JP3031797B2 - Pressure fluctuation adsorption separation method - Google Patents
Pressure fluctuation adsorption separation methodInfo
- Publication number
- JP3031797B2 JP3031797B2 JP5143967A JP14396793A JP3031797B2 JP 3031797 B2 JP3031797 B2 JP 3031797B2 JP 5143967 A JP5143967 A JP 5143967A JP 14396793 A JP14396793 A JP 14396793A JP 3031797 B2 JP3031797 B2 JP 3031797B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- adsorption
- pressure
- adsorption tower
- tower
- 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 - Fee Related
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Description
【０００１】[0001]
【産業上の利用分野】本発明は、圧力変動吸着分離方法
に係り、特に消費動力が小さく、目的成分の回収率が向
上する圧力変動吸着分離方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a pressure fluctuation adsorption / separation method, and more particularly to a pressure fluctuation adsorption / separation method which consumes less power and improves the recovery rate of a target component.
【０００２】[0002]
【従来の技術】圧力変動吸着分離方法（ＰＳＡ法）は、
混合ガス中の易吸着成分を分離回収したり、逆に難吸着
成分の分離回収等に利用されている。図８は、このよう
な圧力変動吸着分離方法を利用したＣＯ分離精製装置の
説明図である。この装置は、原料タンク４１と、製品ガ
スタンク４２と、吸着後ガスタンク４３と、同一容量を
有する４基の吸着塔４４〜４７と、ガスの供給および排
出用のブロワ４８、真空ポンプ４９と、前記吸着塔に設
けられた切り換えバルブ群５０〜７３とから主として構
成されている。2. Description of the Related Art Pressure fluctuation adsorption separation method (PSA method)
It is used for separating and recovering easily adsorbed components in a mixed gas and conversely for separating and recovering hardly adsorbed components. FIG. 8 is an explanatory diagram of a CO separation / purification apparatus using such a pressure fluctuation adsorption separation method. The apparatus comprises a raw material tank 41, a product gas tank 42, a post-adsorption gas tank 43, four adsorption towers 44 to 47 having the same capacity, a blower 48 for supplying and discharging gas, a vacuum pump 49, It mainly comprises switching valve groups 50 to 73 provided in the adsorption tower.
【０００３】このような構成において、昇圧工程、吸着
工程、製品ガスパージ工程および脱着工程は次のように
行われる。すなわち、(1)脱着工程が終了した塔４４の
バルブ５１を開きタンク４３から吸着後ガスを導入して
昇圧する。(2)昇圧工程が終了した塔４５のバルブ５９
とバルブ５８を開き、タンク４１から原料ガスを導入
し、易吸着成分であるＣＯを吸着させる。このとき吸着
後ガスはタンク４３に貯留される。次いで、(3)吸着工
程が終了した塔４６のバルブ６６とバルブ６２を開き、
タンク４２からブロワ４８により製品ガスを導入して吸
着剤に吸着している不純ガスをパージする。パージ後の
ガスはタンク４１に戻して再利用される。次いで、(4)
製品ガスパージ工程が終了した塔４７のバルブ７３を開
き、真空ポンプ４９によって易吸着成分であるＣＯが吸
引、脱着され、製品ＣＯとして製品ガスタンク４２に回
収される。[0003] In such a configuration, the pressure increasing step, the adsorption step, the product gas purging step and the desorption step are performed as follows. That is, (1) the valve 51 of the tower 44 in which the desorption process has been completed is opened, and the gas is adsorbed from the tank 43 and the pressure is increased. (2) The valve 59 of the tower 45 after the completion of the pressure raising step
And the valve 58 are opened, and a raw material gas is introduced from the tank 41 to adsorb CO as an easily adsorbable component. At this time, the gas after adsorption is stored in the tank 43. Next, (3) the valve 66 and the valve 62 of the tower 46 in which the adsorption step has been completed are opened,
The product gas is introduced from the tank 42 by the blower 48 to purge the impurity gas adsorbed on the adsorbent. The purged gas is returned to the tank 41 and reused. Then, (4)
After the product gas purging step is completed, the valve 73 of the tower 47 is opened, and CO, which is an easily adsorbed component, is sucked and desorbed by the vacuum pump 49, and is recovered as product CO in the product gas tank.
【０００４】これらの手順を表１に示す。[0004] Table 1 shows these procedures.
