JPS62176515A - Pretreatment device for gas separation - Google Patents
Pretreatment device for gas separationInfo
- Publication number
- JPS62176515A JPS62176515A JP61017941A JP1794186A JPS62176515A JP S62176515 A JPS62176515 A JP S62176515A JP 61017941 A JP61017941 A JP 61017941A JP 1794186 A JP1794186 A JP 1794186A JP S62176515 A JPS62176515 A JP S62176515A
- Authority
- JP
- Japan
- Prior art keywords
- adsorption
- pressure
- valve
- outlet
- adsorption column
- 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.)
- Granted
Links
- 238000000926 separation method Methods 0.000 title claims description 5
- 238000001179 sorption measurement Methods 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 13
- 239000002994 raw material Substances 0.000 claims description 5
- 239000003463 adsorbent Substances 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims 2
- 229910002092 carbon dioxide Inorganic materials 0.000 claims 1
- 239000001569 carbon dioxide Substances 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 14
- 230000008929 regeneration Effects 0.000 description 12
- 238000011069 regeneration method Methods 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001105 regulatory effect Effects 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
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、ガス分離における前処理として、水分および
Ｃ０２を吸着するガス分屋における前処理装置に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a pretreatment device in a gas branch that adsorbs moisture and CO2 as a pretreatment in gas separation.
従来の装置は、例えば特開昭５８−２１４７７１号記載
のように、再生が終了した吸着塔の加圧風量が予定値に
なるように流量制御することにより、装置内の圧力変動
を抑制していた。しかし、このような制御をしても、再
生時において吸着塔内は大気圧となっており、これをｌ
Ｏ分程度の加圧時間内で吸着圧力まで加圧することによ
って０゜２〜０．３Ｋｇ／ｄの圧力変動が生じていた。Conventional equipment suppresses pressure fluctuations within the equipment by controlling the flow rate so that the pressurized air volume of the adsorption tower after regeneration reaches a predetermined value, as described in JP-A-58-214771, for example. Ta. However, even with this kind of control, the inside of the adsorption tower remains at atmospheric pressure during regeneration, and this
Pressurizing to the adsorption pressure within a pressurizing time of about 0 minutes caused a pressure fluctuation of 0.2 to 0.3 kg/d.
この圧力変動は後工程でのガス分離に悪影響を与え、例
えば上述の圧力変動によって製品Ｎ２の組成の変動が約
０．１−０．３ ｐｐｍＱ２あった。また、この切換時
必要となる加圧ガス量（パージロス）は、原料空気量の
５〜７％程度必要となり、その分製品の原単位を悪くし
ていた。This pressure fluctuation had an adverse effect on gas separation in the subsequent process, and for example, the above-mentioned pressure fluctuation caused a fluctuation in the composition of the product N2 by about 0.1-0.3 ppmQ2. Further, the amount of pressurized gas (purge loss) required at the time of this switching is about 5 to 7% of the amount of raw material air, which worsens the unit consumption of the product.
上記従来技術は、切換時の加圧ガス盟が多く必要なこと
により、装置の圧力変動が大きいという問題があり、パ
ージロスも大きいという問題な残している。The above-mentioned conventional technology has the problem of large pressure fluctuations in the device due to the need for a large number of pressurized gas channels at the time of switching, and still has the problem of large purge loss.
本発明の目的は、従来技術による表面の圧力変動を大幅
に改善することにある。The aim of the invention is to significantly improve surface pressure fluctuations according to the prior art.
再生工程のための脱圧な行う吸着塔と吸着工程のための
加圧を行う吸着塔を均圧することにより、原料空気によ
る加圧ガス量を約５０％減少でき、さらに原単位につい
ても改善できる。このため、本発明では、おのおのの吸
着塔出口と他塔の入口または出口とを連通ずる導管と、
そのおのおのの導管の途中に弁を設ける構成とし、再生
工程のための脱圧な行う吸着塔と吸着工程のための加圧
を行う吸着塔との均圧運転を可能とした。By equalizing the pressure of the adsorption tower that depressurizes for the regeneration process and the adsorption tower that pressurizes for the adsorption process, the amount of pressurized gas due to feed air can be reduced by about 50%, and the basic unit can also be improved. . Therefore, in the present invention, a conduit that communicates the outlet of each adsorption tower with the inlet or outlet of another tower;
A valve was installed in the middle of each conduit to enable equal pressure operation between the adsorption tower that depressurizes the regeneration process and the adsorption tower that pressurizes the adsorption process.
