JPS6139092B2 - - Google Patents
Info
- Publication number
- JPS6139092B2 JPS6139092B2 JP53026086A JP2608678A JPS6139092B2 JP S6139092 B2 JPS6139092 B2 JP S6139092B2 JP 53026086 A JP53026086 A JP 53026086A JP 2608678 A JP2608678 A JP 2608678A JP S6139092 B2 JPS6139092 B2 JP S6139092B2
- Authority
- JP
- Japan
- Prior art keywords
- oxazolidone
- absorbent
- fraction
- heating
- reactor
- 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
- 230000002745 absorbent Effects 0.000 claims description 31
- 239000002250 absorbent Substances 0.000 claims description 31
- IZXIZTKNFFYFOF-UHFFFAOYSA-N 2-Oxazolidone Chemical compound O=C1NCCO1 IZXIZTKNFFYFOF-UHFFFAOYSA-N 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 8
- 239000007864 aqueous solution Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 2
- 125000000467 secondary amino group Chemical class [H]N([*:1])[*:2] 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- WDGCBNTXZHJTHJ-UHFFFAOYSA-N 2h-1,3-oxazol-2-id-4-one Chemical class O=C1CO[C-]=N1 WDGCBNTXZHJTHJ-UHFFFAOYSA-N 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 4
- 229940043276 diisopropanolamine Drugs 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 4
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 150000003335 secondary amines Chemical class 0.000 description 3
- NESWNPQKWACMGV-UHFFFAOYSA-N 3-(2-hydroxypropyl)-5-methyl-1,3-oxazolidin-2-id-4-one Chemical compound OC(CN1[CH-]OC(C1=O)C)C NESWNPQKWACMGV-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 150000003141 primary amines Chemical class 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Heterocyclic Carbon Compounds Containing A Hetero Ring Having Nitrogen And Oxygen As The Only Ring Hetero Atoms (AREA)
Description
本発明は、２種またはそれ以上のガスからCO2
および／またはCOSを除去する吸収剤であつて
Ｎ−（２−ヒドロキシアルキル）第１級および／
または第２級アミンの水性溶液を包含しかつオキ
サゾリドンで汚染されている吸収剤の再生法に関
する。
基−ＮH−Ｃ−ＣOH−を含有するＮ−（２−ヒド
ロキシアルキル）第１級および第２級アミン類
は、それらの水性溶液がCO2用の吸収剤として用
いられる場合オキサゾリドン類を生成することは
わかつており、おそらく次の反応機構に従うもの
であろう。
COSの場合、該アルカノールアミン類は、お
そらく次のように反応するであろう。
２種またはそれ以上のガスからCO2、COS、お
よびH2Sを吸収するのにしばしば用いられかつオ
キサゾリドン生成が起こり得る吸収剤の例とし
て、ジイソプロパノールアミンの水性溶液を挙げ
ることができる。この場合においては、３−（２
−ヒドロキシプロピル）−５−メチル−２−オキ
サゾリドンが生成する。本発明が局限するタイプ
のアルカノールアミン類の他の例はモノエタノー
ルアミンおよびジエタノールアミンであり、それ
らもまた吸収剤として水性溶液で用いられる。
このような吸収剤において、オキサゾリドン類
の生成が許容され得ないことがあり得るので（い
くつかの場合、１％Ｗアルカノールアミンが１時
間当り変換されるような状態である）、再生法は
以前に英国特許明細書第1118687号に提案されて
おり、水酸化カリウムが再生されるべき該吸収剤
に添加され、その結果該オキサゾリドンは炭酸カ
リウムの生成とともに、該アルカノールアミンに
変換される。この方法の欠点は、該炭酸カリウム
を除去しなければならないこと、高価な化学薬品
を消費すること、該再生をほとんど連続的に行な
うことができないこと、および比較的複雑な装置
を必要とすることである。
本発明は、上記の欠点を有さずかつ該アルカノ
ールアミンを簡単な態様で該オキサゾリドンから
回収し得る方法を提供する。
本発明によれば、２種またはそれ以上のガスか