【０００５】[0005]
【表１】 しかしながら、このような圧力変動吸着分離方法は、原
料ガス中の易吸着成分（ＣＯ）濃度が低い場合には、多
量のパージガスが必要となり、動力消費量が多いという
問題があり、また脱着工程において真空ポンプを使用し
ない場合、すなわち高圧から大気圧までの圧力変動を利
用する場合にはＣＯの回収率が低下するという欠点があ
った。[Table 1] However, such a pressure fluctuation adsorption separation method has a problem that when the concentration of the easily adsorbable component (CO) in the raw material gas is low, a large amount of purge gas is required, and the power consumption is large. When a vacuum pump is not used, that is, when a pressure fluctuation from high pressure to atmospheric pressure is used, there is a disadvantage that the recovery rate of CO decreases.
【０００６】[0006]
【発明が解決しようとする課題】本発明の目的は、上記
従来技術の問題点を解決し、消費動力が小さく、脱着工
程で真空ポンプを使用しない場合であっても、目的成分
を高効率で回収することができる圧力変動吸着分離方法
を提供することにある。SUMMARY OF THE INVENTION An object of the present invention is to solve the above-mentioned problems of the prior art and to reduce the power consumption and to efficiently remove the target component even when a vacuum pump is not used in the desorption step. It is an object of the present invention to provide a pressure fluctuation adsorption separation method that can be recovered.
【０００７】[0007]
【課題を解決するための手段】上記目的を達成するため
本発明は、吸着剤を充填した吸着塔に原料ガスを導入し
て易吸着成分を吸着する吸着工程と、該吸着工程後の吸
着塔に前記原料ガスの導入方向と同一方向から製品ガス
を導入して不純ガスをパージする製品ガスパージ工程
と、該製品ガスパージ工程後の吸着塔を前記原料ガス導
入方向と逆方向に減圧して易吸着成分を回収する脱着工
程と、該脱着工程後の吸着塔に前記原料ガス導入方向と
は逆方向から吸着後ガスを導入して昇圧する昇圧工程と
からなる圧力変動吸着分離方法において、前記吸着工程
後で製品ガスパージ工程前の吸着塔を前記原料ガス導入
方向と同一方向に減圧して易吸着成分の吸着フロントを
吸着塔出口側に移動させるとともに、前記昇圧工程時の
昇圧ガスとして前記吸着後ガスに代えて吸着後ガスより
も易吸着成分濃度が低いガスを用いることを特徴とす
る。SUMMARY OF THE INVENTION In order to achieve the above object, the present invention provides an adsorption step in which a raw material gas is introduced into an adsorption tower filled with an adsorbent to adsorb easily adsorbable components, and an adsorption tower after the adsorption step. A product gas purge step of introducing a product gas from the same direction as the source gas introduction direction to purge impure gas, and depressurizing the adsorption tower after the product gas purge step in a direction opposite to the source gas introduction direction for easy adsorption. The pressure-fluctuation adsorption separation method, comprising: a desorption step of recovering components; and a pressure-increasing step of introducing a post-adsorption gas from the direction opposite to the direction of introduction of the raw material gas into the adsorption tower after the desorption step and increasing the pressure. moves the adsorption front of the easily adsorbable component in the adsorption tower outlet was later reduced pressure adsorption tower before the product gas purge step to the raw gas-introducing direction in the same direction, the step-up gas during said boosting step The strongly adsorbed component concentration than the post-adsorption gas in place of the FR wearing gas is characterized by using a low gas.
【０００８】[0008]
【作用】吸着工程、製品ガスパージ工程、脱着工程およ
び昇圧工程からなる圧力変動吸着分離方法の前記吸着工
程後で、製品ガスパージ工程前の吸着塔を前記原料ガス
の供給方向と同一方向（以下、順方向ともいう）に減圧
することにより、主として吸着剤に吸着され難い難吸着
成分が流出して易吸着成分の吸着フロントが吸着塔の出
口付近に到達する。従って、吸着塔内の易吸着成分濃度
が相対的に上昇し、その後のパージ工程における必要パ
ージガス量が少なくなるので、消費動力が著しく低下す
る。After the adsorption step of the pressure fluctuation adsorption separation method including the adsorption step, the product gas purge step, the desorption step and the pressure increase step, the adsorption tower before the product gas purge step is moved in the same direction as the supply direction of the raw material gas (hereinafter referred to as the forward direction). When the pressure is reduced in the direction, the hardly adsorbable component that is hardly adsorbed by the adsorbent mainly flows out, and the adsorption front of the easily adsorbable component reaches near the outlet of the adsorption tower. Therefore, the concentration of the easily adsorbed component in the adsorption tower relatively increases, and the required amount of purge gas in the subsequent purging step is reduced, so that the power consumption is significantly reduced.
