JPH0141371B2 - - Google Patents
Info
- Publication number
- JPH0141371B2 JPH0141371B2 JP57222431A JP22243182A JPH0141371B2 JP H0141371 B2 JPH0141371 B2 JP H0141371B2 JP 57222431 A JP57222431 A JP 57222431A JP 22243182 A JP22243182 A JP 22243182A JP H0141371 B2 JPH0141371 B2 JP H0141371B2
- Authority
- JP
- Japan
- Prior art keywords
- adsorption
- adsorption tower
- gas
- components
- pressure
- 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
Links
- 238000001179 sorption measurement Methods 0.000 claims description 114
- 238000000034 method Methods 0.000 claims description 43
- 238000003795 desorption Methods 0.000 claims description 20
- 239000003463 adsorbent Substances 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 8
- 230000007704 transition Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 description 36
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 238000011067 equilibration Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002441 X-ray diffraction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
Description
この発明は、２基の吸着塔を交互に使用してガ
ス中の難吸着成分を濃縮する方法に関する。
吸着によつてガス中の易吸着成分を吸着除去す
ることで難吸着成分を濃縮する場合、吸着剤の吸
着能力は易吸着成分の吸着の進行にともなつて低
下してくるので、一定量の吸着後に使用を中止し
て脱着を行うことが必要であり、したがつて連続
的な濃縮処理を行う場合には２基の吸着塔が交互
に使用される。このような２塔並設の吸着装置に
おいて、吸着工程では吸着塔に原料ガスが加圧下
で供給され、脱着工程では吸着成分を取出すため
に吸着塔の内部が減圧されるのが普通である。し
かし減圧によつて吸着剤から脱着された易吸着成
分は、脱着工程の終了時点でも吸着塔内に残存す
るので、つぎの吸着工程で原料ガスが導入された
ときに、難吸着成分に混入し、これが製品ガスの
純度を低くする原因となる。
この発明は、脱着工程の終了時点で易吸着成分
を吸着塔から効果的に除去することにより、脱着
工程から吸着工程への切換え時にも製品ガスの純
度を高水準に維持できるようにした難吸着成分濃
縮方法を提供することを目的としている。
以下にこの発明方法の工程の一例を図面にした
がつて説明する。第１図において符号１Ａは第１
吸着塔、１Ｂは第２吸着塔を示し、その各々の内
部には任意の吸着剤が充填されている。難吸着成
分および易吸着成分を含有する原料ガスは、ブロ
ワ２から、バルブＶ１Ａを経て吸着塔１Ａに、ま
たはバルブＶ１Ｂを経て吸着塔１Ｂに各々の底部
から供給されるようになつている。バルブＶ１Ａ
およびＶ１Ｂは所定のシーケンスにしたがつて交
互に開閉制御され、これによつて吸着塔１Ａおよ
び１Ｂにおける吸着工程と脱着工程とが交互に選
択される。いま、吸着塔１Ａが吸着工程にあると
すると、原料ガスはバルブＶ１Ａを通つて吸着塔
１Ａ内にその底部から供給され、常圧で易吸着成
分の吸着分離が行われる。また吸着されなかつた
難吸着成分は、バルブＶ７Ａを経て、フイードバ
ツクタンク３にいつたん入り、逆止弁Ｖ５および
バルブＶ６を経て製品ガスとして外部に取出され
る。また吸着塔１Ｂが吸着工程ににある状態で
は、原料ガスはバルブＶ１Ｂを経て吸着塔１Ｂの
底部に送られ、塔頂に達した難吸着成分がバルブ
Ｖ７Ｂを経てフイードバツクタンク３に導かれ
る。フイードバツクタンク３は、その内部に収容
されたガスの容積に応じて容量が変化する機能を
有するもので、たとえば壁面の一部をベローズで
構成した構造を有する。したがつてフイードバツ
クタンク３内のガスの圧力はほとんど一定に保た
れる。
一方、吸着塔１Ａの脱着工程は、切換バルブＶ
８を吸着塔１Ａ側に切換えるとともにバルブＶ１
Ａ，Ｖ７Ａを閉じ、真空ポンプ５の作用で吸着塔
１Ａ内を減圧することによつて行うことができる
ようになつている。また吸着塔１Ｂの脱着工程
は、切換弁Ｖ８を切換え、バルブＶ１Ｂ，Ｖ７Ｂ
を閉じることによつて同様にして行われ、脱着ガ
スは必要であれば回収される。
さらに吸着塔１Ａの頂部と他方の吸着塔１Ｂの
底部との間には、バルブＶ９Ａおよび逆止弁Ｖ１
０Ａを有するフイードバツク用系路６Ａが設けら
れ、バルブＶ９Ａを開くことにより、吸着塔１Ａ
の頂部から取出された難吸着成分を吸着塔１Ｂの
底部に導入することができるようになつている。
また吸着塔１Ｂの頂部から取出された難吸着成分
を他方の吸着塔１Ａの底部に導入することを可能
にするために、バルブＶ９Ｂおよび逆止弁Ｖ１０
Ｂを有するフイードバツク用系路６Ｂが設けられ
ている。
連続的な難吸着成分濃縮操作は第２図ａ，ｂ，
ｃに示した順序で行われる。まず第２図ａは、第
１吸着塔１Ａが吸着工程、第２吸着塔１Ｂが脱着
工程にある状態を示している。原料ガスは、ブロ
ワ２からバルブＶ１Ａを通つて吸着塔１Ａ内に供
給され、この吸着塔１Ａ内をその底部から頂部ま
で移動する間に、吸着剤による易吸着成分の吸着
分離、すなわち難吸着成分の濃縮が行われる。そ
