JPH0111700Y2 - - Google Patents
Info
- Publication number
- JPH0111700Y2 JPH0111700Y2 JP1982087434U JP8743482U JPH0111700Y2 JP H0111700 Y2 JPH0111700 Y2 JP H0111700Y2 JP 1982087434 U JP1982087434 U JP 1982087434U JP 8743482 U JP8743482 U JP 8743482U JP H0111700 Y2 JPH0111700 Y2 JP H0111700Y2
- Authority
- JP
- Japan
- Prior art keywords
- absorption
- gas
- line
- separation
- liquid
- 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
- 238000010521 absorption reaction Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000003795 desorption Methods 0.000 claims description 11
- GNOIPBMMFNIUFM-UHFFFAOYSA-N hexamethylphosphoric triamide Chemical compound CN(C)P(=O)(N(C)C)N(C)C GNOIPBMMFNIUFM-UHFFFAOYSA-N 0.000 claims description 10
- 229910021591 Copper(I) chloride Inorganic materials 0.000 claims description 9
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 claims description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 229940045803 cuprous chloride Drugs 0.000 claims description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 27
- 239000007789 gas Substances 0.000 description 23
- 238000000034 method Methods 0.000 description 13
- 239000000243 solution Substances 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- XVDBWWRIXBMVJV-UHFFFAOYSA-N n-[bis(dimethylamino)phosphanyl]-n-methylmethanamine Chemical compound CN(C)P(N(C)C)N(C)C XVDBWWRIXBMVJV-UHFFFAOYSA-N 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Landscapes
- Gas Separation By Absorption (AREA)
- Carbon And Carbon Compounds (AREA)
Description
【考案の詳細な説明】
本考案は、一酸化炭素（以下COと記す）の分
離・濃縮装置に係り、特にCOの吸収液を安定に
循環使用するに好適な装置に関する。[Detailed Description of the Invention] The present invention relates to a device for separating and concentrating carbon monoxide (hereinafter referred to as CO), and particularly to a device suitable for stably circulating and using a CO absorption liquid.
化学工業や製鉄工業等において、合成化学用原
料ガスの製造あるいは省エネルギのために、例え
ばプロセス排ガスからCOを分離、濃縮して回収
することが大きな技術的課題になつている。 In the chemical industry, steel industry, etc., separating, concentrating, and recovering CO from process exhaust gas, for example, has become a major technical issue in order to produce raw material gas for synthetic chemicals or to save energy.
COを含有するガス源からCOを分離、濃縮する
方法には、現在、第一銅塩の溶液等の吸収液を使
用する吸収法、およびそれとは原理的に異る深冷
分離法が知られている。後者の深冷分離法は、複
雑な冷却、熱回収システムから構成されており、
操作温度が低温であるため、装置材料として高価
なものを使用する必要があり、また低温を得るた
めに、動力消費量が大きくなるという欠点があ
る。 At present, methods for separating and concentrating CO from a gas source containing CO include an absorption method that uses an absorption liquid such as a cuprous salt solution, and a cryogenic separation method that is fundamentally different from that method. ing. The latter cryogenic separation method consists of a complex cooling and heat recovery system.
Since the operating temperature is low, it is necessary to use expensive equipment materials, and there is also the disadvantage that power consumption is large in order to obtain the low temperature.
一方、吸収法に使用されるCO吸収液としては、
従来、アンモニア性第一銅水溶液または、塩酸性
第一銅塩水溶液が用いられてきた。 On the other hand, the CO absorption liquid used in the absorption method is
Conventionally, an ammoniacal cuprous aqueous solution or a hydrochloric acidic cuprous salt aqueous solution has been used.
しかし、いずれも水溶液単位体積あたりのCO
吸収量が小さいという問題があつた。これに対し
本考案者らは、塩化第一銅（以下CuClと記す）
をトリスジメチルアミノホスフインオキシド（以
下HMPAと記す）に溶解せしめた、CO吸収量の
高い吸収液を開発した（特願昭55−92607号）。こ
の吸収液は単位体積あたりのCO吸収量が水溶液
系のものに較べて非常に高く、実際のプロセスの
適用時には、種々の利点がある。しかし、上記の
吸収液において、水分を含む分離対象ガスと接触
させ、COを吸収せしめた場合、同時にH2Oも吸
収し、そのまま循環使用すると、液中のH2O濃
度が増加してついにはCuClが不溶化するという
問題がある。 However, in both cases, CO per unit volume of aqueous solution
There was a problem that the amount of absorption was small. In contrast, the inventors of the present invention have discovered that cuprous chloride (hereinafter referred to as CuCl)
We have developed an absorbent solution with high CO absorption capacity, which is obtained by dissolving CO in trisdimethylaminophosphine oxide (hereinafter referred to as HMPA) (Japanese Patent Application No. 1983-92607). This absorption liquid has a much higher CO absorption amount per unit volume than an aqueous solution, and has various advantages when applied to actual processes. However, when the above-mentioned absorption liquid is brought into contact with a gas to be separated containing moisture and is allowed to absorb CO, it also absorbs H 2 O at the same time, and if it is recycled as it is, the H 2 O concentration in the liquid increases and eventually There is a problem that CuCl becomes insolubilized.