【０００９】また、昇圧工程における昇圧ガスとして吸
着工程で流出する吸着後ガスよりも易吸着成分濃度が小
さい、高濃度または高純度の難吸着成分ガスを用いるこ
とにより、脱着工程後に吸着塔内に残存する易吸着成分
の吸着塔出口側濃度が低くなる。従って、その後、原料
ガスを導入して易吸着成分を吸着させる際（吸着工程）
に排出される吸着後ガス中の易吸着成分濃度がきわめて
低くなるので、全体として易吸着成分の回収率が向上す
る。[0009] Further, by using a high-concentration or high-purity hardly adsorbable component gas having a lower concentration of easily adsorbed components than the post-adsorption gas flowing out in the adsorption process as a pressurized gas in the pressurization process, the gas can be introduced into the adsorption tower after the desorption process. The concentration of the remaining easily adsorbed components on the outlet side of the adsorption tower decreases. Therefore, when the raw material gas is subsequently introduced to adsorb easily adsorbed components (adsorption step)
Since the concentration of the easily adsorbed component in the post-adsorption gas discharged to the tank becomes extremely low, the recovery rate of the easily adsorbed component is improved as a whole.
【００１０】なお、脱着工程終了後の吸着塔内には比較
的多くの易吸着成分が残存しており、吸着後ガスのよう
に易吸着成分が比較的多く含まれているガスで昇圧する
と、吸着塔出口、すなわち吸着工程のガス流出口付近に
おける易吸着成分濃度が高くなり、次の吸着工程におけ
る流出ガス中の易吸着成分濃度が高くなるので回収率が
低下することになる。[0010] After the desorption step, a relatively large amount of easily adsorbed components remains in the adsorption tower, and if the pressure is increased by a gas containing a relatively large amount of easily adsorbed components such as a gas after adsorption, The concentration of the easily adsorbed component near the outlet of the adsorption tower, that is, near the gas outlet in the adsorption step is increased, and the concentration of the easily adsorbed component in the effluent gas in the next adsorption step is increased, so that the recovery rate is reduced.
【００１１】図２〜図４は、本発明の原理を示す説明図
であり、図２は、吸着工程後、製品ガスパージ工程前の
順方向への減圧工程における吸着塔内の易吸着成分の濃
縮効果を前記順方向への減圧圧力を変えて示したもので
ある。横軸は原料ガス中の易吸着成分、例えばＣＯ濃度
を、縦軸は順方向減圧工程後の吸着塔内のＣＯ濃度をそ
れぞれ示す。図３は、順方向減圧工程後、すなわち製品
ガスパージ工程前の吸着塔内のＣＯ濃度と、製品ガスパ
ージ工程における脱着工程回収ガス量に対する所要パー
ジガス量の比との関係を示すものである。図２および図
３において、吸着工程における圧力Ｐａに対する順方向
減圧工程における圧力Ｐｕの比が小さくなるほど、すな
わち順方向減圧圧力が低くなるほど塔内のＣＯ濃度が高
くなり、塔内ＣＯ濃度が高いほど所要パージガス量が少
なくて済むことが分かる。FIGS. 2 to 4 are explanatory diagrams showing the principle of the present invention. FIG. 2 shows the concentration of the easily adsorbed components in the adsorption tower in the forward depressurization step after the adsorption step and before the product gas purging step. The effect is shown by changing the reduced pressure in the forward direction. The horizontal axis indicates the easily adsorbed component, for example, the CO concentration in the raw material gas, and the vertical axis indicates the CO concentration in the adsorption tower after the forward pressure reduction step. FIG. 3 shows the relationship between the CO concentration in the adsorption tower after the forward pressure reduction step, that is, before the product gas purge step, and the ratio of the required purge gas amount to the desorption step recovery gas amount in the product gas purge step. 2 and 3, as the ratio of the pressure Pu in the forward pressure reduction step to the pressure Pa in the adsorption step becomes smaller, that is, the lower the forward pressure reduction pressure, the higher the CO concentration in the column, and the higher the CO concentration in the tower, It can be seen that the required purge gas amount is small.
