JPH032005B2 - - Google Patents
Info
- Publication number
- JPH032005B2 JPH032005B2 JP57169615A JP16961582A JPH032005B2 JP H032005 B2 JPH032005 B2 JP H032005B2 JP 57169615 A JP57169615 A JP 57169615A JP 16961582 A JP16961582 A JP 16961582A JP H032005 B2 JPH032005 B2 JP H032005B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- solvent
- tower
- absorption
- raw material
- 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 - Lifetime
Links
- 239000002904 solvent Substances 0.000 claims description 44
- 238000010521 absorption reaction Methods 0.000 claims description 33
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 27
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 27
- 238000001179 sorption measurement Methods 0.000 claims description 23
- 239000002994 raw material Substances 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- 238000003795 desorption Methods 0.000 claims description 9
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
- 238000000034 method Methods 0.000 description 12
- 238000011084 recovery Methods 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229910021591 Copper(I) chloride Inorganic materials 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 description 1
- 229940045803 cuprous chloride Drugs 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- GNOIPBMMFNIUFM-UHFFFAOYSA-N hexamethylphosphoric triamide Chemical compound CN(C)P(=O)(N(C)C)N(C)C GNOIPBMMFNIUFM-UHFFFAOYSA-N 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Gas Separation By Absorption (AREA)
- Carbon And Carbon Compounds (AREA)
Description
【発明の詳細な説明】
本発明は、一酸化炭素（CO）分離方法に係り、
特に吸収液法CO分離プロセスに係り、溶剤の回
収を容易に行い、同時に吸着塔での溶剤の脱着用
熱源の調達を容易にした、吸収法によるCO分離
プロセスに関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a carbon monoxide (CO) separation method,
In particular, it relates to a CO separation process using an absorption liquid method, which facilitates the recovery of a solvent and at the same time facilitates the procurement of a heat source for solvent desorption in an adsorption tower.
吸収法COガス分離プロセスは、テネコ社の
COSORB法と当社開発した吸収液を用いる
HISORB法があるが、吸収液が異るのみで基本
的なプロセスの構成はほぼ同一である。このプロ
セスの概要を第１図に示す。図において、COを
含む原料ガスは吸収塔１底部から導入され、塔内
を流下する循環吸収液と向流接触し、原料ガス中
のCOのみが選択的に吸収される。COを吸収した
リツチソルベントは吸収塔１底部から取り出さ
れ、熱交換器３で再生された高温のリーンソルベ
ントと熱交換を行つた後、再生塔２の塔頂へ送ら
れ、リボイラ４によつて供給される熱によつて加
熱され、COを放出する。放出されたCOガスは、
コンデンサー５で溶剤蒸気を凝縮させた後、残り
の未凝縮溶剤を吸着塔６で完全に回収した後、製
品COガスとなつて排出される。一方、再生され
た溶剤（リーンソルベント）は、再生塔２の塔底
から取り出され、前記熱交換器３を経て、クーラ
ー１０で所定の温度まで冷却された後、吸収塔１
の塔頂へ循環される。吸収塔１の塔頂から取り出
されたオフガスは、コンデンサー１３で溶剤を凝
縮回収された後、最終的に吸着塔７に導入され、
ここで溶剤が完全に吸着回収される。吸着塔７で
吸着された溶剤は、スチームストリツピングによ
つて加熱脱着され、溶剤を含むスチームはコンデ
ンサー８で凝縮、回収される。なお、１４はスチ
ーム、１５は冷却水の各ラインを示す。 The absorption CO gas separation process is based on Tenneco's
Using COSORB method and absorption liquid developed by our company
There is the HISORB method, but the basic process structure is almost the same except for the absorption liquid. An overview of this process is shown in Figure 1. In the figure, a raw material gas containing CO is introduced from the bottom of an absorption tower 1, comes into countercurrent contact with the circulating absorption liquid flowing down the tower, and only the CO in the raw material gas is selectively absorbed. The rich solvent that has absorbed CO is taken out from the bottom of the absorption tower 1, exchanges heat with the regenerated high-temperature lean solvent in the heat exchanger 3, and then is sent to the top of the regeneration tower 2, where it is passed through the reboiler 4. It is heated by the supplied heat and releases CO. The released CO gas is
After the solvent vapor is condensed in the condenser 5, the remaining uncondensed solvent is completely recovered in the adsorption tower 6 and then discharged as product CO gas. On the other hand, the regenerated solvent (lean solvent) is taken out from the bottom of the regeneration tower 2, passes through the heat exchanger 3, is cooled to a predetermined temperature in the cooler 10, and is then transferred to the absorption tower 2.