本考案の目的は、上記したCO吸収量が高く、
しかも吸収速度が速い、CuClをHMPAに溶解せ
しめ、さらにトルエンで希釈したCO吸収液（以
下CuCl・HMPA／トルエン液と記す）を用いた
CO分離・濃縮プロセスにおいて、長期間安定に
運転することができる装置を提供するにある。 The purpose of this invention is to achieve the above-mentioned high CO absorption capacity.
Furthermore, we used a CO absorption solution (hereinafter referred to as CuCl/HMPA/toluene solution), which has a fast absorption rate and is made by dissolving CuCl in HMPA and diluting it with toluene.
The purpose of the present invention is to provide a device that can operate stably for a long period of time in a CO separation/concentration process.
本考案は、（一酸化炭素を含有するガスを、塩
化第一銅とトリス（ジメチルアミノ）ホスフイン
オキシド（ヘキサメチルホスホルトリアミド）を
含む吸収液で処理し、高純度のCOを回収する装
置において、脱離塔３後流に、水分離装置６を設
けることを特徴とする一酸化炭素の分離・濃縮装
置。）、である。 The present invention is a device that recovers high-purity CO by treating gas containing carbon monoxide with an absorption liquid containing cuprous chloride and tris(dimethylamino)phosphine oxide (hexamethylphosphortriamide). , a carbon monoxide separation/concentration device characterized in that a water separation device 6 is provided downstream of the desorption column 3.
要するに、本考案は、CuCl・HMPA／トルエ
ン系吸収液を用いたCO分離・濃縮プロセスにお
いて、脱離塔後流に水分離装置を設けることを特
徴とする装置である。 In short, the present invention is an apparatus characterized by providing a water separation device downstream of a desorption column in a CO separation/concentration process using a CuCl/HMPA/toluene-based absorption liquid.
以下、本考案を原理的なフローシートをもつて
詳細に説明する。 Hereinafter, the present invention will be explained in detail using a basic flow sheet.
第１図は、従来のCO分離、濃縮プロセスの原
理的なフローシートである。図において、COお
よびH2O含有ガスは必要に応じて前処理装置１
で前処理され、原料ガスライン１１を通じ吸収塔
２に入り、吸収塔内の吸収液と接触し、COが吸
収される。この時、ガス中の一部のH2Oは、液
中に吸収され、移行する。 Figure 1 is a basic flow sheet for the conventional CO separation and concentration process. In the figure, CO and H 2 O containing gases are
It enters the absorption tower 2 through the raw material gas line 11, comes into contact with the absorption liquid in the absorption tower, and absorbs CO. At this time, some H 2 O in the gas is absorbed into the liquid and transferred.
吸収塔排ガスは、飛沫同伴成分を適宜除去され
たのち、排ガスライン２１を通じ大気中に放出さ
れる。一方、COおよびH2Oを吸収した液は、リ
ツチ溶液ライン３１から熱交換器４をへて脱離塔
３に送られ、ここで昇温又は減圧されることによ
りCOを放散する。しかし分離塔からの放散ガス
ライン４１中には、CO以外に、H2O，HMPAお
よびトルエンの蒸気が共存するため、ガス冷却器
５でそれらの蒸気を冷却、循環ライン７１を通じ
て脱離塔下部へリサイクルする。H2O，HMPA
およびトルエン蒸気を除去した高濃度COガスは、
ガスライン４１をへて回収され、製品ガスとな
る。一方COを放散した液はリーン溶液ライン５
１を通じ吸収塔へもどされ循環使用される。この
ような従来の方法では、脱離塔からの放散ガス中
のH2Oが、再び液中にリサイクルされるため、
液中のH2O濃度が経時的に上昇し、ついには
CuClが沈殿し、CO吸収量の低下をもたらす。 The absorption tower exhaust gas is discharged into the atmosphere through the exhaust gas line 21 after the entrained components are appropriately removed. On the other hand, the liquid that has absorbed CO and H 2 O is sent from the rich solution line 31 through the heat exchanger 4 to the desorption tower 3, where it is heated or depressurized to release CO. However, in addition to CO, H 2 O, HMPA, and toluene vapors coexist in the desorption gas line 41 from the separation tower, so these vapors are cooled in the gas cooler 5 and passed through the circulation line 71 to the lower part of the desorption tower. Recycle to. H2O ，HMPA
and high concentration CO gas from which toluene vapor has been removed.
The gas is recovered through the gas line 41 and becomes a product gas. On the other hand, the liquid from which CO has been released is the lean solution line 5.
