JP2504448B2 - Pressure swing adsorption device - Google Patents
Pressure swing adsorption deviceInfo
- Publication number
- JP2504448B2 JP2504448B2 JP62052301A JP5230187A JP2504448B2 JP 2504448 B2 JP2504448 B2 JP 2504448B2 JP 62052301 A JP62052301 A JP 62052301A JP 5230187 A JP5230187 A JP 5230187A JP 2504448 B2 JP2504448 B2 JP 2504448B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- adsorption tower
- purity
- pipe
- pressure swing
- 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 - Lifetime
Links
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- Separation Of Gases By Adsorption (AREA)
Description
【発明の詳細な説明】 ［産業上の利用分野］ 本発明はCOやN2等の回収目的成分ガスを高純度に精製
するための圧力スイング吸着装置（PSA装置）に関し、
詳細にはPSA装置の運転再開に際して回収目的成分ガス
の純度を短時間に高レベルまで向上させることのできる
PSA装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial application] The present invention relates to a pressure swing adsorption device (PSA device) for purifying a target gas for recovery such as CO and N 2 to high purity,
Specifically, when the operation of the PSA device is restarted, it is possible to improve the purity of the target gas for recovery to a high level in a short time.
It concerns PSA devices.
以下においてはCOを高純度で回収する例について詳述
するが、本発明はこの例に限定されず、O2やN2等、他の
ガスを精製する場合についても適用できる。Hereinafter, an example of recovering CO with high purity will be described in detail, but the present invention is not limited to this example and can be applied to the case of purifying other gas such as O 2 and N 2 .
［従来の技術］ COを濃縮回収する方法としては深冷分離法や化学吸収
法が工業的に汎用されている。これらの方法は高純度ガ
スの大量精製乃至製造には適しており、効果的な運転が
できるが、設備全体が大がかりとなり、高価になってし
まうという欠点がある。[Prior Art] As a method for concentrating and recovering CO, a cryogenic separation method or a chemical absorption method is industrially widely used. These methods are suitable for mass purification or production of high-purity gas and can operate effectively, but have a drawback that the entire equipment becomes bulky and expensive.
これに対し圧力スイング吸着法による場合は設備及び
操作が簡単であり、経済的に有利である為、特定成分の
吸着除去もしくは吸着させたのちの脱着回収をはかるガ
ス分離法またはガス精製法として広く利用されている。On the other hand, the pressure swing adsorption method is easy to install and operate and is economically advantageous. Therefore, it is widely used as a gas separation method or a gas purification method for adsorbing and removing a specific component or desorbing and recovering the adsorbed specific component. It's being used.
例えばCO,N2,H2からなる混合ガス（例えば転炉ガス）
を原料とし、ゼオライト等を吸着剤としてCOの濃縮回収
する方法を代表例として採り上げその方法を説明すると
下記の様な手順で行なわれる。圧力スイング吸着装置と
して第３図（説明図）に示す様な４塔式PSA装置を利用
する場合において、吸着塔2aに注目して諸工程を説明す
る。For example, mixed gas composed of CO, N 2 and H 2 (eg converter gas)
Taking as a representative example a method of concentrating and recovering CO using as a raw material and using zeolite or the like as an adsorbent, the method will be described as follows. When a 4-tower PSA apparatus as shown in FIG. 3 (illustration) is used as the pressure swing adsorption apparatus, the steps will be described by focusing on the adsorption tower 2a.