It is circulated to the top of the tower. The off-gas taken out from the top of the absorption tower 1 condenses and recovers the solvent in the condenser 13, and is finally introduced into the adsorption tower 7.
Here, the solvent is completely adsorbed and recovered. The solvent adsorbed in the adsorption tower 7 is thermally desorbed by steam stripping, and the steam containing the solvent is condensed and recovered in the condenser 8. Note that 14 indicates steam lines and 15 indicates cooling water lines.
しかしながら、上記プロセスにおいてオフガス
からの溶剤（吸収液）の回収は、コンデンサー１
３のみでは不充分であり、ほとんど吸着塔７で回
収されるのが現状である。このため、吸着塔７へ
の負荷が大となり、また吸着塔７での溶剤脱着用
スチームを大量に必要とし、また、溶剤蒸気およ
びスチームのコンデンサー８も必要となる。CO
分離プロセスの運転コストの50〜70％をスチーム
コストが占めることを考えれば、このようなスチ
ームを大量に消費するプロセスは合理的ではな
い。 However, in the above process, the recovery of the solvent (absorbent liquid) from the off-gas is limited to the condenser 1.
3 alone is insufficient, and currently most of it is recovered in the adsorption tower 7. Therefore, the load on the adsorption tower 7 is large, a large amount of steam is required for solvent desorption in the adsorption tower 7, and a condenser 8 for solvent vapor and steam is also required. C.O.
Considering that steam costs account for 50-70% of the operating cost of a separation process, such a steam-intensive process is unreasonable.
本発明の目的は、上記した従来技術の欠点をな
くし、オフガス中の溶剤を効果的に凝縮回収し、
またスチームを用いることなく吸着塔での溶剤の
脱着を可能にし、かつランニングコストを大幅に
低減することができる一酸化炭素分離方法を提供
することにある。 The purpose of the present invention is to eliminate the above-mentioned drawbacks of the prior art, to effectively condense and recover the solvent in the off-gas,
Another object of the present invention is to provide a carbon monoxide separation method that enables solvent desorption in an adsorption tower without using steam and that can significantly reduce running costs.
本発明は、低濃度の一酸化炭素（以下、COと
記す）を含む混合ガスを吸収塔に供給し、吸収液
を用いてCOを吸収した後、該吸収液を再生塔に
送り、ここで放散によりCOを選択的に分離、回
収し、高濃度のCOガスを得るとともに、オフガ
スを吸着塔に供給して吸収液溶剤を回収するCO
ガス分離方法において、吸着塔での吸着溶剤の脱
着に、原料ガスを加圧し、その一部分を使用する
ことを特徴とする。 The present invention supplies a mixed gas containing low concentration carbon monoxide (hereinafter referred to as CO) to an absorption tower, absorbs CO using an absorption liquid, and then sends the absorption liquid to a regeneration tower. CO that selectively separates and recovers CO through diffusion to obtain highly concentrated CO gas, and also supplies the off-gas to an adsorption tower to recover the absorption liquid solvent.
The gas separation method is characterized in that the raw material gas is pressurized and a portion of it is used for desorption of the adsorbed solvent in an adsorption tower.
本発明において、原料ガスを加圧するコンプレ
ツサーを膨張タービンと直結し、吸収塔を出た加
圧オフガスを該膨張タービンに供給し、減圧する
とともに動力を回収し、これを上記コンプレツサ
ーの動力として使用することが望ましい。 In the present invention, a compressor that pressurizes raw material gas is directly connected to an expansion turbine, and the pressurized off-gas leaving the absorption tower is supplied to the expansion turbine to reduce the pressure and recover power, which is used as power for the compressor. This is desirable.