らCO2および／またはCOSを除去するための吸収
剤であつてＮ−（２−ヒドロキシアルキル）第１
級および／または第２級アミンの水性溶液を包含
しかつオキサゾリドンで汚染されている吸収剤の
再生法において、該吸収剤あるいはそれから得ら
れるオキサゾリドン含有留分（フラクシヨン）を
水の存在下昇圧において少なくとも200℃の温度
に加熱する上記方法が提供される。
この昇圧における加熱が、CO2の放出および水
の消費を伴ない、該オキサゾリドンを該吸収剤中
に初めに存在したアルカノールアミンに変換する
ということを見い出した。もし該吸収剤それ自体
を加熱するならば、十分な水は該目的のために存
在する。該吸収剤から得られかつ十分な水を含有
しない留分が加熱されるべきであるならば、いく
らかの水を加えるべきである。
生成したCO2は、好ましくは、水蒸気ストリツ
ピングにより少なくとも200℃の温度での加熱中
除去される。これは、費用がかからずかつ効果的
な方法であり、該吸収剤の汚染を起こさずかつ該
所要温度は容易に達成され得る。さらに、水蒸気
ストリツピングは、生成CO2の連続排出を確実に
する。適当な圧力制御でもつて、水蒸気の使用
が、所望の水量を該オキサゾリドンの変換中維持
することを可能にする。
良好な結果が、200ないし300℃特に200ないし
250℃の範囲の加熱温度で得られる。これらの温
度では、関係のあるアルカノールアミン類および
オキサゾリドン類の熱分解の危険は小さい。
好ましい実施態様によれば、加熱は10〜60気圧
の圧力において起こる。一方、該圧力はその場合
良好な変換のため十分な高さであり、他方所望装
置の費用は、はるかに一層高い圧力の場合よりも
低い。
本発明によるタイプの吸収剤は、２種またはそ
れ以上のガスからH2S、COS、およびCO2を連続
的に除去する方法においてしばしば用いられる。
この目的に対して、該ガスはしばしば上向きの流
れでカラムに通され、そのカラム中には多数の接
触トレイが存在しかつ吸収剤は該頂部からトレイ
に下向きで流れる。該カラムの底において、CO2
およびH2Sを吸収した吸収剤を排出し、頂部にお
いて該精製ガスを排出する。該吸収済吸収剤は該
カラムの底からストリツピングカラムの頂部に連
続的に通され、該ストリツピングカラム中におい
ては該吸収済吸収剤が下向きに流れ、かつ該圧力
を減じることによるか水蒸気のようなストリツピ
ングガスでストリツプすることにより該吸収済吸
収剤は該CO2およびH2Sから遊離される。該吸収
カラムおよび該ストリツピングカラムにおける条
件は、CO2およびH2Sがそれぞれ捕縛されおよび
放出されるような条件である。該ストリツプされ
た溶媒は、該ストリツピングカラムの底から該吸
収カラムの頂部に連続的に再循環する。該ストリ
ツピングカラムでは、温度は一般に175℃より低
く保つ。
該２つのカラム中に生成したオキサゾリドンが
除去または変換されない場合、該オキサゾリドン
分の蓄積が起こり、全量の吸収剤の吸収力は徐々
に減少する。
非常に適当には、ブリード流（bleed
stream）が、該ストリツピングカラムの底から
該吸収カラムの頂部に再循環される吸収剤流から
好ましくは連続的に取られ、そしてこのブリード
流は本発明に従い再生される。
本発明による再生は加熱により（一般に比較的
長期間）行なわれる故に、加熱されるべき液体の
量を減じることにより、必要な熱量を減じること
が有利である。そういうわけで、該ストリツピン
グカラムから該吸収カラムへ再循環されるべき吸
収剤の流れそのままからオキサゾリドンを除去し
ないで、オキサゾリドンを含有するこの流れの留
分から除去することが有利である。このような留
分は、非常に適当には、蒸留によりオキサゾリド
ンを含有する留分およびオキサゾリドンを比較的
低い濃度で含有するか全く含有しない留分に分離
（好ましくは連続的に）することにより得られ
る。該オキサゾリドン含有留分は、本発明による
方法により処理され、次いで例えば該吸収カラム
の頂部に再循環される。この態様では、全量の吸
収剤において常に増加するオキサゾリドン分は防
止され、該吸収剤のオキサゾリドン分は、高圧高
温で多量の吸収剤を処理する必要なしに所望の値
に置かれ得る。
オキサゾリドンを含有する留分が得られる蒸留
は、好ましくは、100〜200℃での水蒸気ストリツ
ピングで行なわれる。該Ｎ−（２−ヒドロキシア
ルキル）アミンは留去され、そしてこのようにし
て得られたオキサゾリドン含有底留分は、該吸収
剤と比べて減少した量の水およびアルカノールア
ミンを含有する。
本発明を次の実施例によりさらに説明する。
実施例
いくつかの実験シリーズにおいて、水と３−
（２−ヒドロキシプロピル）−５−メチル−２−オ
キサゾリドンとの混合物を、種々の温度および昇
圧においてある時間水蒸気でストリツプし、該反
応器内容物の試料を、該オキサゾリドンのジイソ
プロパノールアミンへの変換過程を測定すること
ができるように該反応中採取した。
順次操作は次の通りであつた。
各実験に対して、計量した水量および該オキサ
ゾリドンを反応器に導入し、続いて該反応器を
CO2でフラツシユして空気を追い出した。次い
で、該反応器中の温度およびその結果圧力を徐々
に15分以内に増加させた。該実験中通じた水蒸気
は、常に該反応器から凝縮容器に送られ、該凝縮
容器においてそれから凝縮した留分を集めた。所
望温度に達した後、試料を該反応器中に開口する
管を経て一定の間を置いて採取し、一方該凝縮留
分は同時に排出した。最初の試料を採取した時点
を常に実験の出発点とみなした。
該試料から得られたデータを処理する際、次の
影響を考慮した。
該反応器における該オキサゾリドン濃度は次の
３点で影響される。
(1) 該オキサゾリドンの一部がジイソプロパノー
ルアミンに変換される。
(2) 吹き込まれた水蒸気が、該反応器の内容物を
希釈または濃縮し得る。
(3) 該水蒸気はまた、該オキサゾリドンの一部を
該凝縮留分中に到達させる。
影響(2)および(3)のため、ジイソプロパノールア
