JPS6354411B2 - - Google Patents
Info
- Publication number
- JPS6354411B2 JPS6354411B2 JP55122962A JP12296280A JPS6354411B2 JP S6354411 B2 JPS6354411 B2 JP S6354411B2 JP 55122962 A JP55122962 A JP 55122962A JP 12296280 A JP12296280 A JP 12296280A JP S6354411 B2 JPS6354411 B2 JP S6354411B2
- Authority
- JP
- Japan
- Prior art keywords
- absorption liquid
- boiling point
- solvent
- gas
- 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
- 239000007788 liquid Substances 0.000 claims description 64
- 238000010521 absorption reaction Methods 0.000 claims description 60
- 239000002904 solvent Substances 0.000 claims description 37
- 238000009835 boiling Methods 0.000 claims description 35
- 238000000034 method Methods 0.000 claims description 13
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 6
- 229910021591 Copper(I) chloride Inorganic materials 0.000 claims description 3
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 claims description 3
- 229940045803 cuprous chloride Drugs 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 32
- 238000003795 desorption Methods 0.000 description 9
- GNOIPBMMFNIUFM-UHFFFAOYSA-N hexamethylphosphoric triamide Chemical compound CN(C)P(=O)(N(C)C)N(C)C GNOIPBMMFNIUFM-UHFFFAOYSA-N 0.000 description 9
- 238000012856 packing Methods 0.000 description 9
- 239000000463 material Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Description
【発明の詳細な説明】
本発明は、吸収ガスの回収方法に関し、特に混
合ガス中の特定のガス成分を吸収した吸収液から
前記ガス成分を脱離させる吸収ガスの回収方法に
関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an absorption gas recovery method, and more particularly to an absorption gas recovery method in which a specific gas component in a mixed gas is desorbed from an absorption liquid that has absorbed the gas component.
従来の吸収、脱離プロセスには二酸化炭素、一
酸化炭素、硫化水素、二酸化イオウ等を対象にし
たものであるが、これらのプロセスにおける脱離
方法は、吸収液の温度を高めるか、減圧すること
により、吸収液の溶剤等を蒸発させ、吸収された
特定のガス成分を、溶剤の蒸気とともに放散させ
るものである。 Conventional absorption and desorption processes target carbon dioxide, carbon monoxide, hydrogen sulfide, sulfur dioxide, etc., but the desorption methods in these processes involve increasing the temperature of the absorption liquid or reducing the pressure. This evaporates the solvent of the absorbing liquid and dissipates the absorbed specific gas component together with the solvent vapor.
第１図は、従来の一酸化炭素の吸収、脱離プロ
セスの一例を示すフローシートである。図におい
て、一酸化炭素（以下、COと記すことがある）
を含む原料ガスはライン３から充填材層２を有す
る吸収塔１の下部に供給され、一方、吸収塔の頂
部のライン２１から吸収液が散布され、充填材層
２で原料ガスと向流触媒し、吸収液中にCOが吸
収され、一方、塔頂のライン４からは排ガスが放
出される。COを吸収した液はライン５から循環
ポンプ６により熱交換器７を通つて加熱され、さ
らにライン８を通つて放散塔９に導入され、その
頂部から充填材層１０上へ散布される。放散塔９
の降下液の全部または一部はリボイラ１１に導か
れ、ここでスチーム等の熱媒体により吸収液の一
部を蒸発させて放散塔９に戻し、充填材層１０を
上昇する過程で導管８から散布降下される液と接
触し、COを脱着温度まで加熱する。充填材層で
COの脱着温度を保持することにより吸収液中の
COが脱離され、この回収COはライン１３を通つ
てコンデンサ１４に導入され、ここで吸収液蒸気
が冷却水１５により凝縮液化し、ライン１７を通
つて放散塔９へ還流され、最終的にCOガス１６
が回収される。 FIG. 1 is a flow sheet showing an example of a conventional carbon monoxide absorption and desorption process. In the figure, carbon monoxide (hereinafter sometimes referred to as CO)
A raw material gas containing gas is supplied from a line 3 to the lower part of the absorption tower 1 having a packing material layer 2, while an absorption liquid is sprayed from a line 21 at the top of the absorption tower, and the material gas and the countercurrent catalyst are distributed in the packing material layer 2. However, CO is absorbed into the absorption liquid, while exhaust gas is released from line 4 at the top of the column. The liquid that has absorbed CO is heated through a heat exchanger 7 by a circulation pump 6 from a line 5, and further introduced into a stripping tower 9 through a line 8, and is sprayed onto the packed material bed 10 from the top thereof. Radiant tower 9
All or part of the falling liquid is led to the reboiler 11, where a part of the absorbed liquid is evaporated by a heat medium such as steam, and returned to the stripping tower 9. In the process of rising through the packing layer 10, it is removed from the conduit 8. It comes into contact with the sprayed liquid and heats the CO to its desorption temperature. with filler layer
By maintaining the CO desorption temperature,
CO is desorbed, and this recovered CO is introduced into a condenser 14 through a line 13, where the absorption liquid vapor is condensed into a liquid by cooling water 15, and refluxed through a line 17 to a stripping tower 9, and finally CO gas 16
is collected.