本発明におけるCO吸収液は、いわゆる吸収法
に用いられるものであれば如何なるものでもよい
が、第一銅塩溶液（例えば塩化第１銅のトリス
（ジメチルアミノ）ホスフインオキシド溶液）、該
溶液の粘度調整のために低粘度溶剤（トルエン
等）を混合した場合に好ましく適用される。 The CO absorption solution in the present invention may be any solution as long as it is used in the so-called absorption method, including a cuprous salt solution (for example, a solution of cuprous chloride in tris(dimethylamino)phosphine oxide), It is preferably applied when a low viscosity solvent (such as toluene) is mixed to adjust the viscosity.
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２図は、本発明の一実施例を示す一酸化炭素
分離方法のフローシートである。このプロセス
は、原料ガスをコンプレツサー（加圧タービン）
１１により圧縮、昇温する工程と、加圧された原
料ガスをダンパ２１を介して吸収塔１へ送る一
方、その一部を分岐してライン１９から吸着塔７
に送り、ここでオフガスから吸着された溶剤の脱
着を行ない、さらに溶剤を含む原料ガスをライン
２０を介して元の原料供給ライン２２に戻す工
程、吸収塔１のオフガスをライン２３を介して膨
張タービン１２に送り、減圧、降温させて溶剤を
凝縮、回収する工程、回収された溶剤をライン１
７を介して吸収塔１へ戻す一方、オフガスはライ
ン１８を通して吸着塔７に送り、ここで残りの溶
剤を吸着、回収する工程とから主として構成され
る。再生塔２以下の工程は第１図の従来プロセス
の場合と同様である。 FIG. 2 is a flow sheet of a carbon monoxide separation method showing one embodiment of the present invention. In this process, the raw gas is passed through a compressor (pressurizing turbine).
11, and the pressurized raw material gas is sent to the absorption tower 1 via the damper 21, while a part of it is branched and sent from the line 19 to the adsorption tower 7.
In this step, the solvent adsorbed from the off-gas is desorbed, and the raw material gas containing the solvent is returned to the original raw material supply line 22 via the line 20. The off-gas from the absorption tower 1 is expanded via the line 23. The process of sending the solvent to the turbine 12, reducing the pressure and lowering the temperature to condense and recover the solvent, and the recovered solvent is transferred to the line 1.
The off-gas is returned to the absorption tower 1 via line 18, while the off-gas is sent to the adsorption tower 7 through line 18, where the remaining solvent is adsorbed and recovered. The steps in and after the regeneration tower 2 are the same as in the conventional process shown in FIG.
上記構成において、原料ガスは、加圧タービン
１１によつて例えば約５Kg／cm2Ｇ、100℃に加圧、
昇温され、ライン１９により一部分岐され、分岐
した原料ガスは、吸着塔７の溶剤の脱着に用いら
れ、脱着された溶剤とともにライン２０を通り、
吸収塔１入口で再び合流される。この工程で若干
減圧された原料ガスは、吸収塔１内において吸収
液と向流接触し、COを吸収された後、塔頂から
オフガスとして排出される。オフガスは、ライン
２３から膨張タービン１２に入り、ここで例えば
常圧、−10℃にまで減圧、降温され、この工程で
溶剤が凝縮回収され、該溶剤はタンク１６を経て
ライン１７から吸収塔１に戻される。溶剤を回収
されたオフガスは、ライン１８を経て最終的に吸
着塔７で残りの溶剤が吸着される。この吸着剤の
脱着には、前述したようにスチームの代りに加圧
原料ガスが用いられ、従つて、運転コストを大幅
に下げることができ、しかもスチーム使用の場合
に必要であつたコンデンサー８も不要となる。因
みに、原料ガス（BFG）５万Ｎm3／H〓でCO回収
率９０％とした場合、約30T／H〓のスチームを
低減することができた。 In the above configuration, the raw material gas is pressurized to, for example, about 5 kg/cm 2 G and 100° C. by the pressurizing turbine 11.
The raw material gas is heated and partially branched through line 19, and the branched raw material gas is used for desorption of the solvent in adsorption tower 7, and passes through line 20 together with the desorbed solvent.