してこの難吸着成分は、バルブＶ７Ａを経てフイ
ードバツクタンク３にいつたん貯留され、ついで
逆止弁Ｖ５およびバルブＶ６を経て製品ガスとし
て取出される。
一方、吸着塔１Ｂの内部は、バルブＶ１Ｂ，Ｖ
７Ｂを閉じ、切換バルブＶ８をこの吸着塔１Ｂ側
に切換えた状態で、真空ポンプ５の作用で排気さ
れて減圧となり、前回の吸着工程で吸着剤に吸着
されている易吸着成分の脱着が行われる。
第２図ｂは、吸着塔１Ａの吸着工程および吸着
塔１Ｂの脱着工程が終了してから、吸着塔１Ａが
脱着工程に、吸着塔１Ｂが吸着工程にそれぞれ入
るまでの平衡工程にある状態を示す。吸着塔１Ａ
の吸着工程が終了すると同時に、切換バルブＶ８
が吸着塔１Ｂ側から１Ａ側に切換えられ、バルブ
Ｖ１Ａが閉じられるとともに、バルブＶ７Ｂおよ
びＶ９Ａが開かれる。これによつて、脱着工程で
減圧となつている吸着塔１Ｂの内部に、フイード
バツクタンク３内の製品ガスが頂部から、また吸
着塔１Ａを通過した製品ガスが底部からそれぞれ
同時に流入し、吸着塔１Ｂの内部は製品ガスで充
満される。この平衡工程において、フイードバツ
クタンク３はその内容積を自由に変化させ得る構
造となつているので、このフイードバツクタンク
３から吸着塔１Ｂ内に流れることによつてフイー
ドバツクタンク３内の製品ガスの量が減少して
も、一定容積のタンクのように内部の圧力が低下
して製品ガスの流出を制限するというようなこと
はなく、充分な量の製品ガスが吸着塔１Ｂ内に円
滑に流入し、その結果として吸着塔１Ｂ内の平衡
工程がすみやかに行われる。
なお吸着塔１Ｂの平衡工程において、バルブＶ
１ＡおよびＶ１Ｂはともに閉じているので、ブロ
ワ２を停止させてもよく、あるいはブロワ２を運
転したまま、吐出ガスを開閉弁Ｖ１１およびバル
ブＶ１２を経て他に導いてもよい。吸着および脱
着の各工程が３分間程度であるとすると、平衡工
程は９秒間程度で完了する。
平衡工程が完了したのち、バルブＶ１Ｂが開か
れると同時にバルブＶ９Ａが閉じられ、ブロワ２
からバルブＶ１Ｂを経て供給されたガスが吸着塔
１Ｂを通過する吸着工程にそのまま移行する。ま
た平衡工程時に切換バルブＶ８が切換わると同時
に、吸着塔１Ａ内の排気が始まる（第２図ｃ）。
なお吸着塔１Ａの脱着工程と吸着塔１Ｂの吸着
工程が終了すれば、切換バルブＶ８の切換動作
と、バルブＶ７ＡおよびＶ９Ｂの開動作と、バル
ブＶ１Ｂ，Ｖ７Ｂの閉動作とがほとんど同時に行
われて吸着塔１Ａは平衡工程に入る。そしてこの
平衡工程の終了後に、第２図ａの状態に戻る。こ
の動作が繰返されて連続的な濃縮が行われる。
第１図において、吸着塔１Ａ，１Ｂ内の点線で
示した部分の上部は吸着剤、下部は前処理剤であ
ることを示すが、前処理剤は省略してもよい。
吸着塔１Ａおよび１Ｂにおける吸着は、大気圧
にほぼ等しい圧力で行うこともできるが、使用さ
れる吸着剤の種類、あるいは吸着すべき易吸着成
分の種類によつては、加圧下で行つた方がよい場
合もある。たとえば活性炭を吸着剤として使つて
ガス中のCO2を除去する場合には、常圧で充分な
効果が得られるが、天然凝灰石を使用して空気中
のN2を除去（O2を濃縮）する場合には、1.5Kg／
cm2程度の加圧下で吸着を行つた方がよいことが実
験によつて確認されている。このようなN2吸着
用の吸着剤としては、第１表に示すＸ線回折像を
有する天然凝灰岩（モルデナイト）のほか、半合
成ゼオライト、合成ゼオライトなどのような市販
の吸着剤が挙げられる。
The present invention relates to a method for concentrating difficult-to-adsorb components in a gas by alternately using two adsorption towers. When concentrating difficult-to-adsorb components by adsorbing and removing easily-adsorbable components from a gas, the adsorption capacity of the adsorbent decreases as the adsorption of easily-adsorbable components progresses. After adsorption, it is necessary to stop the use and perform desorption, and therefore, in the case of continuous concentration treatment, two adsorption towers are used alternately. In such an adsorption apparatus with two columns installed side by side, the raw material gas is supplied to the adsorption column under pressure in the adsorption step, and the pressure inside the adsorption column is usually reduced in order to take out the adsorbed components in the desorption step. However, the easily adsorbed components that are desorbed from the adsorbent by reduced pressure remain in the adsorption tower even at the end of the desorption process, so when the raw material gas is introduced in the next adsorption process, they may mix with the poorly adsorbed components. , which causes a decrease in the purity of the product gas. This invention