加圧された混合ガス（以下原料ガスともいう）は供給
管１から導入され、自動開閉弁（以下単に弁という）V1
を経て吸着塔2aへ送られ、原料ガス中のCOは吸着塔2a内
の吸着剤に吸着され（昇圧工程）、吸着されなかったガ
スは排出管８から系外へ放出される。吸着塔2aの吸着剤
が破過に至る直前に原料ガスの供給を弁V1の操作によっ
て停止し、次いで吸着塔2a及び2bをバイパス管10aによ
って連通し吸着塔3a内の圧力を大気圧近くまで減圧す
る。そして後吸着塔2a内に残存している不純成分を置換
除去する目的で、製品ガスタンク４内の高純度COを洗浄
ガスブロア５によって加圧し、洗浄用管12及び弁V6,V3
を介して吸着塔2aへ導入する（洗浄工程）。即ち製品ガ
スの一部を洗浄ガスとして消費するのであるが、吸着塔
2aを洗浄した後の排ガスは弁V5及びバイパス管10aを通
して隣接する吸着塔2bへ送給され回収目的成分として吸
着再回収する様になっている。こうして塔内の洗浄を終
えた吸着塔2aは弁V2及び回収管９を介して真空ポンプ３
に連通され、塔内を減圧してCO脱着し（脱着工程）、脱
着された高純度COは製品ガスタンク４内に貯留し、製品
ガス回収ブロア６により適宜取出管７からユーザー側へ
送り出す。A pressurized mixed gas (hereinafter also referred to as raw material gas) is introduced from the supply pipe 1, and an automatic opening / closing valve (hereinafter simply referred to as valve) V 1
The CO in the raw material gas is adsorbed by the adsorbent in the adsorption tower 2a (pressurizing step), and the unadsorbed gas is discharged from the exhaust pipe 8 to the outside of the system. The supply of the raw material gas is stopped by operating the valve V 1 immediately before the adsorbent in the adsorption tower 2a reaches a breakthrough, and then the adsorption towers 2a and 2b are connected by the bypass pipe 10a so that the pressure in the adsorption tower 3a is close to atmospheric pressure. Depressurize to. Then, in order to replace and remove the impure components remaining in the post-adsorption tower 2a, the high purity CO in the product gas tank 4 is pressurized by the cleaning gas blower 5, and the cleaning pipe 12 and the valves V 6 , V 3
It is introduced into the adsorption tower 2a via (cleaning step). That is, part of the product gas is consumed as cleaning gas, but the adsorption tower
The exhaust gas after cleaning 2a is fed to the adjacent adsorption tower 2b through the valve V 5 and the bypass pipe 10a and is adsorbed and recovered again as a recovery target component. The adsorption tower 2a, which has completed the cleaning in the tower in this way, is connected to the vacuum pump 3 via the valve V 2 and the recovery pipe 9.
The CO is desorbed by decompressing the inside of the tower (desorption process), and the desorbed high-purity CO is stored in the product gas tank 4 and is appropriately sent to the user side from the extraction pipe 7 by the product gas recovery blower 6.
一方前記脱着工程を終了した吸着塔2aでは前述の原料
ガス導入（吸着工程）に始まる一連の工程が繰り返えさ
れる。そして各吸着塔2a〜2dにおいても上記の各工程を
1/4サイクルずつずらして連続的に行なうことによって
高純度COを連続的に製造することができるのである。On the other hand, in the adsorption tower 2a which has completed the desorption step, a series of steps starting from the above-mentioned raw material gas introduction (adsorption step) are repeated. And in each adsorption tower 2a ~ 2d
High-purity CO can be continuously produced by continuously shifting the cycle by 1/4 cycle.
［発明が解決しようとする問題点］ 原料ガスとして転炉ガスを例示して説明してきたが、
転炉ガスの発生源である転炉は、１月に１回の割合で定
期補修が行なわれており、操業が停止される。従ってCO
回収用の前記PSA装置もこれに合わせて運転を中止しな
ければならなくなる。[Problems to be Solved by the Invention] Although the converter gas has been described as an example of the raw material gas,
The converter, which is the source of converter gas, is regularly repaired once a month, and its operation is stopped. Therefore CO
The PSA device for recovery will have to be stopped accordingly.