They are combined again at the entrance of absorption tower 1. The raw material gas, whose pressure has been slightly reduced in this step, comes into countercurrent contact with the absorption liquid in the absorption tower 1, absorbs CO, and is then discharged from the top of the tower as an off-gas. The off-gas enters the expansion turbine 12 from the line 23, where the pressure is reduced to, for example, normal pressure and -10°C, and the temperature is lowered. In this step, the solvent is condensed and recovered, and the solvent is passed through the tank 16 and sent from the line 17 to the absorption tower 1. will be returned to. The off-gas from which the solvent has been recovered passes through the line 18 and finally enters the adsorption tower 7, where the remaining solvent is adsorbed. For the desorption of this adsorbent, pressurized raw material gas is used instead of steam as described above, and therefore operating costs can be significantly reduced, and the condenser 8 required when using steam is also eliminated. No longer needed. Incidentally, when the CO recovery rate was 90% with a raw material gas (BFG) of 50,000 Nm 3 /H, it was possible to reduce steam by approximately 30T/H.
上記実施例によれば、原料ガスをコンプレツサ
ーで加圧することにより、吸収塔１における溶剤
の放散量が低減され、同時に膨張タービンで動力
回収を行う時点で、ガス温度が低下することによ
り、溶剤を凝縮回収することができ、さらに加圧
原料ガスを一部分岐させ、吸着塔７での溶剤の脱
着に使用することにより、従来のコンデンサー８
を不要とすることができる。また上記のように加
圧オフガスの減圧操作で溶剤の凝縮回収が可能な
ため、従来のコンデンサー１３も不要となる。 According to the above embodiment, by pressurizing the raw material gas with the compressor, the amount of solvent released in the absorption tower 1 is reduced, and at the same time, when the power is recovered by the expansion turbine, the gas temperature is lowered, so that the solvent is removed. It can be condensed and recovered, and furthermore, by branching a part of the pressurized raw material gas and using it for desorption of the solvent in the adsorption tower 7, it is possible to
can be made unnecessary. Further, as described above, since the solvent can be condensed and recovered by decompressing the pressurized off-gas, the conventional condenser 13 is also unnecessary.
本発明のプロセスによれば、例えば溶剤の放散
量を従来の８割程度に減少させることができ、ま
た溶剤の凝縮回収も、従来の冷却器では吸収液の
温度が低いため回収率が低かつたが、本発明では
膨張タービンで減圧して温度低下させるので、無
理なく行なうことができる。さらに溶剤の吸着回
収についても、従来は大容量の吸着塔を要してい
たが、膨張タービンによりかなり回収されるの
で、例えば従来の50％の容量の吸着塔でよく、ま
た溶剤脱着時にスチームの代りに原料ガスを用い
た場合には溶剤−水分離器等も不要になる等の利
点がある。 According to the process of the present invention, for example, the amount of solvent dissipated can be reduced to about 80% of the conventional amount, and the recovery rate of the solvent is low in conventional coolers due to the low temperature of the absorption liquid. However, in the present invention, since the pressure is reduced by an expansion turbine to lower the temperature, this can be done without difficulty. Furthermore, for the adsorption and recovery of solvents, conventionally a large-capacity adsorption tower was required, but since a large amount is recovered using an expansion turbine, an adsorption tower with, for example, 50% of the conventional capacity can be used. When raw material gas is used instead, there are advantages such as no need for a solvent-water separator or the like.
本発明は、同様なガス吸収分離プロセスにおい
て、溶剤の回収に多量のスチームを必要とするプ
ロセスに効果的である。また再生塔側吸着塔の脱
着用スチームの代りに、加圧原料ガスを用いるこ
とも可能である。 The present invention is effective in similar gas absorption separation processes that require a large amount of steam for solvent recovery. Furthermore, instead of the steam for desorption in the adsorption tower on the regeneration tower side, it is also possible to use pressurized raw material gas.
以上、本発明によれば、COガス分離プロセス
における溶剤の回収が容易となり、スチーム消費
量の大幅な低減を計り、ランニングコストを大幅
に低下させることができる。 As described above, according to the present invention, it is possible to easily recover the solvent in the CO gas separation process, significantly reduce steam consumption, and significantly reduce running costs.