effectively removes easily adsorbable components from the adsorption tower at the end of the desorption process, thereby maintaining the purity of the product gas at a high level even when switching from the desorption process to the adsorption process. The purpose is to provide a method for concentrating components. An example of the steps of the method of this invention will be explained below with reference to the drawings. In Fig. 1, the symbol 1A indicates the first
The adsorption tower 1B indicates a second adsorption tower, each of which is filled with an arbitrary adsorbent. The raw material gas containing the hardly adsorbable components and the easily adsorbable components is supplied from the bottom of the blower 2 to the adsorption tower 1A via the valve V1A, or to the adsorption tower 1B via the valve V1B. Valve V1A
and V1B are controlled to open and close alternately according to a predetermined sequence, thereby alternately selecting the adsorption process and the desorption process in the adsorption towers 1A and 1B. Assuming that the adsorption tower 1A is currently in the adsorption step, the raw material gas is supplied from the bottom into the adsorption tower 1A through the valve V1A, and the easily adsorbable components are adsorbed and separated at normal pressure. Further, the poorly adsorbed components that are not adsorbed temporarily enter the feedback tank 3 through the valve V7A, and are taken out as product gas through the check valve V5 and the valve V6. Furthermore, when the adsorption tower 1B is in the adsorption process, the raw material gas is sent to the bottom of the adsorption tower 1B via the valve V1B, and the poorly adsorbed components that have reached the top of the tower are led to the feedback tank 3 via the valve V7B. . The feedback tank 3 has a function in which its capacity changes depending on the volume of gas contained therein, and has a structure in which, for example, a part of the wall surface is formed of a bellows. Therefore, the pressure of the gas in the feedback tank 3 is kept almost constant. On the other hand, in the desorption process of the adsorption tower 1A, the switching valve V
8 to the adsorption tower 1A side and valve V1
This can be done by closing A and V7A and reducing the pressure inside the adsorption tower 1A by the action of the vacuum pump 5. In addition, in the desorption process of the adsorption tower 1B, the switching valve V8 is switched, and the valves V1B and V7B are
This is done in a similar manner by closing the desorption gas, and the desorbed gas is recovered if necessary. Further, a valve V9A and a check valve V1 are provided between the top of the adsorption tower 1A and the bottom of the other adsorption tower 1B.