次に転炉の操業が再開されると、上記PSA装置の運転
も再開されるのであるが、運転の立上がり時はCOの純度
が低く高純度COが得られる迄にかなりの時間が必要とさ
れている。第２図の従来例はその一例を示すものであり
100％近い高純度に到達する迄には最低１時間程度の立
上り時間が必要であり、従ってその間に回収されるガス
は特別の用途が開発されない限り廃棄せざるを得ない。
この様に立上り純度が低くなる主な原因は、吸着塔2a〜
2dの洗浄ガスとして運転再開後に発生した低純度の製品
ガスを使用せざるを得ない点にあるものと思われる。即
ち前回運転によって得られた製品ガスは製品ガスタンク
４はほゞ完全に抜き出すのが常法であり、製品ガスタン
ク４内を実質上空にした様な状態で吸着運転を再開して
いたのである。そこで高純度COの一部をPSA再起動時用
として製品ガスタンクに残しておくことも考えられた
が、タンク内に適量を保存しておくことが難かしく、し
かも運転再開時に他の理由で発生した低純度ガスが混入
したものは製品として利用できなくなって高純度製品ガ
スの浪費を招くので、上記対策は好ましい手段ではない
ことが分かった。Next, when the converter operation is restarted, the operation of the PSA device will be restarted, but at the start of the operation, the purity of CO is low and it takes a considerable time to obtain high-purity CO. ing. The conventional example of FIG. 2 shows an example thereof.
It takes at least 1 hour for the rise time to reach a high purity close to 100%, so the gas recovered during that time must be discarded unless a special application is developed.
The main cause of such low startup purity is the adsorption tower 2a-
It seems that there is no choice but to use the low-purity product gas generated after restarting the operation as the 2d cleaning gas. That is, it is a normal method that the product gas obtained by the previous operation is almost completely extracted from the product gas tank 4, and the adsorption operation is restarted in a state where the inside of the product gas tank 4 is substantially emptied. Therefore, it was considered to leave a part of high-purity CO in the product gas tank for PSA restart, but it is difficult to store an appropriate amount in the tank, and it is generated for other reasons when restarting operation. It has been found that the above countermeasure is not a preferable means, because the substance mixed with the low-purity gas cannot be used as a product and wastes the high-purity product gas.
この様なところから本発明者はPSA装置の運転再開
後、短時間のうちに高純度な回収目的成分ガスを取り出
すことのできるPSA装置を提供すべく種々の研究を重ね
た結果、本発明を完成させるに至った。From such a point, the present inventor has conducted various studies to provide a PSA device capable of extracting a high-purity recovery target component gas in a short time after the operation of the PSA device is restarted. It came to completion.
［問題点を解決するための手段］ 上記目的を達成し得た本発明PSA装置は、製品ガスタ
ンクに並列して回収目的成分ガスの一部を吸着させる為
の加熱式吸着塔を設け、該加熱式吸着塔の出側は前記圧
力スイング吸着塔の洗浄ガス用配管に連結してなる点に
要旨を有するものである。[Means for Solving the Problems] The PSA device of the present invention which has achieved the above object is provided with a heating type adsorption tower for adsorbing a part of the recovery target component gas in parallel with the product gas tank, and The gist of the type adsorption tower is that it is connected to the cleaning gas pipe of the pressure swing adsorption tower.
［作用及び実施例］ 第１図は本発明の代表的な実施例を示す説明図であ
る。吸着塔2a〜2d及び製品ガスタンク４等の構造は第３
図に示したPSA装置と同様であるが、本発明の特徴的な
部分は製品ガスタンク４の他にCO吸着装置Ｒを付設した
点にある。即ち製品ガスタンク４に弁V10を介して導入
管13を設け、該導入管13にCO吸着塔11を接合し、該吸着
塔11出側には弁V12及び調圧弁V13を介して導出管15を設
け、導出管15は洗浄用管12に連結する。CO吸着塔11には
アルミナにCuClを担持させたCo吸着剤11aを充填してお
き、また該吸着塔11には熱媒を導入できる加熱装置16を
添設させる。尚符号14の配管は逃し管を示し、CO吸着塔
11の吸着量よりも過剰のCOが供給されたときに、高純度
COを取出管７へ送り込むためのものである。該CO吸着装
置Ｒの使用方法は下記の通りである。即ちPSA装置の定
常運転時に弁V10を開放してCO吸着塔11内の吸着剤11aに
高純度COを吸着させておき、上記PSA装置が停止されて
製品ガスタンク４内に高純度COが無くなったときにおい
ても該CO吸着塔11内にCOを保持させておく。そしてPSA
装置再起動時に加熱装置16へ熱媒を導入し、吸着剤11a
に吸着された高純度COを脱着してPSA装置の吸着塔2a〜2
dの洗浄用ガスとして利用する。尚このとき洗浄ガスブ
ロワ５は停止して弁V6は閉とする。こうすることによっ
てPSA装置の起動初期においても吸着塔2a〜2dは高純度C
Oによって洗浄されることになり、脱着工程における製
品ガスは早期に所定濃度まで高めることができる。尚前
記CO吸着塔１に替えて圧力タンクを配設することも考え
られるが、圧力タンクを設ける場合には、製品ガス圧を