上記一酸化炭素の吸収液としては、例えば特願
昭55−21708号に開示された塩化第１銅のヘキサ
メチルホスホリルアミド溶液（以下、HMPA液
と記す）が優れているが、この液の沸点は235℃
と比較的高温であり、従つて原料ガス中に通常、
含まれる水分が吸収液中に凝縮混入してくること
は避けられない。このようにHMPA液に水分が
混入すると、放散塔９でCOの脱着温度まで加温
する際に水分の蒸発が著しく、水分蒸発のための
無駄な熱源を要することになる。また第１図に示
すようにリボイラー１１でHMPAの蒸気を得る
ためにHMPAの沸点（235℃）以上の高圧スチー
ムを要し、そのための所要熱エネルギーが大とな
る欠点がある。 For example, a hexamethylphosphorylamide solution of cuprous chloride (hereinafter referred to as HMPA liquid) disclosed in Japanese Patent Application No. 55-21708 is excellent as the carbon monoxide absorption liquid, but the boiling point of this liquid is is 235℃
and relatively high temperature, therefore the raw material gas usually contains
It is unavoidable that the water contained condenses into the absorption liquid. If water is mixed into the HMPA liquid in this way, the water will evaporate significantly when heated to the CO desorption temperature in the stripping tower 9, resulting in the need for a wasteful heat source for water evaporation. Furthermore, as shown in FIG. 1, in order to obtain HMPA steam in the reboiler 11, high-pressure steam at a temperature higher than the boiling point of HMPA (235° C.) is required, which has the disadvantage of requiring a large amount of thermal energy.
本発明の目的は、特定ガスを吸収した吸収液の
沸点が高いか、またはその蒸発潜熱が大きい場合
に、該吸収液から特定ガスを脱離するに要する熱
量を減少させ、効率よく前記ガスを分離すること
ができる吸収ガスの回収方法を提供することにあ
る。 An object of the present invention is to reduce the amount of heat required to desorb a specific gas from the absorption liquid when the boiling point of the absorption liquid that has absorbed a specific gas is high or the latent heat of vaporization thereof is large, and to efficiently remove the gas. The object of the present invention is to provide a method for recovering absorbed gas that can be separated.
本発明者は、吸収液の蒸気を用いないで一酸化
炭素を脱離させる方法として、該吸収液より沸点
の低い溶剤の蒸気を吸収液中にパージし、COを
蒸気とともに回収する方法を見出した。すなわ
ち、第２図Ａ，Ｂは、COを吸収した吸収液
（HMPA）中のCO濃度の経時変化を示し、Ａは
放電した場合、Ｂは液中にHMPA液よりも沸点
の低いメチルエチルケトン（以下、MEKと記す）
を吹込んだ場合をそれぞれ示す。図から明らかな
ように、放置した場合Ａは、CO濃度は一定値以
上低下しないのに対し、MEKを吹込んだ場合Ｂ
は、液中のCO濃度が急速に減少し、時間の経過
とともにCOが完全に放散されることがわかる。 The present inventor discovered a method for desorbing carbon monoxide without using the vapor of the absorption liquid, in which the vapor of a solvent with a boiling point lower than that of the absorption liquid is purged into the absorption liquid, and CO is recovered together with the vapor. Ta. That is, Figure 2 A and B show the changes over time in the CO concentration in the absorption liquid (HMPA) that has absorbed CO, and A shows the presence of methyl ethyl ketone (hereinafter referred to as below) in the liquid when it is discharged, and B has a lower boiling point than the HMPA liquid. , MEK)
The following shows the case where . As is clear from the figure, the CO concentration does not decrease beyond a certain value in case A when left as it is, while in case B when MEK is injected.
