅｐに減少した。In the case of the curve a, when the CO 2 content concentration in the raw material gas is 30%, the CO 2 gas flow rate is approximately 22 liters / step, and when it is 95%, the CO 2 gas flow rate is approximately 7 liters / step. It decreased to step.
【００１５】また、曲線ｂの場合、原料ガス中のＣＯ2
含有濃度が３０％のときには、ＣＯ2 のガス流量は略９
リットル／ｓｔｅｐとし、９５％のときには、ＣＯ2 の
ガス流量を略２２リットル／ｓｔｅｐに増大せしめた。In the case of curve b, CO 2 in the raw material gas
When the content concentration is 30%, the gas flow rate of CO 2 is about 9
The gas flow rate of CO 2 was increased to about 22 liters / step at 95%.
【００１６】以上のデータから明らかなように、吸着工
程，洗浄工程でのガス量を時間比率を変えることにより
原料ガスＣＯ2 濃度が変化して、適切に流すことにより
製品純度を確保しながら効率的にＣＯ2 を回収可能とな
る。As is clear from the above data, the CO 2 concentration of the raw material gas changes by changing the time ratio of the gas amount in the adsorption process and the cleaning process, and by appropriately flowing it, the efficiency can be ensured while ensuring product purity. CO 2 can be recovered.
【００１７】図４は、到達真空度５０〜５５Ｔｏｒｒの
もとで製品ＣＯ2 の純度９８．５％を確保しようとした
場合の、原料ガス中のＣＯ2 濃度と回収率の関係を示す
もので、従来のタイムサイクルの調整を行わない従来方
式の場合を示すＢ曲線の場合と比較して、ＣＯ2 の含有
濃度に合わせた供給量とし、タイムサイクルの調整を行
ったＡ曲線に示す本発明の場合は、その回収率は大幅に
増大していることが分かる。FIG. 4 shows the relationship between the CO 2 concentration in the raw material gas and the recovery rate when the purity of the product CO 2 is intended to be 98.5% under the ultimate vacuum of 50 to 55 Torr. In comparison with the case of the B curve showing the case of the conventional method in which the conventional time cycle is not adjusted, the present invention shown in the A curve in which the supply amount is adjusted to the concentration of CO 2 and the time cycle is adjusted In the case of, the recovery rate is significantly increased.
【００１８】[0018]
【発明の効果】本発明によって以下の効果を奏する。The present invention has the following effects.
【００１９】（１）原料ガス中のＣＯ、ＣＯ2 のような
特定成分の濃度変動が著しい場合でも、高い回収率の下
での圧力スイング吸着装置の利用が可能となり、低コス
トによる回収が可能となる。(1) Even when the concentration fluctuations of specific components such as CO and CO 2 in the raw material gas are remarkable, the pressure swing adsorption device can be used under a high recovery rate, and recovery can be performed at low cost. Becomes
【図１】 本発明を適用した圧力スイング吸着方式の設
備フローチャートを示す。FIG. 1 shows an equipment flowchart of a pressure swing adsorption system to which the present invention is applied.
【図２】 本発明の圧力スイング吸着方式におけるタイ
ムサイクル設定の説明図である。FIG. 2 is an explanatory diagram of time cycle setting in the pressure swing adsorption system of the present invention.
【図３】 原料ガス中のＣＯ2 の含有濃度と供給ガス流
量の関係を示す。FIG. 3 shows the relationship between the concentration of CO 2 contained in the raw material gas and the flow rate of the supply gas.
【図４】 本発明によるＣＯ2 の回収率の効果を従来法
によるものとの比較で示す図である。FIG. 4 is a diagram showing the effect of the CO 2 recovery rate according to the present invention in comparison with that according to the conventional method.
【図５】 ビール発酵排ガスの発酵開始からの日数とＣ
Ｏ2 濃度との関係を示す。[Fig. 5] Days from start of fermentation of beer fermentation exhaust gas and C
The relationship with the O 2 concentration is shown.