【００１２】また図４は、昇圧工程で使用される昇圧ガ
ス中の易吸着成分、例えばＣＯ濃度に対する昇圧工程後
の吸着塔内気相ＣＯ濃度との関係を示す図である。図に
おいて、昇圧ガス中のＣＯ濃度が低いほど吸着塔出口側
のＣＯ濃度は低くなり、その後の吸着工程で吸着後ガス
に同伴されるＣＯの損失量が低減されることが分かる。FIG. 4 is a diagram showing the relationship between the easily adsorbed components in the pressurized gas used in the pressurizing step, for example, the CO concentration and the gaseous phase CO concentration in the adsorption tower after the pressurizing step. In the figure, it can be seen that the lower the CO concentration in the pressurized gas, the lower the CO concentration on the outlet side of the adsorption tower, and the smaller the amount of CO entrained in the gas after adsorption in the subsequent adsorption step.
【００１３】本発明において、吸着工程後、製品ガスパ
ージ工程前の吸着塔を順方向に減圧する、順方向減圧工
程において易吸着成分の吸着フロントを前記吸着塔出口
まで到達させるために、前記吸着工程における原料ガス
供給量をあらかじめ調節しておくことが好ましい。本発
明において、吸着後ガスとは吸着工程で吸着塔内に導入
された原料ガスのうち吸着剤に吸着されることなく吸着
塔を流出するガスをいう。In the present invention, after the adsorption step, the adsorption tower before the product gas purging step is depressurized in the forward direction. In the forward depressurization step, the adsorbing step is performed so that the adsorption front of the easily adsorbable component reaches the adsorption tower outlet. It is preferable to adjust the supply amount of the raw material gas in advance. In the present invention, the post-adsorption gas refers to a gas flowing out of the adsorption tower without being adsorbed by the adsorbent among the raw material gases introduced into the adsorption tower in the adsorption step.
【００１４】本発明において、昇圧工程で用いる吸着後
ガスよりも易吸着成分濃度が小さいガスとして、例えば
高濃度の水素ガスをはじめとする高濃度または高純度難
吸着成分ガスが使用されるが、このような昇圧ガス中の
易吸着成分濃度は１０ｖｏｌ％以下、好ましくは２ｖｏ
ｌ％以下、より好ましくは全く含まれていないことであ
る。また、このような昇圧ガスは系外から導入してもよ
い。本発明は、製品ガス脱着工程において真空ポンプを
使用しない、高圧から大気圧までの圧力変動を利用する
場合に特に有効である。In the present invention, as the gas having a lower concentration of easily adsorbed components than the post-adsorption gas used in the pressurizing step, for example, a high-concentration or high-purity hardly-adsorbed component gas such as a high-concentration hydrogen gas is used. The concentration of the easily adsorbed component in such pressurized gas is 10 vol% or less, preferably 2 vol%.
1% or less, more preferably not contained at all. Such a pressurized gas may be introduced from outside the system. The present invention is particularly effective when utilizing a pressure fluctuation from high pressure to atmospheric pressure without using a vacuum pump in the product gas desorption step.
【００１５】[0015]
【実施例】次に本発明を実施例により、さらに詳細に説
明する。図１は、本発明の一実施例を示す圧力変動吸着
分離方法の装置系統図である。この装置は、パージオフ
ガスタンク１と、製品ガスタンク２と、同一容量を有す
る４基の吸着塔３、４、５および６と、ガスの供給およ
び排出に使用されるコンプレッサ７および８と、前記吸
着塔に設けられた切り換えバルブ群１３〜３８とから主
として構成されている。９は吸着塔に原料ガスＡを導入
する原料ガス導入管、１０は製品ガスＢを抜き出す製品
ガス抜出管、１１は、昇圧ガスＣを導入する昇圧ガス導
入管、および１２は排出ガスＤを抜き出す排出ガス管で
ある。Next, the present invention will be described in more detail by way of examples. FIG. 1 is an apparatus system diagram of a pressure fluctuation adsorption separation method showing one embodiment of the present invention. The apparatus comprises a purge-off gas tank 1, a product gas tank 2, four adsorption towers 3, 4, 5 and 6 having the same capacity, compressors 7 and 8 used for supplying and discharging gas, It mainly comprises switching valve groups 13 to 38 provided in the tower. Reference numeral 9 denotes a source gas introduction pipe for introducing the source gas A into the adsorption tower, 10 denotes a product gas extraction pipe for extracting the product gas B, 11 denotes a pressure gas introduction pipe for introducing the pressure gas C, and 12 denotes an exhaust gas D. Exhaust gas pipe to be extracted.