従来技術の切換チャートの例を第２図に、本発明の切換
チャートの例を第３図に示す。An example of a conventional switching chart is shown in FIG. 2, and an example of a switching chart of the present invention is shown in FIG.
従来技術では、例えば１５分切換の場合、吸着圧力（約
６に９／ｃｒ！ｔ）から再生圧力（大気圧）までの脱圧
が約５分、また加圧が約１０分であり３塔を順次切換え
て使用されていた。In the conventional technology, for example, in the case of a 15-minute changeover, it takes about 5 minutes to depressurize from the adsorption pressure (about 6 to 9/cr!t) to the regeneration pressure (atmospheric pressure), and about 10 minutes to pressurize, which requires 3 towers. It was used by switching sequentially.
しかし、各基の加圧時間と他塔の脱圧時間とが一致しな
いため均圧工程を設けられない。本発明では、これを第
３図のようにした。すなわち、例えば１５分切換えの場
合、吸着時間は２０分とし、内２塔使用時間を１０分、
単独使用時間を１０分とす・る。また、脱圧時間は５分
とし、内２分は他塔を加圧する均圧時間、残り３分は約
３ Ｋｐ／ｃｒＩから大気圧までの脱圧時間、加圧時間
は１０分とし、内２分は他より加圧する均圧時間、残り
８分は約３１’ｑ／ｃｆｌより約６ 匂／１ｆｆｌまで
原料空気により加圧する加圧時間とした。However, the pressure equalization step cannot be provided because the pressurization time of each group and the depressurization time of other columns do not match. In the present invention, this is done as shown in FIG. That is, for example, in the case of a 15-minute changeover, the adsorption time is 20 minutes, and the usage time of two towers is 10 minutes,
The individual use time is 10 minutes. In addition, the depressurization time is 5 minutes, of which 2 minutes is the pressure equalization time to pressurize other columns, and the remaining 3 minutes is the depressurization time from about 3 Kp/crI to atmospheric pressure.The pressurization time is 10 minutes. The remaining 8 minutes were a pressure equalization time in which the pressure was increased more than the rest, and the remaining 8 minutes were a pressure application time in which the pressure was increased from about 31'q/cfl to about 6 odor/1ffl using raw air.
したがって加圧に使用する原料空気の量を約半分にでき
、装置への圧力変動および原単位を改善できる。なお吸
着塔自体の負荷は従来と変りなく仕様的には同じものが
使用可能である。Therefore, the amount of raw material air used for pressurization can be approximately halved, and pressure fluctuations to the equipment and unit consumption can be improved. Note that the load on the adsorption tower itself is the same as in the past, and the same specifications can be used.
以下、本発明を具体的な実施例である第１図によって詳
細に説明する。第１図は、３塔式の例であり、ここでは
１５分毎の切替えがなされる場合について説明する。Hereinafter, the present invention will be explained in detail with reference to FIG. 1, which is a specific embodiment. FIG. 1 shows an example of a three-column type, and here, a case will be described in which switching is performed every 15 minutes.
約６ｈ／ｉに圧縮された原料空気は、入口弁ｌａ（ある
いはｌｂ、ｌｃ）より吸着剤を充填した吸着塔８ａ（あ
るいは８ｂ、８ｃ）に送られる。The raw material air compressed to about 6 h/i is sent from an inlet valve la (or lb, lc) to an adsorption tower 8a (or 8b, 8c) filled with an adsorbent.
ここで後流の深冷分離装置内で固化する水分およびＣ０
２を吸着除去し、出口弁２ａ（あるいは２ｂ。Here, water and CO solidify in the downstream cryogenic separator.
2 is adsorbed and removed, and the outlet valve 2a (or 2b) is removed by adsorption.
