JPS6247059B2 - - Google Patents
Info
- Publication number
- JPS6247059B2 JPS6247059B2 JP55021710A JP2171080A JPS6247059B2 JP S6247059 B2 JPS6247059 B2 JP S6247059B2 JP 55021710 A JP55021710 A JP 55021710A JP 2171080 A JP2171080 A JP 2171080A JP S6247059 B2 JPS6247059 B2 JP S6247059B2
- Authority
- JP
- Japan
- Prior art keywords
- absorption
- absorption liquid
- absorbed
- liquid
- amount
- 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 64
- 239000007788 liquid Substances 0.000 claims description 43
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 claims description 18
- 229910021591 Copper(I) chloride Inorganic materials 0.000 claims description 13
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 claims description 13
- 229940045803 cuprous chloride Drugs 0.000 claims description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 229910021551 Vanadium(III) chloride Inorganic materials 0.000 claims description 4
- HQYCOEXWFMFWLR-UHFFFAOYSA-K vanadium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[V+3] HQYCOEXWFMFWLR-UHFFFAOYSA-K 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 22
- 238000000926 separation method Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 239000000243 solution Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 239000012456 homogeneous solution Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000004094 surface-active agent Substances 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Description
【発明の詳細な説明】
本発明は、一酸化炭素（以下、COと記す）の
吸収液に関し、さらに詳しくはCOを含有する各
種ガス源からCOを分離、濃縮して回収するため
の吸収液に関する。[Detailed Description of the Invention] The present invention relates to an absorption liquid for carbon monoxide (hereinafter referred to as CO), and more specifically, an absorption liquid for separating, concentrating, and recovering CO from various gas sources containing CO. Regarding.
化学工業や製鉄工業等において、合成用原料ガ
スの製造または省エネルギといつた考えのもと
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となつてい
る。 In the chemical industry, steel industry, etc., separating, concentrating, and recovering CO from process exhaust gas has become a major technical challenge, with the aim of producing raw material gas for synthesis or saving 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１銅塩の溶液等の吸収液を使
用する吸収液法、およびこ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。 Currently, methods for separating and concentrating CO from a gas source containing CO include the absorption liquid method, which uses an absorption liquid such as a solution of cuprous salt, and the cryogenic separation method, which is fundamentally different from this method. Are known. The latter cryogenic separation method is
It consists of a complex cooling and heat recovery system, and because the operating temperature is low, it is necessary to use expensive equipment materials, and it also has the disadvantage of increasing power consumption to obtain the low temperature. be.
一方、吸収液法に使用されるCO吸収液として
は、従来アンモニア性第１銅塩水溶液または塩酸
性第１銅塩水溶液が用いられてきたが、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。これらの吸収液において
は、CO吸収に直接関与する一価の銅を溶液中に
可溶化させるために、クロロ錯体あるいはアンミ
ン錯体を形成させているものと考えられる。また
最近、塩化第１銅（以下、CuClと記す）と無水
塩化アルミニウム（以下、AlCl3と記す）の錯体
（CuAlCl4）をトルエンに溶解せしめたCO吸収液
が開発され、注目をあつめている。この吸収液は
溶液単位体積あたりのCO吸収量が水溶液系のも
のに較べて非常に高いという特長を有する。この
ため実際のCO分離、濃縮プロセスに適用する場
合、吸収塔における操作で高圧、低温を必要とせ
ず、常温、常圧で運転が可能なため、装置に耐圧
材料等を必要としないこと、およびCOの吸収負
荷が大きいため、溶液循環量が小さくて済むなど
の利点を有している。しかし、上記のような吸収
液は、その構成成分であるAlCl3が水または水蒸
気と接触して定量的に加水分解を受け、それに伴
いCO吸収量も低下するという問題がある。 On the other hand, as the CO absorption liquid used in the absorption liquid method, an ammoniacal cuprous salt aqueous solution or a hydrochloric acidic cuprous salt aqueous solution has conventionally been used, but in either case, the amount of CO absorbed per unit volume of the aqueous solution is The problem was that it was small. In these absorption solutions, it is thought that a chloro complex or ammine complex is formed in order to solubilize monovalent copper, which is directly involved in CO absorption, in the solution. Recently, a CO absorbing liquid in which a complex (CuAlCl 4 ) of cuprous chloride (hereinafter referred to as CuCl) and anhydrous aluminum chloride (hereinafter referred to as AlCl 3 ) is dissolved in toluene has been developed and is attracting attention. . This absorption liquid has a feature that the amount of CO absorbed per unit volume of solution is much higher than that of aqueous solutions. Therefore, when applied to actual CO separation and concentration processes, the absorption tower does not require high pressure or low temperature, and can be operated at room temperature and pressure, so the equipment does not require pressure-resistant materials, etc. Since the CO absorption load is large, it has the advantage of requiring only a small amount of solution circulation. However, the above absorption liquid has a problem in that its constituent AlCl 3 comes into contact with water or steam and undergoes quantitative hydrolysis, resulting in a corresponding decrease in the amount of CO absorbed.