【００１６】このような構成において、昇圧工程、吸着
工程、順方向減圧工程、製品ガスパージ工程および脱着
工程は次のように行われる。 (1)脱着工程が終了した吸着塔３のバルブ１４を開き、
昇圧ガス導入管１１から易吸着成分を含まない昇圧ガス
として、例えば水素ガスを導入して吸着塔を昇圧する。 (2)昇圧工程が終了した吸着塔４のバルブ２３とバルブ
２２を開き、原料ガス導入管９から原料ガスＡを導入し
て易吸着成分、例えばＣＯを吸着させる。このとき吸着
後ガスは、排出ガス管１２から抜き出されて図示省略し
た排出ガスタンクに貯留される。 (3)吸着工程が終了した塔５のバルブ２６を開き、易吸
着成分、例えばＣＯの吸着フロントが吸着塔の出口まで
達するように減圧する。このとき吸着塔から流出する、
主として難吸着成分を含むガスは排出ガスタンクに導か
れる。 (4)順方向減圧工程が終了した後、吸着塔５のバルブ３
０を開いて製品ガスタンク２から製品ガスＢを導入して
吸着塔内の不純ガス（難吸着成分）をパージする。この
ときパージ後のガスは、易吸着成分を比較的多く含むの
でパージオフガスタンク１に導入され、再利用される。 (5)製品ガスパージ工程が終了した吸着塔６のバルブ３
８を開きコンプレッサ７により、吸着された易吸着成
分、例えばＣＯを吸引、脱着して製品タンク２に回収す
る。In such a configuration, the pressure increasing step, the adsorption step, the forward pressure reducing step, the product gas purging step, and the desorption step are performed as follows. (1) Open the valve 14 of the adsorption tower 3 after the desorption step is completed,
For example, hydrogen gas is introduced as a pressurized gas containing no easily adsorbed component from the pressurized gas introduction pipe 11 to pressurize the adsorption tower. (2) Open the valves 23 and 22 of the adsorption tower 4 after the completion of the pressure raising step, and introduce the raw material gas A from the raw gas introduction pipe 9 to adsorb easily adsorbable components, for example, CO. At this time, the post-adsorption gas is extracted from the exhaust gas pipe 12 and stored in an exhaust gas tank (not shown). (3) Open the valve 26 of the tower 5 where the adsorption step is completed, and reduce the pressure so that the adsorption front of the easily adsorbed component, for example, CO, reaches the outlet of the adsorption tower. At this time, it flows out of the adsorption tower,
The gas mainly containing the hardly adsorbable component is led to the exhaust gas tank. (4) After the forward decompression step is completed, the valve 3 of the adsorption tower 5
0 is opened and the product gas B is introduced from the product gas tank 2 to purge the impurity gas (the hardly adsorbable component) in the adsorption tower. At this time, the purged gas contains a relatively large amount of easily adsorbed components, and is introduced into the purge off gas tank 1 and reused. (5) The valve 3 of the adsorption tower 6 after the product gas purge step has been completed.
8 is opened, and the adsorbed easily adsorbed component, for example, CO, is sucked and desorbed by the compressor 7 and collected in the product tank 2.
【００１７】これらの操作手順をまとめて表２に示す。Table 2 summarizes these operating procedures.
【００１８】[0018]
【表２】 [Table 2]
【００１９】本実施例において、各吸着塔は、昇圧工
程、吸着工程、順方向減圧工程、製品ガスパージ工程お
よび脱着工程を順次繰り返して易吸着成分の分離回収を
行う。昇圧工程、吸着工程および脱着工程はそれぞれ同
一時間、すなわち表２における２工程分行われるが、順
方向減圧工程と製品ガスパージ工程はそれぞれ１工程分
行われる。In this embodiment, each of the adsorption towers sequentially separates and recovers easily adsorbed components by sequentially repeating a pressure raising step, an adsorption step, a forward pressure reducing step, a product gas purging step and a desorption step. The pressure increasing step, the adsorption step, and the desorption step are each performed at the same time, that is, two steps in Table 2, but the forward depressurization step and the product gas purge step are each performed for one step.
