JPS63192737A - Purification and recovery of methyl ethyl ketone - Google Patents
Purification and recovery of methyl ethyl ketoneInfo
- Publication number
- JPS63192737A JPS63192737A JP62023583A JP2358387A JPS63192737A JP S63192737 A JPS63192737 A JP S63192737A JP 62023583 A JP62023583 A JP 62023583A JP 2358387 A JP2358387 A JP 2358387A JP S63192737 A JPS63192737 A JP S63192737A
- Authority
- JP
- Japan
- Prior art keywords
- ethyl ketone
- methyl ethyl
- mek
- water
- caustic soda
- 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.)
- Pending
Links
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 title claims abstract description 97
- 238000011084 recovery Methods 0.000 title claims abstract description 8
- 238000000746 purification Methods 0.000 title description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 51
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 35
- 238000004821 distillation Methods 0.000 claims abstract description 20
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 13
- 239000012535 impurity Substances 0.000 claims abstract description 8
- 239000007864 aqueous solution Substances 0.000 claims abstract description 6
- 239000002904 solvent Substances 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 12
- 238000010533 azeotropic distillation Methods 0.000 claims description 3
- 238000003795 desorption Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 abstract description 7
- 230000005484 gravity Effects 0.000 abstract description 3
- 238000010992 reflux Methods 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract 3
- 150000001875 compounds Chemical class 0.000 abstract 1
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 9
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 8
- 239000002351 wastewater Substances 0.000 description 5
- QSJXEFYPDANLFS-UHFFFAOYSA-N Diacetyl Chemical group CC(=O)C(C)=O QSJXEFYPDANLFS-UHFFFAOYSA-N 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- -1 cyclohexane gold Chemical compound 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- FDPIMTJIUBPUKL-UHFFFAOYSA-N dimethylacetone Natural products CCC(=O)CC FDPIMTJIUBPUKL-UHFFFAOYSA-N 0.000 description 2
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- JYVHOGDBFNJNMR-UHFFFAOYSA-N hexane;hydrate Chemical compound O.CCCCCC JYVHOGDBFNJNMR-UHFFFAOYSA-N 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明はメチルエチルケトン含有空気中から活性炭吸着
式溶剤回収装置によりメチルエチルケトンを精製回収す
る方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for purifying and recovering methyl ethyl ketone from air containing methyl ethyl ketone using an activated carbon adsorption type solvent recovery device.
〔従来の技術］
活性炭吸着式溶剤回収装置における従来のメチルエチル
ケトン（以下、ＭＫＫと記す）精製回収方法上第２図に
よって説明する。[Prior Art] A conventional method for purifying and recovering methyl ethyl ketone (hereinafter referred to as MKK) using an activated carbon adsorption type solvent recovery device will be explained with reference to FIG.
ＭＫＫ含有空気（以下、鳳ガスと言う）はガスブロア１
により吸着槽２−１又は２−２に送られ原ガス中のＭＩ
Ｋは吸着槽２−１又は２−２内の活性炭３−１又は３−
２に吸着捕集される。MKK-containing air (hereinafter referred to as Otori gas) is supplied by gas blower 1.
MI in the raw gas is sent to adsorption tank 2-1 or 2-2 by
K is activated carbon 3-1 or 3- in adsorption tank 2-1 or 2-2
2 is adsorbed and collected.
活性炭３−１又は３−２のＭＩＩＩＫ吸着量が限界にな
ると原ガスを停止し吸着槽２−１又は２−２に水蒸気上
投入し、活性ｌ１ｔ５−１又は３−２に吸着したＭ Ｉ
ｎ Ｋ を脱着させる。脱着したＭＩＫ蒸気は水蒸気と
ともに７ラツシユタンク４に流れ、ここで後記のセパレ
ータ６からの排水と気液接触し、排水中に溶解している
ＭＩＩｉＫｔ−蒸発回収させる。さらにこ＼でＭＩＸ蒸
気は苛性ソーダと気液接触し、ＭＩＫ中の不純物である
シア七チルを分解除去する。When the amount of MIIIK adsorbed on the activated carbon 3-1 or 3-2 reaches its limit, the raw gas is stopped and the MIIIK adsorbed on the activated carbon 5-1 or 3-2.
Detach n K . The desorbed MIK vapor flows together with water vapor into the 7-lush tank 4, where it comes into gas-liquid contact with the waste water from the separator 6, which will be described later, and evaporates and recovers the MIIiKt dissolved in the waste water. Furthermore, the MIX vapor comes into gas-liquid contact with caustic soda to decompose and remove the impurities in MIK, i.e., cyanatyl.