２ｃ）を経て精製空気として後流に送られる。なお、吸
着塔での吸着方式は圧力差スイング方式（ＰＳＡ）で行
う。一方、再生ガスとしては、後工程の深冷分離装置で
窒素、酸素やアルゴンを製品として採取した残りのほぼ
大気圧の不純窒素ガスを用い、再生ガス人口弁３ｃ（あ
るいは３ａ、３ｂ）よりＰＳＡ吸着塔８ｃ（あるいは８
ａ、ｓｂ）に送られる。ここで吸着されている水分およ
びＣ０２を脱看再生後弁４ｃ（あるいは４ａ、４ｂ）を
経て大気に放出される。一方再生が完了し、吸着圧力ま
で加圧されたＰ８に吸着塔８ｂ（あるいは８ｃ、８ａ）
は、所定の切換時間（１５分）経過後、大口弁１ｂ（あ
るいはＩｃ、ｉａＬ出口弁２ｂ（あるい＋！２ｃ、２ａ
）が開となり、Ａ塔。2c) and sent to the downstream stream as purified air. The adsorption method in the adsorption tower is a pressure differential swing method (PSA). On the other hand, as the regeneration gas, the remaining impure nitrogen gas at almost atmospheric pressure, which is obtained by collecting nitrogen, oxygen, and argon as products in the post-process cryogenic separator, is used. Adsorption tower 8c (or 8
a, sb). The moisture and CO2 adsorbed here are released into the atmosphere through the valve 4c (or 4a, 4b) after being regenerated. On the other hand, the regeneration is completed and the adsorption tower 8b (or 8c, 8a) is placed in P8 which has been pressurized to the adsorption pressure.
After the predetermined switching time (15 minutes) has passed, the large outlet valve 1b (or Ic, iaL outlet valve 2b (or +!2c, 2a)
) becomes open and A tower.
Ｂ塔の２塔を同時に吸着させる（５分間）。Ｃ塔の再生
工程が終了次第、均圧弁７ａ（あるいは７ｂ、７ｃ）を
開とし、Ａ塔とＣ塔を約３Ｋｑ／ｉに均圧する（２分間
）。均圧後Ａ塔は、脱圧弁６ａ（あるいは６ｂ、ｓｃ）
を開とし、塔内を大気圧まで脱圧後、つぎの再生工程に
そなえ、一方Ｃ塔は、加圧弁５ｃ（あるいはｓａ、ｓｂ
）により約６ Ｋ９／ｄまで加圧される。この加圧工程
時のガス量は、加圧ガス量調節計９で調節し、装置の圧
力変動を最小に抑九る。なおこの均圧および脱圧工程時
の再生ガスが流れない工程では、深冷分離装置より連続
して排出される不純窒素ガスを圧力調節計１０により調
節して、弁１１により大気放出される。以上の工程は、
第３図に示した切換チャートの如く順次各基について進
められる。Adsorb the two towers of B tower at the same time (5 minutes). As soon as the regeneration process of the C tower is completed, the pressure equalization valve 7a (or 7b, 7c) is opened to equalize the pressure of the A tower and the C tower to about 3 Kq/i (for 2 minutes). After pressure equalization, the A tower is operated by pressure relief valve 6a (or 6b, sc)
After opening the column and depressurizing the inside of the column to atmospheric pressure, the column is prepared for the next regeneration step.
) to approximately 6 K9/d. The amount of gas during this pressurization step is adjusted by a pressurized gas amount controller 9 to minimize pressure fluctuations in the apparatus. Note that in the pressure equalization and depressurization steps in which the regeneration gas does not flow, the impure nitrogen gas continuously discharged from the cryogenic separator is regulated by the pressure regulator 10 and released into the atmosphere by the valve 11. The above process is
The switching is performed sequentially for each group as shown in the switching chart shown in FIG.
以上に述べたように各塔出口と他塔入口とを連通する導
管と、各導管途中に均圧弁７ａ＋７ｂ。As described above, there are conduits that communicate the outlet of each column with the inlet of another column, and pressure equalization valves 7a and 7b in the middle of each conduit.