本発明の目的は、水または水蒸気と接触しても
加水分解を受けにくく、高い一酸化炭素吸収性能
を維持する吸収液を提供することにある。 An object of the present invention is to provide an absorption liquid that is resistant to hydrolysis even when it comes into contact with water or steam and maintains high carbon monoxide absorption performance.
上記目的を達成するため、本発明の吸収液は、
塩化第１銅とジメチルスルホキシドとを含むこと
を特徴とする。 In order to achieve the above object, the absorption liquid of the present invention is
It is characterized by containing cuprous chloride and dimethyl sulfoxide.
本発明の吸収液はスラリ、均一溶液のいずれの
状態でも使用可能であるが、操作の容易性という
観点からは均一溶液の方が好ましい。吸収液中の
塩化第１銅等の分散性を改善するために、本発明
においては前記成分にさらに三塩化バナジウムを
添加することが望ましい。 The absorption liquid of the present invention can be used in either the form of a slurry or a homogeneous solution, but a homogeneous solution is preferable from the viewpoint of ease of operation. In order to improve the dispersibility of cuprous chloride and the like in the absorption liquid, it is desirable in the present invention to further add vanadium trichloride to the above components.
上記各成分の構成比は、塩化第１銅およびジメ
チルスルホキシドからなる系では、塩化第１銅：
ジメチルスルホキシドのモル比で１：４〜60の範
囲が適当であり、特に１：６〜25の範囲が好まし
い。 In the system consisting of cuprous chloride and dimethyl sulfoxide, the composition ratio of each of the above components is cuprous chloride:
The molar ratio of dimethyl sulfoxide is suitably in the range of 1:4 to 60, particularly preferably in the range of 1:6 to 25.
三塩化バナジウムを含む系の構成比では、塩化
第１銅：三塩化バナジウム：ジメチルスルホキシ
ドのモル比で１：0.01〜0.5：４〜60の範囲が適
当であり、特に１：0.02〜0.2：６〜25の範囲が
好ましい。 Regarding the composition ratio of the system containing vanadium trichloride, the molar ratio of cuprous chloride: vanadium trichloride: dimethyl sulfoxide is suitably in the range of 1:0.01 to 0.5:4 to 60, particularly 1:0.02 to 0.2:6. A range of ~25 is preferred.
本発明において、吸収液中の各成分の分散性を
向上させるために適当な界面活性剤などを添加す
ることができる。本発明の構成成分の選択に当つ
ては、吸収液の粘度が小さく、安定性がよいこ
と、また構成成分がCO含有ガスと接触する際、
またはCOを分離する際に系外に揮散しないもの
であることが好ましい。 In the present invention, a suitable surfactant or the like may be added to improve the dispersibility of each component in the absorption liquid. When selecting the components of the present invention, it is important that the absorption liquid has low viscosity and good stability, and that when the components come into contact with CO-containing gas,
Alternatively, it is preferable that it not volatilize out of the system when CO is separated.
次に、本発明の吸収液を使用してCO含有ガス
中のCOを吸収分離し、濃縮COとして回収する際
の操作条件について説明する。 Next, operating conditions for absorbing and separating CO in a CO-containing gas using the absorption liquid of the present invention and recovering it as concentrated CO will be described.