A feedback line 6A having 0A is provided, and by opening the valve V9A, the adsorption tower 1A
The difficult-to-adsorb components taken out from the top of the adsorption tower 1B can be introduced into the bottom of the adsorption tower 1B.
In addition, in order to make it possible to introduce the poorly adsorbed components taken out from the top of the adsorption tower 1B into the bottom of the other adsorption tower 1A, valve V9B and check valve V10 are installed.
A feedback line 6B having a feedback line 6B is provided. Continuous concentration operations for difficult-to-adsorb components are shown in Figure 2 a, b,
The steps are performed in the order shown in c. First, FIG. 2a shows a state in which the first adsorption tower 1A is in the adsorption process and the second adsorption tower 1B is in the desorption process. The raw material gas is supplied into the adsorption tower 1A from the blower 2 through the valve V1A, and while moving inside the adsorption tower 1A from the bottom to the top, the adsorbent adsorbs and separates the easily adsorbed components, that is, the poorly adsorbed components. is concentrated. This poorly adsorbed component is temporarily stored in the feedback tank 3 via the valve V7A, and then taken out as a product gas via the check valve V5 and the valve V6. On the other hand, inside the adsorption tower 1B, valves V1B and V
7B is closed and the switching valve V8 is switched to the adsorption tower 1B side, the vacuum pump 5 is evacuated and the pressure is reduced, and easily adsorbable components adsorbed by the adsorbent in the previous adsorption process are desorbed. be exposed. Figure 2b shows the state in which the adsorption tower 1A is in the equilibrium process after the adsorption process and the adsorption tower 1B have finished the adsorption process and until the adsorption tower 1A enters the desorption process and the adsorption tower 1B enters the adsorption process, respectively. show. Adsorption tower 1A
At the same time as the adsorption process of
is switched from the adsorption tower 1B side to the 1A side, valve V1A is closed, and valves V7B and V9A are opened. As a result, the product gas in the feedback tank 3 flows simultaneously from the top into the adsorption tower 1B, which is under reduced pressure during the desorption process, and the product gas that has passed through the adsorption tower 1A flows from the bottom. The interior of the adsorption tower 1B is filled with product gas. In this equilibrium step, since the feedback tank 3 has a structure that allows its internal volume to be freely changed, the content inside the feedback tank 3 is increased by flowing from the feedback tank 3 into the adsorption tower 1B. Even if the amount of product gas in the adsorption tower 1B decreases, the internal pressure will not drop and restrict the outflow of product gas unlike in a fixed volume tank, and a sufficient amount of product gas will remain in the adsorption tower 1B. As a result, the equilibrium process within the adsorption tower 1B is carried out quickly. In addition, in the equilibrium step of the adsorption tower 1B, the valve V
1A and V1B are both closed, the blower 2 may be stopped, or the discharged gas may be guided elsewhere via the on-off valve V11 and the valve V12 while the blower 2 is kept operating. Assuming that each step of adsorption and desorption takes about 3 minutes, the equilibration step is completed in about 9 seconds. After the equilibrium process is completed, valve V1B is opened and valve V9A is closed at the same time, blower 2
The gas supplied through the valve V1B directly proceeds to an adsorption step in which it passes through the adsorption tower 1B. Further, at the same time as the switching valve V8 is switched during the equilibrium step, exhaustion of the adsorption tower 1A starts (FIG. 2c). Note that once the desorption process of the adsorption tower 1A and the adsorption process of the adsorption tower 1B are completed, the switching operation of the switching valve V8, the opening operation of the valves V7A and V9B, and the closing operation of the valves V1B and V7B are performed almost simultaneously. The adsorption tower 1A enters an equilibrium step. After this equilibration step is completed, the state returns to the state shown in FIG. 2a. This operation is repeated to achieve continuous concentration. In FIG. 1, the upper part of the part indicated by the dotted line in the adsorption towers 1A and 1B is an adsorbent, and the lower part is a pretreatment agent, but the pretreatment agent may be omitted. Adsorption in the adsorption towers 1A and 1B can be performed at a pressure approximately equal to atmospheric pressure, but depending on the type of adsorbent used or the type of easily adsorbable component to be adsorbed, it is better to perform the adsorption under pressure. In some cases, it is better. For example, when activated carbon is used as an adsorbent to remove CO 2 from gas, a sufficient effect can be obtained at normal pressure, but natural tuff is used to remove N 2 (O 2 ) from the air. 1.5Kg/concentration)
Experiments have confirmed that it is better to perform adsorption under pressure of about cm 2 . Examples of adsorbents for adsorbing N 2 include natural tuff (mordenite) having the X-ray diffraction pattern shown in Table 1, as well as commercially available adsorbents such as semi-synthetic zeolite and synthetic zeolite.