【００２０】表２において、吸着塔３で昇圧工程が行わ
れている工程１および工程２の間に、吸着塔４では順方
向減圧工程に引き続いて製品ガスパージ工程が行われ、
吸着塔５では脱着工程が行われ、吸着塔６では吸着工程
がそれぞれ行われる。次いで、工程３および工程４のと
きは、吸着塔３で吸着工程、吸着塔４で脱着工程、吸着
塔５で昇圧工程、吸着塔６で順方向減圧工程および製品
ガスパージ工程がそれぞれ行われ、以下表２に示したサ
イクルに従って各工程が進み、例えば易吸着成分として
ＣＯが分離、回収される。In Table 2, between Step 1 and Step 2 in which the pressure increasing step is performed in the adsorption tower 3, a product gas purging step is performed in the adsorption tower 4 following the forward pressure reducing step.
In the adsorption tower 5, a desorption step is performed, and in the adsorption tower 6, an adsorption step is performed. Next, in Steps 3 and 4, the adsorption step in the adsorption tower 3, the desorption step in the adsorption tower 4, the pressure increasing step in the adsorption tower 5, the forward depressurizing step and the product gas purging step in the adsorption tower 6 are performed, respectively. Each step proceeds according to the cycle shown in Table 2, and, for example, CO is separated and recovered as an easily adsorbed component.
【００２１】本実施例において、昇圧工程の一部と順方
向減圧工程の一部で圧力均等化（均圧）操作を行うこと
もできる。次に本発明を具体的実施例によってさらに詳
細に説明する。 実施例１ 図１に示すＰＳＡ装置において、吸着剤として合成ゼオ
ライトを用い、吸着塔の充填層容量：７６０ｍｌ／塔、
吸着圧力：９ａｔｍ、順方向減圧圧力：４．５ａｔｍ、
減圧脱着圧力：１．３ａｔｍ、周囲温度：２５℃、脱着
工程の時間を１８０ｓｅｃとしてＣＯとＨ2 とが１対１
に混合された２成分混合ガスからＣＯを分離した。運転
操作は前記表２に従って行った。そのフローシートと、
供給ガス、排出ガスおよび製品ガスのガス流量ならびに
使用濃度の測定結果を図５に示した。なお、ガス流量は
１工程（１８０ｓｅｃ）間に流れるガス量を吸着塔空塔
容積を１として換算して示したものである（以下、図６
および図７において同様）。In this embodiment, a pressure equalizing (equalizing) operation can be performed in a part of the pressure increasing step and a part of the forward pressure reducing step. Next, the present invention will be described in more detail with reference to specific examples. Example 1 In the PSA apparatus shown in FIG. 1, a synthetic zeolite was used as an adsorbent, and the packed bed capacity of the adsorption tower was 760 ml / tower.
Adsorption pressure: 9 atm, forward depressurization pressure: 4.5 atm,
Decompression pressure: 1.3 atm, ambient temperature: 25 ° C., desorption step time 180 sec, CO: H 2 ratio is 1: 1
CO was separated from the mixed gas of the two components mixed in. The driving operation was performed according to Table 2 above. The flow sheet,
FIG. 5 shows the measurement results of the gas flow rates of the supply gas, the exhaust gas, and the product gas and the usage concentrations. The gas flow rate is obtained by converting the amount of gas flowing during one process (180 seconds) by converting the empty space of the adsorption tower to 1 (hereinafter, FIG. 6).
And FIG. 7).
【００２２】実施例２ 実施例１における順方向減圧工程時に発生する主として
難吸着成分を含むガスを昇圧ガスとして（均圧工程で）
利用した以外は実施例１と同様にして同様の吸着分離実
験を行った。そのフローシートと、供給ガス、排出ガス
および製品ガスのガス流量ならびに使用濃度の測定結果
を図６に示した。Example 2 A gas mainly containing hardly adsorbable components, which is generated in the forward pressure reducing step in Example 1, is used as a pressurized gas (in the pressure equalizing step).