It can be seen that the CO concentration in the liquid decreases rapidly and the CO is completely dissipated over time.
本発明は、上記原理を吸収液中の特定成分の脱
離回収システムに応用したもので、特定ガスを吸
収した吸収液を、該吸収液より沸点の低い溶剤の
蒸気と、該溶剤の沸点以上、前記吸収液の沸点よ
り以下の温度で接触させて溶剤蒸気とともに特定
ガスを放散させる第１の工程、および前記特定ガ
スを含む溶剤蒸気を凝縮させ、該溶剤から特定ガ
スを分離する第２の工程、および前記凝縮させた
溶媒を加熱して溶剤蒸気とし、再び前記第１の工
程に循環させる第３の工程とを含むことを特徴と
する。 The present invention applies the above principle to a desorption/recovery system for specific components in an absorption liquid. , a first step of contacting the absorption liquid at a temperature below the boiling point to diffuse the specific gas together with the solvent vapor, and a second step of condensing the solvent vapor containing the specific gas and separating the specific gas from the solvent. and a third step of heating the condensed solvent to turn it into solvent vapor and circulating it again to the first step.
以下、本発明を図面によりさらに詳細に説明す
る。 Hereinafter, the present invention will be explained in more detail with reference to the drawings.
第１図は、本発明を適用した一酸化炭素回収プ
ロセスの実施例を示す装置系統図である。この場
合、吸収液としては前述の塩化第１銅のHMPA
溶液、低沸点溶剤としてはMEK（沸点約80℃）を
用いている。図において、吸収塔（図示省略）で
COを吸収した吸収液は、吸収液供給管５Ａから
加熱器７Ａを通り、後述する低沸点溶剤の沸点以
上、望ましくは５〜30℃高い温度に加熱され、放
散塔９の充填材層１０上へ散布される。放散塔９
は一般には充填塔、棚段塔、スプレー塔等が用い
られるが、ここでは充填塔方式を採用した。吸収
液は充填物の間を通り、塔内を流下するが、この
間、配気供給管２３から低沸点溶剤の蒸気が供給
され、吸収液まわりのCOガス濃度を下げること
により、COの脱離速度を早めると同時に吸収液
中のCOをほほぼ完全に分離する。COを分離され
た吸収液は抜き出し管１８Ａを通り再び吸収塔へ
戻される。脱離されたCOガスは低沸点溶剤の蒸
気とともに放散塔９から抜き出され、冷却器１４
Ａへ入る。冷却器１４Ａでは冷媒で冷却されて低
沸点溶剤は凝縮し、COガスと分離されてリボイ
ラ２２に直接送入される。ここで低沸点溶剤は再
び蒸発され、加熱器７Ａを介して放散塔９内に再
び供給される。放散塔９の吸収液の温度は、
MEKの沸点（約80℃）以上、HMPA液の沸点
（約235℃）より以下、望ましくは約85〜110℃、
特にHMPA液中の水分等の蒸発による熱ロスを
考慮して90〜95℃の範囲が最適である。なお、放
散塔内の吸収液の昇温は溶剤の蒸気のみでは不可
能なので、放散塔９の入口には吸収液加熱器７Ａ
を設け、上述の放散塔操作温度まで予め加熱して
おく必要がある。 FIG. 1 is an apparatus system diagram showing an embodiment of a carbon monoxide recovery process to which the present invention is applied. In this case, the absorption liquid is HMPA of cuprous chloride mentioned above.