第１図は、本発明の吸収液を用いたCOの分
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が選択的に吸収される。吸収塔排ガス
は、飛洙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を吸収した液は、吸収ライン３１から熱交換
器４をへて分離塔３に送られ、ここで昇温または
減圧されることにより、COを放散する。分離塔
からの排ガスは高濃度のCOを含有するが、飛洙
同伴成分を除去した後、ガスライン４１をへて回
収され、製品ガスとなる。COを分離した吸収液
は、ライン５１から吸収塔２にもどり循環使用さ
れる。 FIG. 1 is a basic flow sheet of the CO separation and concentration process using the absorption liquid of the present invention. In the figure, CO-containing gas is pretreated in a pretreatment device 1 as necessary, and a raw material gas line 11
, enters the absorption tower 2, contacts the absorption liquid in the absorption tower, and CO is selectively absorbed. The absorption tower exhaust gas is discharged into the atmosphere through the exhaust gas line 21 after the components entrained in the air are appropriately removed. on the other hand,
The liquid that has absorbed CO is sent from the absorption line 31 through the heat exchanger 4 to the separation column 3, where it is heated or depressurized to release CO. The exhaust gas from the separation tower contains a high concentration of CO, but after removing the components entrained in the air, it is recovered through the gas line 41 and becomes a product gas. The absorption liquid from which CO has been separated is returned to the absorption tower 2 through the line 51 and is used for circulation.
本発明の吸収液を、実際のCO濃縮、分離プロ
セスに適用する場合の操作温度および圧力は、
CO含有ガス中のCO含有割合、接触時間、吸収液
の組成等に応じて変化することができる。一般に
吸収温度を低下させるとCO吸収量は増加する
が、低温生成のための冷却装置が必要となり、ま
た吸収液の粘度が増加し、時には吸収液が凝固す
ることがある。一方、吸収温度を余り高くすると
CO吸収量が小さくなる。上記の点から吸収温度
は一般に10〜80℃とすることが好ましい。さらに
吸収圧力は高い方がCO吸収量が大きくなり、ま
た吸収速度も高くなるが、ガスの圧縮機が必要に
なり、さらに装置を耐圧構造にせねばならず、建
設費が高くなる。このような点から、吸収圧力
は、一般にゲージ圧で０〜20Kg／cm2とすることが
好ましい。 The operating temperature and pressure when applying the absorption liquid of the present invention to the actual CO concentration and separation process are as follows:
It can be changed depending on the CO content rate in the CO-containing gas, the contact time, the composition of the absorption liquid, etc. In general, lowering the absorption temperature increases the amount of CO absorbed, but requires a cooling device for low-temperature production, increases the viscosity of the absorption liquid, and sometimes causes the absorption liquid to solidify. On the other hand, if the absorption temperature is too high,
The amount of CO absorbed becomes smaller. In view of the above, the absorption temperature is generally preferably 10 to 80°C. Furthermore, the higher the absorption pressure, the greater the amount of CO absorbed and the faster the absorption rate, but a gas compressor is required, and the equipment must also have a pressure-resistant structure, which increases construction costs. From this point of view, the absorption pressure is generally preferably 0 to 20 kg/cm 2 in gauge pressure.
COを吸収した吸収液は、吸収温度よりも温度
を上げ、もしくは圧力を下げることにより、また
は不活性の媒体（例えば水蒸気、ベンゼン蒸気
等）と接触させることにより、さらにはCOの用
途によつては水素ガス等と接触させることによ
り、COを放散し、再生される。上記放散の操作
は単独でも組合せて行つてもよい。放散された
COを捕集すれば濃縮COガスを得ることができる
が、これらのガスは燃料または化学合成用原料ガ
スとして有効に使用される。 The absorption liquid that has absorbed CO can be prepared by raising the temperature or lowering the pressure above the absorption temperature, or by contacting it with an inert medium (e.g. water vapor, benzene vapor, etc.), or depending on the use of CO. By contacting with hydrogen gas etc., CO is released and regenerated. The above-mentioned dispersion operations may be performed alone or in combination. dissipated
By collecting CO, concentrated CO gas can be obtained, and these gases are effectively used as fuel or raw material gas for chemical synthesis.
以下、本発明を実施例により更に詳細に説明す
る。なお、実施例中のガスの体積はいずれも標準
状態（０℃、1atm）の値である。 Hereinafter, the present invention will be explained in more detail with reference to Examples. Note that the volumes of gases in the examples are all values under standard conditions (0° C., 1 atm).