【表】
第３図は、加圧下で吸着を行う場合の装置を示
すものである。この場合には、吸着塔１Ａの塔頂
ガスをクツシヨンタンク３に導入するための開閉
弁Ｖ２Ａ、バルブＶ３Ａおよび逆止弁Ｖ４Ａを有
する第１のレギユレータ系と、吸着塔１Ｂの塔頂
ガスをクツシヨンタンク３に導入するための開閉
弁Ｖ２Ｂ、バルブＶ３Ｂおよび逆止弁Ｖ４Ｂを有
する第２のレギユレータ系とが設けられる。バル
ブＶ３ＡおよびＶ３Ｂは、それぞれ吸着塔１Ａお
よび１Ｂの塔頂ガス圧が設定値に達したことを検
知する圧力スイツチ４Ａおよび４Ｂによつてそれ
ぞれ制御され、フイードバツクタンク３にほぼ常
圧で製品ガスを供給する。バルブＶ７ＡおよびＶ
７Ｂは、それぞれ吸着塔１Ａおよび１Ｂが平衡工
程にあるときだけ開き、フイードバツクタンク３
内の製品ガスをそれぞれ吸着塔１Ａおよび１Ｂに
供給するように動作する。
なおクツシヨンタンク３をその最大容積とほぼ
等しい容積のケース内に収容しておけば、何かの
原因でクツシヨンタンク３の内圧が異常に上昇し
ても、クツシヨンタンク３が破裂するようなこと
はなくなる。
吸着塔１Ａおよび１Ｂとして、それぞれ800Kg
のゼオライトを充填密度0.73で充填したものを使
用し、空気中のO2を前記の本発明方法にしたが
つて濃縮する実験を行つた。他の条件は下記のと
おりであつた。
ブロワ送気量：４m3／min
真空ポンプ排気量：10m3／min
この実験で得られた製品O2濃度と有効酸素量
（EO2）との関係を第４図に、また製品O2濃度と
１塔当りの真空ポンプ排気量（VP）に対する有
効酸素量（EO2）との関係を第５図にそれぞれ示
す。なお有効酸素量（EO2）は下記の式にしたが
つて計算された値である。
EO2＝ｘ％−21％／79％×ｙm3／hr
ｘ：製品O2の濃度
ｙ：製品O2の流量
第４図および第５図から明らかなように、高濃
度のO2が大きい流量で得られていることがわか
る。
なお第５図において、EO2／2VP＝1.0の点は、
３塔（初吸着、終吸着、脱着）で通常行われてい
る方法の典形的な例を基準としたものであり、２
塔で行われるこの発明方法でも、常圧の場合、製
品O2濃度が80％の点で90％（図中の0.9の点）以
上の効果が得られることが示されている。吸着塔
を３塔から２塔にすることは、吸着塔の減少に加
えて、バルブ数の減少という大きなメリツトを与
えるので、この発明の有用性はきわめて高い。
また吸着を加圧下で行つた場合には、製品O2
の濃度が80％の点で、EO2／2VPの値は約1.0に
達し、３塔の場合にほとんど劣らないことが示さ
れている。
以上のようにこの発明によれば、２基の吸着塔
で吸着および脱着を繰返して原料ガス中の難吸着
成分を濃縮するに際して、脱着工程を終了した吸
着塔内に、その底部から吸着工程を終えた吸着塔
の製品ガスを導入するとともに、これと同時に製
品ガスを貯えているフイードバツクタンクから製
品ガスを頂部に導入することにより底部と頂部の
両方で、かつ同時に吸着塔内の圧力を平衡させる
ようにしたので、脱着工程から吸着工程への切換
え時にも製品ガスの純度を高水準に維持でき、難
吸着成分を高濃度で能率良く得ることができる。
また、平衡工程は極めて短時間で完了し、効果的
な濃縮処理が行える。しかもフイードバツクタン
クは容積可変であるので、吸着塔内における平衡
を達成するのに必要な量の製品ガスを供給圧力の
低下をほとんど伴わずに供給できるので、平衡工
程は短時間で完了する。[Table] Figure 3 shows an apparatus for adsorption under pressure. In this case, a first regulator system having an on-off valve V2A, a valve V3A, and a check valve V4A for introducing the top gas of the adsorption tower 1A into the cushion tank 3, and a first regulator system for introducing the top gas of the adsorption tower 1B into the compression tank 3 are used. A second regulator system having an on-off valve V2B, a valve V3B, and a check valve V4B for introduction into the cushion tank 3 is provided. Valves V3A and V3B are controlled by pressure switches 4A and 4B, respectively, which detect when the top gas pressures of adsorption towers 1A and 1B reach a set value, and supply the product to feedback tank 3 at approximately normal pressure. Supply gas. Valve V7A and V
7B is opened only when adsorption towers 1A and 1B are in the equilibrium process, respectively, and feed back tank 3
The product gases in the adsorption towers 1A and 1B are supplied to the adsorption towers 1A and 1B, respectively. If the cushion tank 3 is housed in a case with a volume approximately equal to its maximum volume, even if the internal pressure of the cushion tank 3 rises abnormally for some reason, the cushion tank 3 will not explode. Nothing will happen. 800Kg each for adsorption towers 1A and 1B