１ 冷却塔 ２ 脱湿器 ３ 原ガスホールダ
ー ４ ブロアー ５Ａ，５Ｂ 吸着塔1 Cooling tower 2 Dehumidifier 3 Raw gas holder 4 Blower 5A, 5B Adsorption tower
Claims (1)
変動する原料ガスから特定成分を回収する圧力スイング
吸着方法であって、吸着塔へ流入させる特定回収成分の
濃度と原料ガス流量に応じて圧力スイング吸着装置のタ
イムサイクルを変化させ追従させる圧力スイング吸着方
法。1. A pressure swing adsorption method for recovering a specific component from a raw material gas in which the concentration of the specific recovered component in the raw material gas greatly fluctuates, the method according to the concentration of the specific recovered component flowing into the adsorption tower and the flow rate of the raw material gas. A pressure swing adsorption method in which the time cycle of the pressure swing adsorption device is changed and followed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4253283A JPH0699015A (en) | 1992-09-22 | 1992-09-22 | Pressure swing adsorption method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4253283A JPH0699015A (en) | 1992-09-22 | 1992-09-22 | Pressure swing adsorption method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0699015A true JPH0699015A (en) | 1994-04-12 |
Family
ID=17249132
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4253283A Pending JPH0699015A (en) | 1992-09-22 | 1992-09-22 | Pressure swing adsorption method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0699015A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007209868A (en) * | 2006-02-08 | 2007-08-23 | Mitsubishi Kakoki Kaisha Ltd | Stable operation method of pressure swing adsorption device |
| JP2009262151A (en) * | 2008-04-21 | 2009-11-12 | Air Products & Chemicals Inc | Cyclical swing adsorption process |
| WO2015146213A1 (en) * | 2014-03-28 | 2015-10-01 | 住友精化株式会社 | Method and system for purifying carbon dioxide gas |
| JP2017030996A (en) * | 2015-07-30 | 2017-02-09 | 住友精化株式会社 | Separation recovery method and separation recovery device for carbon dioxide |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6388015A (en) * | 1986-07-24 | 1988-04-19 | ユニオン・カ−バイド・コ−ポレ−シヨン | Method and apparatus for controlling purity of product by pressure swing adsorption |
| JPS6447421A (en) * | 1987-08-16 | 1989-02-21 | Kansai Coke & Chemicals | Pressure alteration type absorbing separation system |
-
1992
- 1992-09-22 JP JP4253283A patent/JPH0699015A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6388015A (en) * | 1986-07-24 | 1988-04-19 | ユニオン・カ−バイド・コ−ポレ−シヨン | Method and apparatus for controlling purity of product by pressure swing adsorption |
| JPS6447421A (en) * | 1987-08-16 | 1989-02-21 | Kansai Coke & Chemicals | Pressure alteration type absorbing separation system |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007209868A (en) * | 2006-02-08 | 2007-08-23 | Mitsubishi Kakoki Kaisha Ltd | Stable operation method of pressure swing adsorption device |
| JP2009262151A (en) * | 2008-04-21 | 2009-11-12 | Air Products & Chemicals Inc | Cyclical swing adsorption process |
| KR101317618B1 (en) * | 2008-04-21 | 2013-10-14 | 에어 프로덕츠 앤드 케미칼스, 인코오포레이티드 | Improvements in cyclical swing adsorption processes |
| WO2015146213A1 (en) * | 2014-03-28 | 2015-10-01 | 住友精化株式会社 | Method and system for purifying carbon dioxide gas |
| JPWO2015146213A1 (en) * | 2014-03-28 | 2017-04-13 | 住友精化株式会社 | Carbon dioxide purification method and purification system |
| JP2017030996A (en) * | 2015-07-30 | 2017-02-09 | 住友精化株式会社 | Separation recovery method and separation recovery device for carbon dioxide |
| TWI698396B (en) * | 2015-07-30 | 2020-07-11 | 日商住友精化股份有限公司 | Carbon dioxide separation and recovery method and separation and recovery system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0302658B1 (en) | Process for producing high purity oxygen gas from air | |
| US6245127B1 (en) | Pressure swing adsorption process and apparatus | |
| US4013429A (en) | Fractionation of air by adsorption | |
| US4775394A (en) | Process for separation of high purity gas from mixed gas | |
| US4359328A (en) | Inverted pressure swing adsorption process | |
| JPS63126522A (en) | Method of separating component of gas fluid | |
| JPH0724735B2 (en) | Over-adsorption recovery system in pressure swing adsorption | |
| US6045603A (en) | Two phase pressure swing adsorption process | |
| JPS5922625A (en) | Method for removing gaseous nitrogen contained in gaseous carbon monoxide or gaseous mixture of carbon monoxide and carbon dioxide by adsorption method | |
| KR950029183A (en) | Adsorptive separation method and apparatus for separating argon and hydrogen in high concentration from ammonia purge gas | |
| JPH0699015A (en) | Pressure swing adsorption method | |
| JPS6137970B2 (en) | ||
| CA1182765A (en) | Repressurization for pressure swing adsorption system | |
| EP0055961B1 (en) | Repressurization process for pressure swing adsorption system | |
| JPH0555171B2 (en) | ||
| JP3025653B2 (en) | Improved pressure swing adsorption method | |
| JP2003019415A (en) | Method for separating gaseous mixture | |
| JP4195131B2 (en) | Single tower type adsorption separation method and apparatus | |
| KR100228239B1 (en) | Apparatus and process for producing nitrogen using psa system depending on nitrogen concentration in the product | |
| JPS62117612A (en) | Regenerating method for adsorption tower | |
| JPH1025102A (en) | Chlorine removal apparatus and oxygen separation by pressure swing adsorption | |
| JPH0967104A (en) | Oxygen concentrating method by pressure swing adsorption | |
| JPS625645B2 (en) | ||
| JPS62193623A (en) | Method for taking out easily-adsorbing substance as high-purity gas | |
| JPH04161214A (en) | Concentration of oxygen gas |