A similar adsorption / separation experiment was performed in the same manner as in Example 1 except for using the same. FIG. 6 shows the flow sheet and the measurement results of the gas flow rates of the supply gas, the exhaust gas, and the product gas and the concentrations used.
【００２３】比較例１ 吸着工程、製品ガスパージ工程、脱着工程および昇圧工
程からなる従来の圧力変動吸着分離方法で真空ポンプを
使用することなく大気圧以上で脱着工程を行った場合、
すなわち、吸着工程と製品ガスパージ工程との間で、順
方向に減圧することなく、しかも昇圧工程における昇圧
ガスとして吸着後ガスをそのまま用い、吸着圧力：９ａ
ｔｍ、脱着圧力：１．３ａｔｍとした以外は前記実施例
１と同様にして同様のＣＯ分離回収実験を行った。その
フローシートと、供給ガス、排出ガスおよび製品ガスの
ガス流量ならびに使用濃度の測定結果を図７に示した。COMPARATIVE EXAMPLE 1 A conventional pressure-fluctuation adsorption / separation method comprising an adsorption step, a product gas purging step, a desorption step and a pressure increasing step, when the desorption step was carried out at atmospheric pressure or higher without using a vacuum pump,
That is, between the adsorption step and the product gas purging step, the post-adsorption gas is used as it is as the pressurized gas in the pressurizing step without reducing the pressure in the forward direction, and the adsorbing pressure: 9a
The same CO separation and recovery experiment was performed in the same manner as in Example 1 except that tm and desorption pressure were set to 1.3 atm. FIG. 7 shows the flow sheet and the measurement results of the gas flow rates of the supply gas, the exhaust gas, and the product gas and the usage concentrations.
【００２４】図５、６および７から、吸着工程後、製品
ガスパージ工程前に順方向減圧工程を行った実施例１お
よび実施例２におけるＣＯ回収率は比較例１に比べて著
しく高くなった。また実施例１および実施例２は、昇圧
ガスとして吸着後ガスよりも易吸着成分濃度が小さいガ
スを用いたことにより、製品ガスパージ工程で使用する
製品ガス量が比較例１に比べて少量で済んだので、消費
動力が著しく低減した。5, 6, and 7, the CO recovery in Examples 1 and 2 in which the forward pressure reducing step was performed after the adsorption step and before the product gas purging step was significantly higher than that in Comparative Example 1. Further, in Example 1 and Example 2, the amount of the product gas used in the product gas purging step was smaller than that in Comparative Example 1 because a gas having a lower concentration of easily adsorbed components than the gas after adsorption was used as the pressurized gas. As a result, power consumption has been significantly reduced.
【００２５】[0025]
【発明の効果】本発明によれば、吸着工程後、製品ガス
パージ工程前の吸着塔を順方向に減圧する、順方向減圧
工程を行うことにより、吸着塔内の難吸着成分が排出さ
れて易吸着成分の吸着フロントが塔出口まで移動し、相
対的に易吸着成分濃度が高くなるので原料ガス中の易吸
着成分濃度を高くした場合と同様の効果が得られ、製品
ガスパージ工程における必要パージガス量が減少し、消
費動力量を大幅に低減することができる。According to the present invention, after the adsorption step, the adsorption tower before the product gas purging step is depressurized in the forward direction. By performing the forward depressurization step, the hardly adsorbed components in the adsorption tower are easily discharged. Since the adsorption front of the adsorbed component moves to the tower outlet and the concentration of the easily adsorbed component becomes relatively high, the same effect as when the concentration of the easily adsorbed component in the raw material gas is increased is obtained. And power consumption can be greatly reduced.
【００２６】また、本発明によれば、昇圧ガスとして易
吸着成分濃度の低いガスを用いることにより、その後の
吸着工程で排出される吸着後ガス中の易吸着成分濃度が
極めて低くなり、全体として回収率が向上する。Further, according to the present invention, by using a gas having a low concentration of easily adsorbed components as the pressurized gas, the concentration of easily adsorbed components in the post-adsorption gas discharged in the subsequent adsorption step becomes extremely low. Recovery rate is improved.
【図１】本発明の一実施例を示す装置系統図。FIG. 1 is a system diagram showing an embodiment of the present invention.
【図２】、FIG.
【図３】、FIG.
【図４】本発明の原理を示す説明図FIG. 4 is an explanatory view showing the principle of the present invention.