７Ｃとを設けたこと着こより、従来加圧工程で０→６
Ｋｑ ／ ｃｒｄの昇圧を１０分間で行っていたのを、
３→６す／ｃｒＩｌの昇圧を８分間で行えば良いことに
なる。これは原料空気ｍｆｍの割合を約６０％にできる
ことを示すすなわち（３／８ ）／（６／Ｉ Ｏ）中０
．６０となる。Since 7C was installed, the conventional pressurization process changed from 0 to 6.
Kq/crd was boosted in 10 minutes, but
It is sufficient to increase the pressure from 3 to 6 s/crIl in 8 minutes. This indicates that the ratio of feed air mfm can be approximately 60%, that is, (3/8)/(6/I O) 0
．． It will be 60.
言い換えると定容量式の圧縮機の場合は、深冷分離器に
送られる精製空気量の変動を小さくでき圧力変動を小さ
くして安定した製品純度が得られることになる。さらに
付は加えると、従来この変動分を考慮して定格原空量の
６〜８チ大きめの圧縮機が必要であったのを小型化でき
ることになる。In other words, in the case of a fixed displacement compressor, it is possible to reduce fluctuations in the amount of purified air sent to the cryogenic separator, reduce pressure fluctuations, and obtain stable product purity. Furthermore, in consideration of this variation, a compressor that was 6 to 8 inches larger than the rated raw air capacity was previously required, but it is now possible to downsize the compressor.
一方、脱圧ガスを約５０チ回収することにより、従来切
換によるパージロスとして原空量の５〜７チあったロス
を半減でき、製品の原単位向上も計れた。On the other hand, by recovering approximately 50 inches of depressurized gas, the purge loss due to conventional switching, which was 5 to 7 inches of the original air volume, could be halved, and the product consumption rate could be improved.
本発明によれば、圧力変動を少なくできる。また、これ
によって、製品ガスの純度の安定化にも役立つ。更に、
パージロスを少な（できることになり、製品の原単位の
改善にもなる。According to the present invention, pressure fluctuations can be reduced. This also helps stabilize the purity of the product gas. Furthermore,
This will reduce purge loss and improve the unit consumption of the product.
第１図は本発明の一実施例のフローシートである。第２
図は従来技術のＰＳＡ切換チャートである。第３図は本
発明の一実施例におけるＰＳＡ切換チャートである。
Ｉ ａ、 ｂ、 ｃ−−−−−−空気人口弁、
２ａ、ｂ、ｃ−・・空気出口弁、３ａ、ｂ、ｃ・・・・
・・再生ガス入口弁、４ａ、ｂ、ｃ・・・・・・再生ガ
ス出口弁、５ａ、 ｂ、 ｃ・・・・・・加圧弁、
５ａ、ｂ、ｃ・・・・・・脱圧弁、７ａ、ｂ。FIG. 1 is a flow sheet of one embodiment of the present invention. Second
The figure is a conventional PSA switching chart. FIG. 3 is a PSA switching chart in one embodiment of the present invention. I a, b, c------Pneumatic valve,
2a, b, c--air outlet valve, 3a, b, c...
... Regeneration gas inlet valve, 4a, b, c ... Regeneration gas outlet valve, 5a, b, c ... Pressurization valve,
5a, b, c... pressure relief valve, 7a, b.