MEK (boiling point approximately 80°C) is used as the solution and low boiling point solvent. In the figure, an absorption tower (not shown)
The absorption liquid that has absorbed CO passes from the absorption liquid supply pipe 5A to the heater 7A, and is heated to a temperature higher than the boiling point of the low boiling point solvent (described later), preferably 5 to 30°C higher, and is heated to a temperature higher than the boiling point of the low boiling point solvent, which will be described later, and placed on the packing material layer 10 of the stripping tower 9. distributed to. Radiant tower 9
Generally, packed towers, tray towers, spray towers, etc. are used, but here a packed tower method was adopted. The absorption liquid passes between the packings and flows down inside the tower. During this time, low boiling point solvent vapor is supplied from the distribution supply pipe 23 to reduce the CO gas concentration around the absorption liquid, thereby desorbing CO. It speeds up the speed and at the same time almost completely separates CO in the absorption liquid. The absorption liquid from which CO has been separated passes through the extraction pipe 18A and is returned to the absorption tower. The desorbed CO gas is extracted from the stripping tower 9 together with the vapor of the low boiling point solvent, and is sent to the cooler 14.
Enter A. In the cooler 14A, the low boiling point solvent is cooled with a refrigerant, condensed, separated from the CO gas, and sent directly to the reboiler 22. Here, the low boiling point solvent is evaporated again and is again supplied into the stripping tower 9 via the heater 7A. The temperature of the absorption liquid in the stripping tower 9 is
Above the boiling point of MEK (about 80℃), below the boiling point of HMPA liquid (about 235℃), preferably about 85 to 110℃,
In particular, a temperature range of 90 to 95°C is optimal, taking into account heat loss due to evaporation of water, etc. in the HMPA liquid. In addition, since it is impossible to raise the temperature of the absorption liquid in the stripping tower using solvent vapor alone, an absorption liquid heater 7A is installed at the entrance of the stripping tower 9.
It is necessary to provide a tank and heat it in advance to the above-mentioned stripping tower operating temperature.
本実施例では、上記のように、放散塔９に送ら
れる吸収液の温度を低沸点溶剤の沸点以上に保つ
て操作するため、放散塔下部から供給された低沸
点溶剤の蒸気は吸収液の中へ溶解することなく、
パージガスとしての働きをした後、COガスとと
もに放散塔９を出て冷却され、全量回収され、再
び加熱蒸気として放散塔に循環使用される。 In this embodiment, as described above, the temperature of the absorption liquid sent to the stripping tower 9 is maintained above the boiling point of the low-boiling point solvent, so the vapor of the low-boiling point solvent supplied from the lower part of the stripping tower is without dissolving into the
After serving as a purge gas, it exits the stripping tower 9 together with the CO gas, is cooled, is recovered in its entirety, and is recycled to the stripping tower again as heated steam.
本実施例によれば、高沸点の吸収液の蒸気を用
いる代りに、該吸収液より低沸点の溶剤蒸気をキ
ヤリアガスとして吸収液中のCOを放散させ、さ
らにこの低沸点溶剤を循環使用するようにしたの
で、リボイラ２２のスチーム量は低沸点溶剤の蒸
発に必要な少量ですみ、省エネルギー化を図るこ
とができる。 According to this embodiment, instead of using the vapor of the absorption liquid with a high boiling point, a solvent vapor with a lower boiling point than the absorption liquid is used as a carrier gas to diffuse CO in the absorption liquid, and furthermore, this low boiling point solvent is recycled and used. Therefore, the amount of steam in the reboiler 22 is only a small amount required for evaporating the low boiling point solvent, and energy saving can be achieved.