1 and returned to the absorption tower for circulation. In such conventional methods, H 2 O in the gas released from the desorption tower is recycled back into the liquid.
The H 2 O concentration in the liquid increases over time, and eventually
CuCl precipitates, resulting in a decrease in CO absorption.
第２図に、本考案に基く、CO分離・濃縮プロ
セスの原理的なフローシートを示した。 Figure 2 shows a basic flow sheet for the CO separation and concentration process based on the present invention.
脱離塔後流の循環ライン７１に、水分離装置６
を設置したことが特徴である。即ち、ガス冷却器
５からのH2O，HMPAおよびトルエンは、循環
ライン７１を通じて水分離装置６に入り、水が分
離され、HMPAおよびトルエンのみが、循環ラ
イン８１を通じ脱離塔下部へリサイクルされる。
分離されたH2Oは、水ライン９１をへて系外へ
除去される。これにより、循環液中でのH2Oの
蓄積はなくなり、長期にわたり安定に運転するこ
とが可能になる。なお、水分離装置としては、ト
ルエンと水が溶け合わないことによる比重差を利
用する方法、あるいはモレキユラーシーブ、活性
炭等を用いた吸着法等、原理的に水とトルエンを
分離する公知の装置で充分である。 A water separator 6 is installed in the circulation line 71 downstream of the desorption tower.
It is characterized by the fact that it has been installed. That is, H 2 O, HMPA, and toluene from the gas cooler 5 enter the water separator 6 through the circulation line 71, water is separated, and only HMPA and toluene are recycled to the lower part of the desorption tower through the circulation line 81. Ru.
The separated H 2 O is removed from the system through a water line 91. This eliminates the accumulation of H 2 O in the circulating fluid, making it possible to operate stably over a long period of time. In addition, as a water separation device, there are known methods that can separate water and toluene in principle, such as a method that utilizes the difference in specific gravity due to the incompatibility of toluene and water, or an adsorption method that uses molecular sieves, activated carbon, etc. The equipment is sufficient.
本考案によれば、吸収液中に水が吸収されその
濃度が増加する現象を防止でき、水分による吸収
液の能力低下を防止しつつ、効率良くCOを分離
濃縮することができる。 According to the present invention, it is possible to prevent the phenomenon in which water is absorbed into the absorption liquid and its concentration increases, and it is possible to efficiently separate and concentrate CO while preventing the capacity of the absorption liquid from decreasing due to moisture.
第１図は、従来のCOの分離、濃縮システムを
示すフローシートであり、第２図は本考案の実施
例を示す原理的なフローシートである。
１……前処理装置、２……吸収塔、３……脱離
塔、５……ガス冷却器、６……水分離装置、１１
……ガス供給ライン、２１……排ガスライイン、
３１……リツチ溶液ライン、４１……脱離塔出口
ガスライン、５１……リーン溶液ライン、６１…
…製品COガスライン、７１……循環ライン(1)、
８１……循環ライン(2)、９１……水ライン。
FIG. 1 is a flow sheet showing a conventional CO separation and concentration system, and FIG. 2 is a principle flow sheet showing an embodiment of the present invention. 1... Pretreatment device, 2... Absorption tower, 3... Desorption tower, 5... Gas cooler, 6... Water separation device, 11
...Gas supply line, 21...Exhaust gas line,
31... Rich solution line, 41... Desorption column outlet gas line, 51... Lean solution line, 61...
...Product CO gas line, 71...Circulation line (1),
81...Circulation line (2), 91...Water line.
Claims (1)
リス（ジメチルアミノ）ホスフインオキシド（ヘ
キサメチルホスホルトリアミド）を含む吸収液で
処理し、高純度のCOを回収する装置において、
脱離塔３後流に、水分離装置６を設けることを特
徴とする一酸化炭素の分離・濃縮装置。 In an apparatus that recovers high-purity CO by treating gas containing carbon monoxide with an absorption liquid containing cuprous chloride and tris(dimethylamino)phosphine oxide (hexamethylphosphortriamide),
A carbon monoxide separation/concentration device characterized in that a water separation device 6 is provided downstream of a desorption column 3.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1982087434U JPS58189138U (en) | 1982-06-14 | 1982-06-14 | Carbon monoxide separation/concentration equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1982087434U JPS58189138U (en) | 1982-06-14 | 1982-06-14 | Carbon monoxide separation/concentration equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58189138U JPS58189138U (en) | 1983-12-15 |
| JPH0111700Y2 true JPH0111700Y2 (en) | 1989-04-06 |
Family
ID=30096151
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1982087434U Granted JPS58189138U (en) | 1982-06-14 | 1982-06-14 | Carbon monoxide separation/concentration equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58189138U (en) |
-
1982
- 1982-06-14 JP JP1982087434U patent/JPS58189138U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58189138U (en) | 1983-12-15 |
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