【図５】、FIG.
【図６】本発明の実施例を示す説明図。FIG. 6 is an explanatory view showing an embodiment of the present invention.
【図７】、FIG.
【図８】従来技術を示す説明図。FIG. 8 is an explanatory view showing a conventional technique.
１…パージオフガスタンク、２…製品ガスタンク、３〜
６…吸着塔、７〜８…コンプレッサ、９…原料ガス導入
管、１０…製品ガス抜出管、１１…昇圧ガス導入管、１
２…排出ガス管。1 ... Purge off gas tank, 2 ... Product gas tank, 3 ~
6 ... Adsorption tower, 7-8 ... Compressor, 9 ... Raw material gas introduction pipe, 10 ... Product gas extraction pipe, 11 ... Pressurized gas introduction pipe, 1
2. Exhaust gas pipe.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 井汲 真之佑 千葉県市原市八幡海岸通１番地 三井造 船株式会社 千葉事業所内 (56)参考文献 特開 平１−262919（ＪＰ，Ａ) 特開 昭62−121615（ＪＰ，Ａ) 特公 平４−78324（ＪＰ，Ｂ２) (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 53/04 ────────────────────────────────────────────────── ─── Continuing from the front page (72) Inventor Shinnosuke Ibuki 1 Yawata Kaigandori, Ichihara City, Chiba Prefecture Mitsui Engineering & Shipbuilding Co., Ltd. Chiba Works (56) References JP-A-1-262919 (JP, A) 62-121615 (JP, A) JP 4-78324 (JP, B2) (58) Fields investigated (Int. Cl. 7 , DB name) B01D 53/04
Claims (1)
入して易吸着成分を吸着する吸着工程と、該吸着工程後
の吸着塔に前記原料ガスの導入方向と同一方向から製品
ガスを導入して不純ガスをパージする製品ガスパージ工
程と、該製品ガスパージ工程後の吸着塔を前記原料ガス
導入方向と逆方向に減圧して易吸着成分を回収する脱着
工程と、該脱着工程後の吸着塔に前記原料ガス導入方向
とは逆方向から吸着後ガスを導入して昇圧する昇圧工程
とからなる圧力変動吸着分離方法において、前記吸着工
程後で製品ガスパージ工程前の吸着塔を前記原料ガス導
入方向と同一方向に減圧して易吸着成分の吸着フロント
を吸着塔出口側に移動させるとともに、前記昇圧工程時
の昇圧ガスとして前記吸着後ガスに代えて吸着後ガスよ
りも易吸着成分濃度が低いガスを用いることを特徴とす
る圧力変動吸着分離方法。1. An adsorption step of introducing a raw material gas into an adsorption tower filled with an adsorbent to adsorb easily adsorbable components, and a product gas is introduced into the adsorption tower after the adsorption step from the same direction as the introduction direction of the raw material gas. A product gas purging step of introducing and purging an impurity gas, a desorption step of depressurizing the adsorption tower after the product gas purge step in a direction opposite to the raw material gas introduction direction to collect easily adsorbed components, and an adsorption step after the desorption step. A pressure fluctuation adsorption separation method comprising: a step of introducing a gas after adsorption from a direction opposite to the direction of introduction of the raw material gas into the column, and increasing the pressure. under reduced pressure in a direction the same direction moves the adsorption front of the easily adsorbable component in the adsorption tower outlet, the strongly adsorbed component concentration than the post-adsorption gas in place of the post-adsorption gas as a boost gas during said boosting step Pressure fluctuation adsorption separation method characterized by using a gas having a low pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5143967A JP3031797B2 (en) | 1993-06-15 | 1993-06-15 | Pressure fluctuation adsorption separation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5143967A JP3031797B2 (en) | 1993-06-15 | 1993-06-15 | Pressure fluctuation adsorption separation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07744A JPH07744A (en) | 1995-01-06 |
| JP3031797B2 true JP3031797B2 (en) | 2000-04-10 |
Family
ID=15351227
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5143967A Expired - Fee Related JP3031797B2 (en) | 1993-06-15 | 1993-06-15 | Pressure fluctuation adsorption separation method |
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| Country | Link |
|---|---|
| JP (1) | JP3031797B2 (en) |
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1993
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Also Published As
| Publication number | Publication date |
|---|---|
| JPH07744A (en) | 1995-01-06 |
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