高める必要上圧縮機等を別途設けなければならず、設備
費が高くつくことになる。しかも圧力タンクはCO吸着塔
よりもCO貯留量が小さいので、大型の圧力タンクを準備
しなければならないといった不都合がある。[Operation and Example] FIG. 1 is an explanatory view showing a typical example of the present invention. The structure of the adsorption towers 2a-2d and the product gas tank 4 is the third
Although it is similar to the PSA device shown in the figure, a characteristic part of the present invention is that a CO adsorption device R is additionally provided in addition to the product gas tank 4. That is, the product gas tank 4 is provided with an inlet pipe 13 via a valve V 10 , a CO adsorption tower 11 is joined to the inlet pipe 13, and the outlet side of the adsorption tower 11 is led out via a valve V 12 and a pressure regulating valve V 13. A pipe 15 is provided, and the outlet pipe 15 is connected to the cleaning pipe 12. The CO adsorption tower 11 is filled with a Co adsorbent 11a in which CuCl is supported on alumina, and the adsorption tower 11 is additionally provided with a heating device 16 capable of introducing a heating medium. The pipe number 14 indicates a relief pipe, and is a CO adsorption tower.
High purity when CO is supplied in excess of 11
It is for sending CO into the extraction pipe 7. The method of using the CO adsorption device R is as follows. That is, during steady operation of the PSA device, the valve V 10 is opened to adsorb high-purity CO to the adsorbent 11a in the CO adsorption tower 11, and the PSA device is stopped so that the product gas tank 4 does not contain high-purity CO. Even in this case, CO is kept in the CO adsorption tower 11. And PSA
When the device is restarted, the heat medium is introduced into the heating device 16, and the adsorbent 11a
Adsorption towers 2a-2
It is used as a cleaning gas for d. At this time, the cleaning gas blower 5 is stopped and the valve V 6 is closed. By doing so, the adsorption towers 2a to 2d will have high purity C even at the initial startup of the PSA device.
Since it is cleaned by O, the product gas in the desorption process can be quickly raised to a predetermined concentration. It is possible to install a pressure tank instead of the CO adsorption tower 1, but if a pressure tank is installed, a compressor or the like must be installed separately because the product gas pressure needs to be increased, so the equipment cost is low. It will be expensive. Moreover, since the pressure tank has a smaller CO storage amount than the CO adsorption tower, there is the inconvenience that a large pressure tank must be prepared.
第２図に示される破線のグラフは、第３図に示す従来
装置を使ってPSA装置の再起動を行った場合の製品ガス
純度の挙動であり、実線で示される本発明例は、第１図
に示す本発明装置を使って装置の再起動を行った場合の
製品ガス純度の挙動を表わす。従来の装置の場合製品ガ
スが所定純度に達するのに約４時間を要したが、本発明
の装置を使用した場合には、1/8の約30分の所定純度と
することができ、原料ガスの消費及びPSA装置の予備運
転時間を大幅に削減できる様になった。The broken line graph shown in FIG. 2 shows the behavior of the product gas purity when the PSA apparatus is restarted using the conventional apparatus shown in FIG. 3, and the example of the present invention shown by the solid line is the first 7 shows the behavior of product gas purity when the apparatus of the present invention shown in the figure is used to restart the apparatus. In the case of the conventional apparatus, it took about 4 hours for the product gas to reach the predetermined purity, but when the apparatus of the present invention is used, it is possible to obtain the predetermined purity of about 1/8 of about 30 minutes. It has become possible to significantly reduce the gas consumption and the pre-operation time of the PSA device.