ミンに変換されたオキサゾリドンの留分は、特別
な態様で測定しなければならなかつた。すなわ
ち、該留物は、該反応器への供給物、該反応器か
らの試料、および該凝縮留分の分析によつて得ら
れた質量収支から計算した。この測定に際して、
該凝縮留分からのオキサゾリドンは、常に、該オ
キサゾリドンの未変換部分に属するものとみなし
た。
結果を次の表に要約した。
The present invention enables CO 2 to be extracted from two or more gases.
and/or an absorbent for removing COS, comprising N-(2-hydroxyalkyl) primary and/or
or to a method for regenerating an absorbent containing an aqueous solution of a secondary amine and contaminated with oxazolidone. N-(2-hydroxyalkyl) primary and secondary amines containing the group -N H -C-C OH - are suitable for oxazolidones when their aqueous solutions are used as absorbents for CO2 . It is known that it is produced, and it probably follows the following reaction mechanism. In the case of COS, the alkanolamines would likely react as follows. An example of an absorbent that is often used to absorb CO 2 , COS, and H 2 S from two or more gases and in which oxazolidone formation can occur is an aqueous solution of diisopropanolamine. In this case, 3-(2
-hydroxypropyl)-5-methyl-2-oxazolidone is produced. Other examples of alkanolamines of the type to which this invention is directed are monoethanolamine and diethanolamine, which are also used in aqueous solutions as absorbents. Since the formation of oxazolidones in such absorbents can be unacceptable (in some cases such that 1% W alkanolamine is converted per hour), regeneration methods have previously been proposed in British Patent Specification No. 1118687, in which potassium hydroxide is added to the absorbent to be regenerated, so that the oxazolidone is converted to the alkanolamine with the production of potassium carbonate. The disadvantages of this method are that the potassium carbonate has to be removed, that it consumes expensive chemicals, that the regeneration cannot be carried out nearly continuously, and that it requires relatively complex equipment. It is. The present invention provides a process which does not have the above-mentioned drawbacks and by which the alkanolamines can be recovered from the oxazolidones in a simple manner. According to the present invention, an absorbent for removing CO 2 and/or COS from two or more gases, comprising N-(2-hydroxyalkyl) primary
In a process for regenerating an absorbent containing an aqueous solution of a primary and/or secondary amine and contaminated with oxazolidone, the absorbent or the oxazolidone-containing fraction obtained therefrom is at least The above method of heating to a temperature of 200°C is provided. It has been found that heating at this elevated pressure converts the oxazolidone to the alkanolamine