ここでＭＩＫ中の不純物であるジアセチル拡Ｍｌ！ＩＫ
が活性炭３−１又嬬３−２で吸脱着する際、活性炭３−
１又は３−２の触媒作用にょ９ＭｌＩＣの一部が分解し
生成するものである。Here, diacetyl expansion Ml, which is an impurity in MIK! IK
When adsorbed and desorbed by activated carbon 3-1 or 3-2, activated carbon 3-
A part of 9MlIC is decomposed and produced by the catalytic action of 1 or 3-2.
フラッシュタンク４會出７ｊ Ｍ Ｉ Ｋ蒸気及び水蒸
気はコンデンサ５に流れ凝縮冷却される。この凝縮液は
セパレータ６に流れ、ＭＪＣＫと水に比重分離する。水
は一部ＭＢＫが平衡溶解しているので、前記フラッシュ
メンク４に流しＭｆｆｉＫを回収する。The flash tank 4 output 7j M I K steam and water vapor flow into the condenser 5 and are condensed and cooled. This condensed liquid flows into the separator 6 and is separated into MJCK and water by specific gravity. Since MBK is partially dissolved in the water in equilibrium, it is poured into the flashmenc 4 to recover MffiK.
Ｍコに％平衡溶解量の水分を含むため、そのままでは再
利用できないため、次の方法で脱水している。Since M co contains % equilibrium dissolved amount of water, it cannot be reused as it is, so it is dehydrated using the following method.
セパレータ６から出７ｊ Ｍ ＲＫは、フィードポンプ
８により中間メンク７ｔ−経由し蒸留塔９に送る。蒸留
塔？では分離器１１に注入され九シクロヘキサンにより
抽出蒸留が行われ、ＭＩＫ。7j M RK output from the separator 6 is sent to the distillation column 9 via an intermediate membrane 7t- by a feed pump 8. Distillation tower? Then, it is injected into the separator 11 and subjected to extractive distillation using nine cyclohexane, resulting in MIK.
水、シクロヘキサンの３成分共沸物が蒸留塔々頂から出
てり７ラツクスコンデン？１０Ｋ１５ｔｎ、凝縮された
後分離器１１に流れる０分組１１では液々平衡によシ水
と溶剤ＣＭＭＫ及びシクロヘキサン）に分離する。A three-component azeotrope of water and cyclohexane comes out from the top of the distillation column, and is it 7 lux condensate? 10K15tn is condensed and then flows into a separator 11 where it is separated into water, solvent CMMK and cyclohexane) by liquid-liquid equilibrium.
このようにシクロヘキサン金注入することによシ、蒸留
塔９及び分離器１１間で共沸！［及び液々平衡組成の差
にょシ水を糸外へ排出するものである。By injecting cyclohexane gold in this way, azeotropic distillation occurs between the distillation column 9 and the separator 11! [Due to the difference in liquid-liquid equilibrium composition, water is discharged to the outside of the yarn.
従来の方法において
１）ＭＩＫＩＣ中の水分を除去するために注入するシク
ロへΦサンかＭＫＫに混入し、再利用に問題を生じる場
合かある。In the conventional method, 1) Φ-san may be mixed into MKK when injected to remove water from MIKIC, causing problems in reuse.
２〕 蒸留塔内が３成分の気液平衡になるため、運転制
御か複雑になる。2) Since there is a vapor-liquid equilibrium of three components in the distillation column, operation control becomes complicated.
３）蒸留塔内にシクロヘキサンが多量還流するため、蒸
留塔での蒸気消費ｔか多くなシランユングコストが高く
つく。3) Since a large amount of cyclohexane is refluxed into the distillation column, the steam consumption in the distillation column is large, resulting in high silane costs.
４）ＭＩＫ中のジアセチル除去専用に苛性ソーダが必要
である几め、ランニングコストがかかる。4) Caustic soda is required exclusively for removing diacetyl from MIK, which increases running costs.
５）シクロヘキサンの替わ）にトルエンを注入し水を抽
出除去する方法もあるが、ＭＪｌｆＫとトルエンを分離
する蒸留塔が別に必要になる。5) There is also a method of injecting toluene into cyclohexane (instead of cyclohexane) to extract and remove water, but this requires a separate distillation column to separate MJlfK and toluene.