An experiment was conducted to condense O 2 in the air according to the method of the present invention using a zeolite packed with a packing density of 0.73. Other conditions were as follows. Blower air supply volume: 4 m 3 /min Vacuum pump displacement volume: 10 m 3 /min Figure 4 shows the relationship between the product O 2 concentration and the effective oxygen amount (EO 2 ) obtained in this experiment, and the product O 2 concentration Figure 5 shows the relationship between the effective oxygen amount (EO 2 ) and the vacuum pump displacement (VP) per tower. Note that the effective oxygen amount (EO 2 ) is a value calculated according to the following formula. EO 2 = x% - 21%/79% x ym 3 /hr x: Concentration of product O 2 y: Flow rate of product O 2 As is clear from Figures 4 and 5, high concentration O 2 is large. It can be seen that this is obtained from the flow rate. In Figure 5, the point EO 2 /2VP=1.0 is
This is based on a typical example of a method that is normally performed in three columns (initial adsorption, final adsorption, and desorption), and
It has been shown that even in the method of this invention carried out in a column, at normal pressure, an effect of 90% or more (point 0.9 in the figure) can be obtained at a point where the product O 2 concentration is 80%. Changing the number of adsorption towers from three to two has the great advantage of reducing the number of valves in addition to the reduction in the number of adsorption towers, so the usefulness of this invention is extremely high. In addition, when adsorption is performed under pressure, the product O 2
At the point where the concentration of EO 2 /2VP is 80%, the value of EO 2 /2VP reaches about 1.0, indicating that it is almost as good as the three-column case. As described above, according to the present invention, when concentrating difficult-to-adsorb components in a raw material gas by repeating adsorption and desorption in two adsorption towers, the adsorption step is started from the bottom of the adsorption tower that has completed the desorption step. By introducing the product gas from the finished adsorption tower and at the same time introducing the product gas from the feedback tank storing the product gas to the top, the pressure inside the adsorption tower can be reduced at both the bottom and the top at the same time. Since equilibrium is achieved, the purity of the product gas can be maintained at a high level even when switching from the desorption process to the adsorption process, and difficult-to-adsorb components can be efficiently obtained at a high concentration.
In addition, the equilibration process can be completed in an extremely short time, and effective concentration processing can be performed. Moreover, since the feedback tank has a variable volume, it is possible to supply the amount of product gas necessary to achieve equilibrium in the adsorption tower with almost no drop in supply pressure, so the equilibrium process can be completed in a short time. .