originally present in the absorbent, with the release of CO2 and consumption of water. If the absorbent itself is heated, sufficient water is present for the purpose. If the fraction obtained from the absorbent and not containing sufficient water is to be heated, some water should be added. The CO 2 produced is preferably removed during heating at a temperature of at least 200° C. by steam stripping. This is an inexpensive and effective method that does not cause contamination of the absorbent and the required temperature can be easily achieved. Furthermore, steam stripping ensures continuous evacuation of the CO 2 produced. With appropriate pressure control, the use of steam makes it possible to maintain the desired amount of water during the conversion of the oxazolidone. Good results are obtained at 200 to 300℃, especially at 200 to 300℃.
Obtained at heating temperatures in the range of 250°C. At these temperatures, the risk of thermal decomposition of the alkanolamines and oxazolidones involved is small. According to a preferred embodiment, heating takes place at a pressure of 10 to 60 atmospheres. On the one hand, the pressure is then high enough for good conversion, and on the other hand the cost of the desired equipment is lower than in the case of much higher pressures. Absorbents of the type according to the invention are often used in processes for the continuous removal of H 2 S, COS and CO 2 from two or more gases.
For this purpose, the gas is often passed in an upward flow through a column in which there are a number of contact trays and the absorbent flows downward into the trays from the top. At the bottom of the column, CO 2
and the absorbent that has absorbed H 2 S is discharged, and the purified gas is discharged at the top. The absorbed absorbent is passed continuously from the bottom of the column to the top of a stripping column in which the absorbed absorbent flows downward and by reducing the pressure. The absorbed absorbent is liberated from the CO 2 and H 2 S by stripping with a stripping gas such as steam. The conditions in the absorption column and the stripping column are such that CO2 and H2S are trapped and released, respectively. The stripped solvent is continuously recycled from the bottom of the stripping column to the top of the absorption column. In the stripping column, the temperature is generally kept below 175°C. If the oxazolidone produced in the two columns is not removed or converted, the oxazolidone fraction will accumulate and the absorption capacity of the total absorbent will gradually decrease. A very suitable term is bleed flow.