第１図および第２図は、それぞれ従来および本
発明のCO分離方法の基本的構成を示す装置系統
図である。
１……吸収塔、２……再生塔、３……吸収液熱
交換器、５……コンデンサー、７……吸着塔、
８，９……コンデンサー、１１……コンプレツサ
ー、１２……膨張タービン。
FIG. 1 and FIG. 2 are system diagrams showing the basic configurations of the conventional CO separation method and the present invention, respectively. 1...Absorption tower, 2...Regeneration tower, 3...Absorption liquid heat exchanger, 5...Condenser, 7...Adsorption tower,
8, 9... Condenser, 11... Compressor, 12... Expansion turbine.
Claims (1)
含む混合ガスを吸収塔に供給し、吸収液を用いて
COを吸収した後、該吸収液を再生塔に送り、こ
こで放散によりCOを選択的に分離、回収し、高
濃度のCOガスを得るとともに、オフガスを吸着
塔に供給して吸収液溶剤を回収するCOガス分離
方法において、吸着塔での吸着溶剤の脱着に、原
料ガスを加圧し、その一部分を使用することを特
徴とする一酸化炭素分離方法。 ２ 特許請求の範囲第１項において、原料ガスを
加圧するコンプレツサーを膨張タービンと直結
し、吸収塔を出た加圧オフガスを該膨張タービン
に供給し、減圧するとともに動力を回収し、これ
を上記コンプレツサーの動力として使用すること
を特徴とする一酸化炭素分離方法。 ３ 特許請求の範囲第２項において、前記加圧オ
フガスを減圧する時点で溶剤を凝縮、回収するこ
とを特徴とする一酸化炭素分離方法。[Claims] 1. A mixed gas containing low concentration carbon monoxide (hereinafter referred to as CO) is supplied to an absorption tower, and an absorption liquid is used to
After absorbing CO, the absorption liquid is sent to the regeneration tower, where CO is selectively separated and recovered by dissipation to obtain highly concentrated CO gas, and off-gas is supplied to the adsorption tower to remove the absorption liquid solvent. A carbon monoxide separation method for recovering CO gas, characterized in that a raw material gas is pressurized and a portion of it is used for desorption of an adsorption solvent in an adsorption tower. 2. In claim 1, a compressor that pressurizes raw material gas is directly connected to an expansion turbine, and the pressurized off-gas exiting the absorption tower is supplied to the expansion turbine to reduce the pressure and recover the power, which is then used to A carbon monoxide separation method characterized by use as a power source for a compressor. 3. The carbon monoxide separation method according to claim 2, characterized in that the solvent is condensed and recovered at the time of reducing the pressure of the pressurized off-gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57169615A JPS5964515A (en) | 1982-09-30 | 1982-09-30 | Separation of carbon monoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57169615A JPS5964515A (en) | 1982-09-30 | 1982-09-30 | Separation of carbon monoxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5964515A JPS5964515A (en) | 1984-04-12 |
| JPH032005B2 true JPH032005B2 (en) | 1991-01-14 |
Family
ID=15889777
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57169615A Granted JPS5964515A (en) | 1982-09-30 | 1982-09-30 | Separation of carbon monoxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5964515A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1481779A2 (en) | 2003-05-20 | 2004-12-01 | Ngk Insulators, Ltd. | Forming JIG and method for producing formed body using same |
| US8883329B2 (en) | 2009-06-02 | 2014-11-11 | Fujifilm Corporation | Hexagonal ferrite magnetic powder and method of manufacturing the same, and magnetic recording medium and method of manufacturing the same |
-
1982
- 1982-09-30 JP JP57169615A patent/JPS5964515A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1481779A2 (en) | 2003-05-20 | 2004-12-01 | Ngk Insulators, Ltd. | Forming JIG and method for producing formed body using same |
| US8883329B2 (en) | 2009-06-02 | 2014-11-11 | Fujifilm Corporation | Hexagonal ferrite magnetic powder and method of manufacturing the same, and magnetic recording medium and method of manufacturing the same |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5964515A (en) | 1984-04-12 |
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