第１図はこの発明の実施に用いられた装置の系
統図、第２図ａ，ｂ，ｃは第１図の装置の工程順
を示す説明図、第３図はこの発明に使用される他
の装置の系統図、第４図は製品O2濃度と有効酸
素量との関係を示すグラフ、第５図は製品O2濃
度と性能比率との関係を示すグラフである。
１Ａ，１Ｂ……吸着塔、２……ブロワ、３……
フイードバツクタンク、４Ａ，４Ｂ……圧力スイ
ツチ、５……真空ポンプ、６Ａ，６Ｂ……系路。
Fig. 1 is a system diagram of the apparatus used in carrying out this invention, Fig. 2 a, b, and c are explanatory diagrams showing the process order of the apparatus of Fig. 1, and Fig. 3 is an illustration of other equipment used in this invention. Fig. 4 is a graph showing the relationship between product O 2 concentration and effective oxygen amount, and Fig. 5 is a graph showing the relationship between product O 2 concentration and performance ratio. 1A, 1B...Adsorption tower, 2...Blower, 3...
Feedback tank, 4A, 4B...pressure switch, 5...vacuum pump, 6A, 6B...system.
Claims (1)
の一方に原料ガスを供給して易吸着成分を吸着さ
せることによつて難吸着成分を濃縮する吸着工程
と、他方の吸着塔に前回の吸着工程で吸着された
易吸着成分を減圧下で脱着させる脱着工程とを各
吸着塔について交互に行わせるガス中の難吸着成
分濃縮方法において、吸着工程中の一方の吸着塔
から取り出した製品ガスを、内部のガスをその容
積にかかわらずほぼ一定の圧力で収容できる可変
容積のフイードバツクタンク内に一時的貯留し、
この一方の吸着塔が吸着工程を終了したときに該
一方の吸着塔を通過し、吸着工程終了後の製品ガ
スを脱着工程を終了して内部が減圧状態にあり、
次回の吸着工程へ移行中の他方の吸着塔の底部に
導入すると同時に、この他方の吸着塔の頂部に上
記フイードバツクタンク内の上記製品ガスを導入
することによつて、脱着工程を終了し、次回の吸
着工程へ移行中の該他方の吸着塔内の圧力を平衡
させる平衡工程を付加したことを特徴とするガス
中の難吸着成分濃縮方法。 ２ 上記吸着塔の塔頂ガス圧が所定圧に達したと
きに上記製品ガスをフイードバツクタンク内へ貯
留されるように制御されていることを特徴とする
特許請求の範囲第１項記載のガス中の難吸着成分
濃縮方法。[Scope of Claims] 1. An adsorption step of supplying a raw material gas to one of two adsorption towers filled with a selective adsorbent to adsorb easily adsorbed components, thereby concentrating difficult-adsorbed components; In a method for concentrating difficult-to-adsorbable components in gas, in which each adsorption tower alternately performs a desorption step in which easily adsorbable components adsorbed in the other adsorption step in the previous adsorption step are desorbed under reduced pressure. The product gas extracted from the adsorption tower is temporarily stored in a variable volume feedback tank that can accommodate the internal gas at a nearly constant pressure regardless of its volume.
When this one adsorption tower finishes the adsorption process, the product gas passes through the one adsorption tower and the product gas after the adsorption process is completed and the interior is in a reduced pressure state,
The desorption process is completed by introducing the product gas in the feedback tank into the top of the other adsorption tower at the same time that it is introduced into the bottom of the other adsorption tower that is transitioning to the next adsorption process. . A method for concentrating difficult-to-adsorb components in a gas, characterized in that an equilibrium step is added to balance the pressure in the other adsorption tower during transition to the next adsorption step. 2. The adsorption tower according to claim 1, wherein the product gas is controlled to be stored in a feedback tank when the top gas pressure of the adsorption tower reaches a predetermined pressure. A method for concentrating difficult-to-adsorb components in gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57222431A JPS59112821A (en) | 1982-12-17 | 1982-12-17 | Concentration of difficult to adsorb component in gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57222431A JPS59112821A (en) | 1982-12-17 | 1982-12-17 | Concentration of difficult to adsorb component in gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59112821A JPS59112821A (en) | 1984-06-29 |
| JPH0141371B2 true JPH0141371B2 (en) | 1989-09-05 |
Family
ID=16782284
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57222431A Granted JPS59112821A (en) | 1982-12-17 | 1982-12-17 | Concentration of difficult to adsorb component in gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59112821A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0177828U (en) * | 1987-11-12 | 1989-05-25 |
-
1982
- 1982-12-17 JP JP57222431A patent/JPS59112821A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59112821A (en) | 1984-06-29 |
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