stream) is preferably continuously taken from the absorbent stream recycled from the bottom of the stripping column to the top of the absorption column, and this bleed stream is regenerated according to the invention. Since regeneration according to the invention is carried out by heating (generally for a relatively long period of time), it is advantageous to reduce the amount of heat required by reducing the amount of liquid that has to be heated. That is why it is advantageous not to remove the oxazolidone directly from the absorbent stream to be recycled from the stripping column to the absorption column, but from the fraction of this stream containing the oxazolidone. Such a fraction is very suitably obtained by separating (preferably continuously) by distillation into a fraction containing oxazolidones and a fraction containing relatively low concentrations or no oxazolidones. It will be done. The oxazolidone-containing fraction is treated by the method according to the invention and then recycled, for example to the top of the absorption column. In this embodiment, a constantly increasing oxazolidone content in the total amount of absorbent is prevented, and the oxazolidone content of the absorbent can be brought to the desired value without the need to process large amounts of absorbent at high pressures and high temperatures. The distillation resulting in the oxazolidone-containing fraction is preferably carried out with steam stripping at 100-200°C. The N-(2-hydroxyalkyl)amine is distilled off and the oxazolidone-containing bottom fraction thus obtained contains reduced amounts of water and alkanolamines compared to the absorbent. The invention is further illustrated by the following examples. Examples In several series of experiments, water and 3-
(2-Hydroxypropyl)-5-methyl-2-oxazolidone is stripped with steam for a period of time at various temperatures and elevated pressures, and a sample of the reactor contents is converted to diisopropanolamine. Samples were taken during the reaction so that the process could be measured. The sequential operations were as follows. For each experiment, a metered amount of water and the oxazolidone are introduced into the reactor, and the reactor is then
Air was expelled by flushing with CO2 . The temperature and therefore the pressure in the reactor was then gradually increased within 15 minutes. The steam passing through during the experiment was constantly sent from the reactor to a condensing vessel, where the condensed fraction was collected. After reaching the desired temperature, samples were taken at regular intervals via a tube opening into the reactor, while the condensed fraction was discharged at the same time. The point at which the first sample was taken was always considered the starting point of the experiment. When processing the data obtained from the samples, the following effects were considered. The oxazolidone concentration in the reactor is influenced by the following three points. (1) A portion of the oxazolidone is converted to diisopropanolamine. (2) The injected water vapor may dilute or concentrate the contents of the reactor. (3) The steam also allows some of the oxazolidone to reach the condensed fraction. Because of effects (2) and (3), the fraction of oxazolidone converted to diisopropanolamine had to be measured in a special manner. That is, the distillate was calculated from the mass balance obtained by analysis of the feed to the reactor, the sample from the reactor, and the condensed fraction. During this measurement,
The oxazolidone from the condensed fraction was always considered to belong to the unconverted portion of the oxazolidone. The results are summarized in the table below.
【表】【table】
【表】【table】
【表】
〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓
〓 〓 〓 〓 〓 〓 〓 〓 〓
該表は、本発明の特許請求の範囲内にある昇圧
昇温において、該オキサゾリドンのかなりの部分
が隠当な時間内にアミンに変換され得るというこ
とを示している。[Table] 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓 〓
〓 〓 〓 〓 〓 〓 〓 〓 〓
The table shows that at elevated pressures and temperatures within the claimed scope of the present invention, a significant portion of the oxazolidone can be converted to amines within a reasonable amount of time.
Claims (1)
またはCOSを除去するための吸収剤であつてＮ
−（２−ヒドロキシアルキル）第１級および／ま
たは第２級アミンの水性溶液を包含しかつオキサ
ゾリドンで汚染されている吸収剤の再生法におい
て、該吸収剤あるいはそれから得られるオキサゾ
リドン含有留分を水の存在下昇圧において少なく
とも200℃の温度に加熱する上記方法。 ２ 該加熱温度が200゜ないし300℃である特許請
求の範囲第１項に記載の方法。 ３ 該加熱温度が200゜ないし250℃である特許請
求の範囲第２項に記載の方法。 ４ 加熱中生成したCO2を水蒸気ストリツピング