実施例 １
容積100mlの円筒状ガラス容器に、CuClを9.90
ｇ（0.1モル）採取し、ジメチルスルホキシドを
55.0ｇ（0.7モル）添加した後、80℃で３時間加
熱したところ、スラリ状の溶液が得られた。この
溶液を30℃に冷却したのち、同温度に保ちなが
ら、CO20％、N280％（容量％）からなる組成の
ガスを常圧で連続的に吹き込み、本条件下での
COの平衡吸収量を求めた。その結果、本吸収液
は１ml当たり8.9mlのCOを吸収した。比較のため
に、CuCl9.9ｇ（0.1モル）を8NHCl水溶液50mlに
溶解させたもの（従来の塩酸酸性第１銅溶液）の
同一条件下におけるCO平衡吸収量を求めたとこ
ろ、吸収液１ml当たり4.5mlのCOを吸収するにす
ぎなかつた。Example 1 9.90 ml of CuCl was placed in a cylindrical glass container with a volume of 100 ml.
g (0.1 mol) was collected and dimethyl sulfoxide was added.
After adding 55.0 g (0.7 mol), heating was performed at 80° C. for 3 hours, and a slurry-like solution was obtained. After cooling this solution to 30℃, while keeping it at the same temperature, a gas consisting of 20% CO and 80% N2 (volume %) was continuously blown in at normal pressure.
The equilibrium absorption amount of CO was determined. As a result, this absorption liquid absorbed 8.9 ml of CO per 1 ml. For comparison, we calculated the equilibrium CO absorption amount under the same conditions for 9.9 g (0.1 mol) of CuCl dissolved in 50 ml of 8NHCl aqueous solution (conventional acidic cuprous solution of hydrochloric acid), and found that it was 4.5 per ml of absorption liquid. ml of CO was absorbed.
実施例 ２
容積100mlの円筒状ガラス容器に、CuClを4.45
ｇ（0.1モル）採取し、これにジメチルスルホキ
シドを55.0ｇ（0.7モル）添加したのち、80℃で
３時間加熱した。次にこれを30℃に冷却したの
ち、実施例１と同一条件でCO平衡吸収量を測定
したところ、吸収液１ml当たり5.8mlのCOを吸収
した。Example 2 4.45 ml of CuCl was placed in a cylindrical glass container with a volume of 100 ml.
After adding 55.0 g (0.7 mol) of dimethyl sulfoxide to this, it was heated at 80° C. for 3 hours. Next, after cooling this to 30° C., the CO equilibrium absorption amount was measured under the same conditions as in Example 1, and 5.8 ml of CO was absorbed per 1 ml of absorption liquid.
実施例 ３
実施例１で得られた、平衡量のCOを吸収した
液を100℃に加熱し、50mmHgの減圧状態にしたと
ころ、吸収液１ml当たり、8.7mlのCOが回収され
た。Example 3 When the liquid obtained in Example 1 that had absorbed an equilibrium amount of CO was heated to 100°C and reduced to 50 mmHg, 8.7 ml of CO was recovered per 1 ml of the absorbed liquid.
実施例 ４
容積100mlの円筒状ガラス容器に、CuClを9.90
ｇ（0.1モル）を採取し、ジメチルスルホキシド
を5.50ｇ（0.7モル）添加し、さらにこれにVCl3
を1.17ｇ（0.0075モル）添加したところ、緑色の
均一溶液が得られた。この吸収液について、実施
例１と同一条件でCO平衡吸収量を測定したとこ
ろ、吸収液１ml当たり12.8mlのCOを吸収した。Example 4 CuCl was added at 9.90 ml in a cylindrical glass container with a volume of 100 ml.
g (0.1 mol) was collected, 5.50 g (0.7 mol) of dimethyl sulfoxide was added, and VCl 3
When 1.17 g (0.0075 mol) of was added, a green homogeneous solution was obtained. Regarding this absorption liquid, when the CO equilibrium absorption amount was measured under the same conditions as in Example 1, 12.8 ml of CO was absorbed per 1 ml of the absorption liquid.
実施例 ５
実施例４で得られた、平衡量のCOを吸収した
液を100℃に加熱し、50mmHgの減圧状態にしたと
ころ、吸収液１ml当たり12.4mlのCOが回収され
た。Example 5 When the liquid obtained in Example 4, which had absorbed an equilibrium amount of CO, was heated to 100°C and brought to a reduced pressure of 50 mmHg, 12.4 ml of CO was recovered per ml of the absorbed liquid.