［発明の効果］ 本発明のPSA装置を使用することにより、PSA装置再起
動時に短時間内で高純度な回収目的成分ガスが得られる
様になり、PSA装置再起動時における原料ガスの浪費やP
SA装置の無駄な予備運転時間を極力抑制することができ
る様になった。しかもこれらの効果は最小限の設備を追
加するだけで達成され、極めて経済的である。[Advantages of the Invention] By using the PSA apparatus of the present invention, a high-purity recovery target component gas can be obtained within a short time when the PSA apparatus is restarted, and the waste of raw material gas when the PSA apparatus is restarted P
It has become possible to suppress the unnecessary preliminary operation time of the SA device as much as possible. Moreover, these effects can be achieved by adding a minimum amount of equipment, which is extremely economical.
第１図は本発明の代表的な実施例を示す説明図、第２図
は本発明装置及び従来装置による再起動時の製品ガス純
度の変化を示すグラフ、第３図は従来装置を示す説明図
である。 １……原料ガス供給管、2a〜2d……PSA吸着塔 ３……真空ポンプ、４……製品ガスタンク ５……洗浄ガスブロワー ６……製品ガス回収ブロワー ７……取出管、８……排出管 ９……回収管、10a……バイパス管 11……CO吸着塔、12……洗浄用管 13……導入管、14……逃し管 15……導出管、16……加熱装置FIG. 1 is an explanatory view showing a typical embodiment of the present invention, FIG. 2 is a graph showing a change in product gas purity at the time of restart by the device of the present invention and a conventional device, and FIG. 3 is an explanation of the conventional device. It is a figure. 1 ... Raw material gas supply pipe, 2a to 2d ... PSA adsorption tower 3 ... Vacuum pump, 4 ... Product gas tank 5 ... Cleaning gas blower 6 ... Product gas recovery blower 7 ... Extraction pipe, 8 ... Discharge Pipe 9 …… Recovery pipe, 10a …… Bypass pipe 11 …… CO adsorption tower, 12 …… Cleaning pipe 13 …… Introduction pipe, 14 …… Escape pipe 15 …… Outlet pipe, 16 …… Heating device
Claims (1)
成分ガスを吸着させ、該吸着塔の減圧脱着によって上記
回収目的成分ガスを高濃度で製品ガスタンク内へ回収す
る圧力スイング吸着装置であって、前記製品ガスタンク
に並列して回収目的成分ガスの一部を吸着させる為の加
熱式吸着塔を設け、該加熱式吸着塔の出側は前記圧力ス
イング吸着塔の洗浄ガス用配管に連結してなることを特
徴とする圧力スイング吸着装置。1. A pressure swing adsorption device for adsorbing a recovery target component gas on an adsorbent in a pressure swing adsorption tower, and recovering the recovery target component gas at a high concentration into a product gas tank by desorption and desorption of the adsorption tower. And a heating type adsorption tower for adsorbing a part of the target gas for collection is provided in parallel with the product gas tank, and the outlet side of the heating type adsorption tower is connected to the cleaning gas pipe of the pressure swing adsorption tower. A pressure swing adsorption device characterized by the following.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62052301A JP2504448B2 (en) | 1987-03-06 | 1987-03-06 | Pressure swing adsorption device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62052301A JP2504448B2 (en) | 1987-03-06 | 1987-03-06 | Pressure swing adsorption device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63218229A JPS63218229A (en) | 1988-09-12 |
| JP2504448B2 true JP2504448B2 (en) | 1996-06-05 |
Family
ID=12910970
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62052301A Expired - Lifetime JP2504448B2 (en) | 1987-03-06 | 1987-03-06 | Pressure swing adsorption device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2504448B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4627571B2 (en) * | 2010-08-20 | 2011-02-09 | 住友精化株式会社 | Carbon monoxide separation method and carbon monoxide separation apparatus |
-
1987
- 1987-03-06 JP JP62052301A patent/JP2504448B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS63218229A (en) | 1988-09-12 |
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