により除去する特許請求の範囲第１〜３項のいず
れか一項に記載の方法。 ５ 該加熱が10〜60気圧の圧力で起こる特許請求
の範囲第１〜４項のいずれか一項に記載の方法。 ６ オキサゾリドン含有留分を該吸収剤の一部か
ら蒸留により連続的に分離し、この留分を加熱し
かつこの留分を次いで再循環する特許請求の範囲
第１〜５項のいずれか一項に記載の方法。 ７ 該蒸留を100〜200℃において水蒸気ストリツ
ピングで行なう特許請求の範囲第６項に記載の方
法。[Claims] 1. CO2 and / or CO2 from two or more gases
Or an absorbent for removing COS and N
- (2-Hydroxyalkyl) In a process for regenerating an absorbent containing an aqueous solution of a primary and/or secondary amine and contaminated with oxazolidone, the absorbent or the oxazolidone-containing fraction obtained therefrom is The above method of heating to a temperature of at least 200°C at elevated pressure in the presence of. 2. The method according to claim 1, wherein the heating temperature is 200° to 300°C. 3. The method according to claim 2, wherein the heating temperature is 200° to 250°C. 4. The method according to any one of claims 1 to 3, wherein CO2 generated during heating is removed by steam stripping. 5. A method according to any one of claims 1 to 4, wherein said heating occurs at a pressure of 10 to 60 atmospheres. 6. Any one of claims 1 to 5, characterized in that an oxazolidone-containing fraction is continuously separated by distillation from a portion of the absorbent, this fraction is heated and this fraction is then recycled. The method described in. 7. The method according to claim 6, wherein the distillation is carried out by steam stripping at 100-200°C.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7702650A NL7702650A (en) | 1977-03-11 | 1977-03-11 | PROCESS FOR THE REGENERATION OF AN ALKANOLAMINE-BASED SOLVENT FOR GASES CONTAINING CO2 AND / OR COS. |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS53113290A JPS53113290A (en) | 1978-10-03 |
| JPS6139092B2 true JPS6139092B2 (en) | 1986-09-02 |
Family
ID=19828153
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2608678A Granted JPS53113290A (en) | 1977-03-11 | 1978-03-09 | Regeneration of alkanol amine based absorbent for gases containing co2 and*or cos |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS53113290A (en) |
| BR (1) | BR7801458A (en) |
| CA (1) | CA1104996A (en) |
| DE (1) | DE2810249C2 (en) |
| FR (1) | FR2382922A1 (en) |
| GB (1) | GB1572682A (en) |
| NL (1) | NL7702650A (en) |
| NO (1) | NO146184C (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4282193A (en) | 1980-02-19 | 1981-08-04 | Exxon Research & Engineering Co. | Process for converting cyclic urea to corresponding diamine in a gas treating system |
| US4282194A (en) | 1980-02-19 | 1981-08-04 | Exxon Research & Engineering Co. | Process for converting cyclic urea to corresponding diamine in a gas treating system |
| US4514379A (en) * | 1983-06-28 | 1985-04-30 | Union Oil Company Of California | Catalytic process for converting 2-oxazolidinones to their corresponding alkanolamines |
| US5137702A (en) * | 1988-12-22 | 1992-08-11 | Mobil Oil Corporation | Regeneration of used alkanolamine solutions |
| US5108551A (en) * | 1990-12-17 | 1992-04-28 | Mobil Oil Corporation | Reclamation of alkanolamine solutions |
| CN1035103C (en) * | 1992-12-24 | 1997-06-11 | 四川化工总厂 | Method for removing carbon dioxide from mixed gas |
| EP0918049A1 (en) * | 1997-10-27 | 1999-05-26 | Shell Internationale Researchmaatschappij B.V. | Process for the purification of an alkanolamine |
| NO20023050L (en) | 2002-06-21 | 2003-12-22 | Fleischer & Co | Process and facilities for carrying out the process |
-
1977
- 1977-03-11 NL NL7702650A patent/NL7702650A/en not_active Application Discontinuation
-
1978
- 1978-02-06 CA CA296,314A patent/CA1104996A/en not_active Expired
- 1978-03-09 JP JP2608678A patent/JPS53113290A/en active Granted
- 1978-03-09 BR BR7801458A patent/BR7801458A/en unknown
- 1978-03-09 FR FR7806800A patent/FR2382922A1/en active Granted
- 1978-03-09 NO NO780825A patent/NO146184C/en unknown
- 1978-03-09 GB GB9396/78A patent/GB1572682A/en not_active Expired
- 1978-03-09 DE DE2810249A patent/DE2810249C2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE2810249A1 (en) | 1978-09-14 |
| NO780825L (en) | 1978-09-12 |
| FR2382922A1 (en) | 1978-10-06 |
| CA1104996A (en) | 1981-07-14 |
| DE2810249C2 (en) | 1985-09-19 |
| NO146184B (en) | 1982-05-10 |
| GB1572682A (en) | 1980-07-30 |
| FR2382922B1 (en) | 1983-02-04 |
| JPS53113290A (en) | 1978-10-03 |
| NO146184C (en) | 1982-08-18 |
| BR7801458A (en) | 1978-10-10 |
| NL7702650A (en) | 1978-09-13 |
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