次に本発明の他の実施例を第４図に示す。この
実施例では、放散塔９内に充填材層が２段に設け
られ、これらの充填材層１０Ａおよび１０Ｂでそ
れぞれ低沸点溶剤の蒸気と吸収液が向流接触する
ようになつている。先ずCOを含む原料ガスはラ
イン３から吸収塔１の充填材層２に供給され、吸
収液と向流接触し、COを吸収除去された後、排
ガスとしてライン４から放出される。COを吸収
した液はライン５から循環ポンプ６により熱交換
器７、吸収液加熱器７Ａを介して放散塔９へ導入
される。放散塔９では吸収液が充填層１０Ａおよ
び１０Ｂを降下し、一方、溶剤リボイラ２２で発
生した溶剤蒸気がライン２３Ａおよび２３Ｂを通
つて上記各充填材層の下部から上方にパージさ
れ、下降する吸収液と向流接触する際にCOが分
離される。COを分離した吸収液は、ライン１８
Ａを通り、循環ポンプ２５、熱交換器７、および
吸収液冷却器２６を介して再び吸収塔１内に戻さ
れる。一方、放散ガスは放散塔９の塔頂からライ
ン１３を経てコンデンサ１４Ａ内に入り、ここで
冷却管３０により冷却され、低沸点溶剤は凝縮
し、COと分離される。COを含むガスはライン１
６を通り、吸収液冷却器２６で冷熱を回収した
後、ライン２７から分離回収される。一方、低沸
点溶剤はライン２８を通つてリボイラ２２に導入
され、スチーム加熱管１２により加熱蒸発し、そ
の蒸気はライン２３を通つて再び放散塔９に供給
される。 Next, another embodiment of the present invention is shown in FIG. In this embodiment, two stages of packing material layers are provided in the stripping tower 9, and the vapor of the low boiling point solvent and the absorption liquid are brought into countercurrent contact with each other in these packing material layers 10A and 10B. First, a raw material gas containing CO is supplied from line 3 to packing layer 2 of absorption tower 1, comes into countercurrent contact with an absorption liquid, absorbs and removes CO, and is then discharged from line 4 as exhaust gas. The liquid that has absorbed CO is introduced into the stripping tower 9 from the line 5 by the circulation pump 6 via the heat exchanger 7 and the absorption liquid heater 7A. In the stripping tower 9, the absorption liquid descends through the packed beds 10A and 10B, while the solvent vapor generated in the solvent reboiler 22 is purged upward from the bottom of each of the above-mentioned packing layers through lines 23A and 23B. CO is separated during countercurrent contact with the liquid. The absorption liquid from which CO has been separated is line 18
A, and is returned to the absorption tower 1 via the circulation pump 25, the heat exchanger 7, and the absorption liquid cooler 26. On the other hand, the diffused gas enters the condenser 14A from the top of the diffuser tower 9 via the line 13, where it is cooled by the cooling pipe 30, and the low boiling point solvent is condensed and separated from CO. Gas containing CO is line 1
6, the cold energy is recovered by an absorption liquid cooler 26, and then separated and recovered from a line 27. On the other hand, the low boiling point solvent is introduced into the reboiler 22 through the line 28, heated and evaporated by the steam heating tube 12, and the vapor is supplied to the stripping tower 9 again through the line 23.
上記実施例によれば、充填層を１０Ａおよび１
０Ｂに２分割し、低沸点溶媒の蒸気を分割して供
給することにより、気液接触効率を高め、COを
さらに効果的に分離することができる。また溶剤
コンデンサー１４Ａで過冷されたCOガスを、吸
収塔１に導入される吸収液の冷却に用い、冷熱の
有効利用を図ることができる。 According to the above embodiment, the packed bed is 10A and 1
By dividing the 0B into two parts and supplying the vapor of the low boiling point solvent in parts, the gas-liquid contact efficiency can be increased and CO can be separated more effectively. Furthermore, the CO gas subcooled by the solvent condenser 14A can be used to cool the absorption liquid introduced into the absorption tower 1, thereby making it possible to effectively utilize cold energy.
本発明は一酸化炭素の分離のみならず、二酸化
炭素、硫化水素、二酸化イオウ等の分離回収にも
応用することができる。 The present invention can be applied not only to the separation of carbon monoxide, but also to the separation and recovery of carbon dioxide, hydrogen sulfide, sulfur dioxide, and the like.