実施例 ６
実施例４で示した同一組成の吸収液を新たに調
整し、これに２％（容量％）の水を添加した後、
30℃にて24時間放置した。その後、実施例１と同
一条件でCO平衡吸収量を測定した。その結果、
吸収液１ml当たり12.8mlのCOを吸収し、水を添
加しても性能に全く変化がないことが分つた。Example 6 After preparing a new absorption liquid with the same composition as shown in Example 4 and adding 2% (volume %) of water to it,
It was left at 30°C for 24 hours. Thereafter, the CO equilibrium absorption amount was measured under the same conditions as in Example 1. the result,
It was found that 12.8 ml of CO was absorbed per ml of absorption liquid, and there was no change in performance even when water was added.
実施例 ７
容積100mlの円筒状ガラス容器に、CuClを9.90
ｇ（0.1モル）採取し、ジメチルスルホキシドを
55.0ｇ（0.7モル）添加し、さらにこれにVCl3を
4.68ｇ（0.03モル）添加したところ、実施例４と
同様に緑色の均一溶液が得られた。この吸収液に
関し、実施例１と同一条件でCO平衡吸収量を測
定したところ、吸収液１ml当たり8.7mlのCOを吸
収した。Example 7 9.90% CuCl was added to a cylindrical glass container with a volume of 100ml.
g (0.1 mol) was collected and dimethyl sulfoxide was added.
Added 55.0g (0.7mol) and further added VCl 3 to this.
When 4.68 g (0.03 mol) was added, a green homogeneous solution was obtained as in Example 4. Regarding this absorption liquid, when the CO equilibrium absorption amount was measured under the same conditions as in Example 1, 8.7 ml of CO was absorbed per 1 ml of the absorption liquid.
以上、本発明によれば、COを含有する各種の
ガス源からCOを効率良くかつ安定して分離、濃
縮することができる。すなわち、本発明の吸収液
は水に対して安定で、しかもCO吸収量が非常に
高いため、従来のように水分除去のための前処理
が不要になり、また吸収塔の操作で高圧、低温を
必要とせず、常圧、常温で運転することができ
る。しかもCO吸収負荷を大きくとることができ
るため、溶液循環量が小さくて済み、効率および
経済性の高いCO分離、濃縮プロセスとすること
ができる。 As described above, according to the present invention, CO can be efficiently and stably separated and concentrated from various gas sources containing CO. In other words, the absorption liquid of the present invention is stable against water and has a very high CO absorption amount, so there is no need for pretreatment to remove water as in the past, and the absorption tower can be operated at high pressure and low temperature. It can be operated at normal pressure and temperature. Furthermore, since the CO absorption load can be increased, the amount of solution circulation can be small, making it possible to achieve a highly efficient and economical CO separation and concentration process.
第１図は、本発明の吸収液を用いた一酸化炭素
分離、濃縮プロセスの一実施例を示すフローシー
トである。
２……吸収塔、３……分離塔、４……熱交換
器、１１……ガス供給ライン。
FIG. 1 is a flow sheet showing an example of a carbon monoxide separation and concentration process using the absorption liquid of the present invention. 2... Absorption tower, 3... Separation tower, 4... Heat exchanger, 11... Gas supply line.
Claims (1)
とを特徴とする一酸化炭素の吸収液。 ２ 特許請求の範囲第１項において、前記吸収液
はさらに三塩化バナジウムを含むことを特徴とす
る一酸化炭素の吸収液。[Claims] 1. A carbon monoxide absorption liquid characterized by containing cuprous chloride and dimethyl sulfoxide. 2. The carbon monoxide absorption liquid according to claim 1, wherein the absorption liquid further contains vanadium trichloride.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2171080A JPS56118722A (en) | 1980-02-25 | 1980-02-25 | Absorbent liquid for carbon monoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2171080A JPS56118722A (en) | 1980-02-25 | 1980-02-25 | Absorbent liquid for carbon monoxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56118722A JPS56118722A (en) | 1981-09-17 |
| JPS6247059B2 true JPS6247059B2 (en) | 1987-10-06 |
Family
ID=12062609
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2171080A Granted JPS56118722A (en) | 1980-02-25 | 1980-02-25 | Absorbent liquid for carbon monoxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56118722A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61268338A (en) * | 1985-05-23 | 1986-11-27 | Agency Of Ind Science & Technol | Selective separation of gas |
-
1980
- 1980-02-25 JP JP2171080A patent/JPS56118722A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56118722A (en) | 1981-09-17 |
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