Claims (1)
のそれぞれの入側に入口弁と、該吸着塔のそれぞれの出
側に出口弁とを設け、該入口弁および出口弁を操作する
ことによって、原料ガスを少なくとも一つの吸着塔に供
給して、原料ガス中の水分および二酸化炭素を圧力スイ
ング方式で吸着除去するようにしたガス分離における前
処理装置において、前記おのおのの吸着塔出口と他塔の
入口または出口とを連通する導管を設けると共に、それ
ら各導管の途中に弁を設けたことを特徴とするガス分離
における前処理装置。1. It has three or more adsorption towers filled with adsorbent, and an inlet valve is provided on the inlet side of each of the adsorption towers, and an outlet valve is provided on the outlet side of each of the adsorption towers, and the inlet valve and the outlet valve are provided. In a pretreatment device for gas separation, in which a raw material gas is supplied to at least one adsorption tower and moisture and carbon dioxide in the raw material gas are adsorbed and removed by a pressure swing method, each of the adsorption towers is 1. A pretreatment device for gas separation, characterized in that a conduit is provided that communicates a column outlet with an inlet or an outlet of another column, and a valve is provided in the middle of each of these conduits.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61017941A JPH0683771B2 (en) | 1986-01-31 | 1986-01-31 | Pretreatment method for gas separation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61017941A JPH0683771B2 (en) | 1986-01-31 | 1986-01-31 | Pretreatment method for gas separation |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7259855A Division JP2644211B2 (en) | 1995-10-06 | 1995-10-06 | Pretreatment method in gas separation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62176515A true JPS62176515A (en) | 1987-08-03 |
| JPH0683771B2 JPH0683771B2 (en) | 1994-10-26 |
Family
ID=11957803
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61017941A Expired - Lifetime JPH0683771B2 (en) | 1986-01-31 | 1986-01-31 | Pretreatment method for gas separation |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0683771B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7031442B1 (en) | 1997-02-10 | 2006-04-18 | Genesys Telecommunications Laboratories, Inc. | Methods and apparatus for personal routing in computer-simulated telephony |
| US6104802A (en) | 1997-02-10 | 2000-08-15 | Genesys Telecommunications Laboratories, Inc. | In-band signaling for routing |
| US6985943B2 (en) | 1998-09-11 | 2006-01-10 | Genesys Telecommunications Laboratories, Inc. | Method and apparatus for extended management of state and interaction of a remote knowledge worker from a contact center |
| US7907598B2 (en) | 1998-02-17 | 2011-03-15 | Genesys Telecommunication Laboratories, Inc. | Method for implementing and executing communication center routing strategies represented in extensible markup language |
| US6332154B2 (en) | 1998-09-11 | 2001-12-18 | Genesys Telecommunications Laboratories, Inc. | Method and apparatus for providing media-independent self-help modules within a multimedia communication-center customer interface |
| US9008075B2 (en) | 2005-12-22 | 2015-04-14 | Genesys Telecommunications Laboratories, Inc. | System and methods for improving interaction routing performance |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52122273A (en) * | 1976-02-27 | 1977-10-14 | Boc Ltd | Method and apparatus for increasing ratio of ingredient gas |
| JPS5528725A (en) * | 1978-08-22 | 1980-02-29 | Murakami Masako | Recovery method of oil floating on water surface |
| JPS5595079A (en) * | 1979-01-10 | 1980-07-18 | Hitachi Ltd | Method and device for previously treating air separator |
| JPS5750722A (en) * | 1980-09-05 | 1982-03-25 | Ranco Inc | Snap operating switch |
| JPS5813510A (en) * | 1981-06-25 | 1983-01-26 | ドクタ− レンチユラ アルツナイミツテル ゲ−エムベ−ハ− ウント コンパニ− | Solid medicine for oral administration |
| JPS60239310A (en) * | 1984-05-14 | 1985-11-28 | Nippon Steel Corp | Process for recovering argon from smelting waste gas using argon-oxygen mixture |
-
1986
- 1986-01-31 JP JP61017941A patent/JPH0683771B2/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52122273A (en) * | 1976-02-27 | 1977-10-14 | Boc Ltd | Method and apparatus for increasing ratio of ingredient gas |
| JPS5528725A (en) * | 1978-08-22 | 1980-02-29 | Murakami Masako | Recovery method of oil floating on water surface |
| JPS5595079A (en) * | 1979-01-10 | 1980-07-18 | Hitachi Ltd | Method and device for previously treating air separator |
| JPS5750722A (en) * | 1980-09-05 | 1982-03-25 | Ranco Inc | Snap operating switch |
| JPS5813510A (en) * | 1981-06-25 | 1983-01-26 | ドクタ− レンチユラ アルツナイミツテル ゲ−エムベ−ハ− ウント コンパニ− | Solid medicine for oral administration |
| JPS60239310A (en) * | 1984-05-14 | 1985-11-28 | Nippon Steel Corp | Process for recovering argon from smelting waste gas using argon-oxygen mixture |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0683771B2 (en) | 1994-10-26 |
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