以上、本発明によれば、特定ガスを吸収した液
に低沸点溶剤蒸気をパージレ、さらに該蒸気を凝
縮させることにより、吸収液中の特定ガスを低エ
ネルギーで脱離させることができる。 As described above, according to the present invention, the specific gas in the absorption liquid can be desorbed with low energy by purging the liquid that has absorbed the specific gas with low boiling point solvent vapor and further condensing the vapor.
第１図は、従来の一酸化炭素の吸収、脱離シス
テムを示すフローシート、第２図ＡおよびＢは、
本発明の原理を説明する吸収液中のCO濃度の経
時変化を示す図、第３図は、本発明の実施例を示
すCO吸収液からCOを回収する方法の装置系統
図、第４図は、本発明の他の実施例を示すCO吸
収、脱離システムのフローシートである。
１……吸収塔、５Ａ……CO含有ガスライン、
９……放散塔、１０……充填材層、１６……CO
排出ライン、２２……低沸点溶剤のリボイラー。
Figure 1 is a flow sheet showing a conventional carbon monoxide absorption and desorption system, Figure 2 A and B are
Figure 3 is a diagram showing the change in CO concentration in the absorption liquid over time to explain the principle of the present invention. Figure 3 is an apparatus system diagram of a method for recovering CO from the CO absorption liquid, which shows an example of the present invention. Figure 4 is a diagram showing the change in CO concentration in the absorption liquid over time. , is a flow sheet of a CO absorption and desorption system showing another embodiment of the present invention. 1...Absorption tower, 5A...CO-containing gas line,
9...Diffusion tower, 10...Filling material layer, 16...CO
Discharge line, 22... reboiler for low boiling point solvent.
Claims (1)
沸点の低い溶剤の蒸気と、該溶剤の沸点以上、前
記吸収液の沸点より以下の温度で接触させて溶剤
蒸気とともに特定ガスを放散させる第１の工程、
および前記特定ガスを含む溶剤蒸気を凝縮させ、
該溶剤から特定ガスを分離する第２の工程、およ
び前記凝縮させた溶剤を加熱蒸気とし、再び前記
第１の工程に循環させる第２の工程とを含むこと
を特徴とする吸収ガスの回収方法。 ２ 特許請求の範囲第１項において、前記特定ガ
スが一酸化炭素、前記吸収液が塩化第１銅とヘキ
サメチルホスホリルアミドを含む溶液、および前
記吸収液より沸点の低い溶剤がメチルエチルケト
ンであることを特徴とする吸収ガスの回収方法。[Scope of Claims] 1. An absorption liquid that has absorbed a specific gas is brought into contact with the vapor of a solvent whose boiling point is lower than that of the absorption liquid at a temperature that is higher than the boiling point of the solvent and lower than the boiling point of the absorption liquid, and together with the solvent vapor. A first step of dissipating the specific gas,
and condensing the solvent vapor containing the specific gas,
A method for recovering absorbed gas, comprising: a second step of separating a specific gas from the solvent; and a second step of turning the condensed solvent into heated steam and circulating it back to the first step. . 2. Claim 1 provides that the specific gas is carbon monoxide, the absorption liquid is a solution containing cuprous chloride and hexamethylphosphorylamide, and the solvent having a boiling point lower than that of the absorption liquid is methyl ethyl ketone. Features: Absorbed gas recovery method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55122962A JPS5748328A (en) | 1980-09-06 | 1980-09-06 | Recovery of absorbed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55122962A JPS5748328A (en) | 1980-09-06 | 1980-09-06 | Recovery of absorbed gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5748328A JPS5748328A (en) | 1982-03-19 |
| JPS6354411B2 true JPS6354411B2 (en) | 1988-10-27 |
Family
ID=14848922
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP55122962A Granted JPS5748328A (en) | 1980-09-06 | 1980-09-06 | Recovery of absorbed gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5748328A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62153010U (en) * | 1986-03-20 | 1987-09-28 | ||
| CN104174258A (en) * | 2014-08-21 | 2014-12-03 | 山东迪赛机电有限公司 | Solvent recovery device for producing film |
-
1980
- 1980-09-06 JP JP55122962A patent/JPS5748328A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5748328A (en) | 1982-03-19 |
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