本発明は従来のＭＩＫの精製回収方法における上述した
不具合を屏消しうるＭＪｅｌｃの精製回収方法上提供し
ようとするものである。゛〔問題点を解決する次めの手
段〕
本発明は、メチルエチルケト７を含有する空気中から活
性炭吸着式溶剤回収装置によ）メチルエチルケトンを回
収する方法において、活性炭に吸着したメチルエチルケ
トンを水蒸気等で脱着し、凝縮回収したメチルエチルケ
トンを蒸留塔に送）、メチルエチルケトン中にｆ！Ｉｓ
している水分を共沸蒸留させ、この共沸液に苛性ソーダ
又は苛性ソーダ水ｇ＊ｖ注入することによジメチルエチ
ルケトン中に溶解している水分を抽出分離させ、水分を
抽出されたメチルエチルケトンは蒸留塔に還流させ、一
方抽出した水分を含む苛性ソーダ溶液は前記脱着工程で
活性炭から脱着したメチルエチルケトン蒸気と気液接触
させ、メチルエチルケトン中に含まれる不純物を分解除
去することを特徴とするメチルエチルケトンの精製回収
方法である。The present invention aims to provide a method for purifying and recovering MJelc that can eliminate the above-mentioned problems in conventional methods for purifying and recovering MIK. [Next means for solving the problem] The present invention provides a method for recovering methyl ethyl ketone from air containing methyl ethyl ketone (using an activated carbon adsorption solvent recovery device), in which methyl ethyl ketone adsorbed on activated carbon is desorbed by water vapor or the like. Then, the condensed and collected methyl ethyl ketone is sent to a distillation column), and f! Is
The water dissolved in dimethyl ethyl ketone is extracted and separated by azeotropic distillation of the water dissolved in dimethyl ethyl ketone by injecting g*v of caustic soda or caustic soda water into this azeotropic liquid, and the methyl ethyl ketone from which water has been extracted is passed through a distillation column. A method for purifying and recovering methyl ethyl ketone, characterized in that the extracted caustic soda solution containing water is brought into gas-liquid contact with the methyl ethyl ketone vapor desorbed from the activated carbon in the desorption step, and impurities contained in the methyl ethyl ketone are decomposed and removed. be.
水元明嫁、ＭＩＫを蒸留塔に送１ｉｌＫ中に溶解してい
る水分全共沸蒸留させ、この共沸液（水含有ＭＰＩＫλ
に笥性ソーダ水溶液ｔ−注入するものである。これは苛
性ンーダの吸水性を利用し、ＭＩＫ中に溶解している水
分を抽出分離するもので、従来のシクロヘキサノ、トル
エン等の抽出剤よシ効来が高い。Mizumoto Akiyome sends MIK to a distillation column and azeotropically distills all the water dissolved in ilK, and this azeotropic liquid (water-containing MPIKλ
An aqueous solution of soda is injected into the tank. This extracts and separates water dissolved in MIK by utilizing the water absorbing properties of caustic powder, and is more effective than conventional extractants such as cyclohexano and toluene.
さらに、この苛性ソーダ水溶１１ＭＫＫ中の不純物上分
解除去するのに利用するものである。Furthermore, it is used to decompose and remove impurities in this aqueous solution of caustic soda 11MKK.
本発明によるＭＩＫ、Ｋｎ製回収方法の一実施態様を第
１図によって説明する。An embodiment of the method for recovering MIK and Kn products according to the present invention will be explained with reference to FIG.
ここでＭＭＫ含有空気（以下、原ガスと言う）はガスブ
ロア１により吸着槽２−１又は２−２に送られ鳳ガス中
のＭＩＫは吸着槽内の活性炭３−１又は３−２に吸着捕
集される。（吸着工程）
活性炭３−１又は３−２のＭＩＸ吸着食が限界になると
原ガス七停止し、吸着槽２−１又は２−２に水蒸気を投
入し、活性炭３−１又扛５−２に吸着したＭＩＫｔ−脱
着させる。（脱着工程）
脱着したＭＩＣＫ蒸気は水蒸気とともに７ラツシユタン
ク４に流れ、仁こで後記のセパレータ６からの排水と気
液接触し、排水中に溶解しているＭＩＫｔ−蒸発回収さ
せる。さらにＭＩＸ蒸気は後記の分離器１１からの苛性
ソーダ水溶液と気液接触し、ＭＩＫ中の不純物であるジ
アセチルを分解除去する。フラッシュタンク４ｔ″出ｆ
ｔ；−Ｍ Ｉ Ｋ蒸気及び水蒸気はコンデンサ５に流れ
凝縮冷却される。この凝縮液はセパレータ６に流れ、Ｍ
ＩＫと水に比重分離する。水は一部ＭＢＫが平衡溶解し
ているので、前記のとお夛７ラツシユタンク４に流れＭ
ＩＸを回収する。Here, MMK-containing air (hereinafter referred to as raw gas) is sent to an adsorption tank 2-1 or 2-2 by a gas blower 1, and MIK in the Otori gas is adsorbed and captured by activated carbon 3-1 or 3-2 in the adsorption tank. collected. (Adsorption process) When the MIX adsorption of activated carbon 3-1 or 3-2 reaches its limit, the raw gas is stopped, water vapor is introduced into adsorption tank 2-1 or 2-2, and activated carbon 3-1 or 5-2 is heated. MIKt adsorbed on - is desorbed. (Desorption step) The desorbed MICK vapor flows together with water vapor into the 7-lush tank 4, where it comes into gas-liquid contact with the waste water from the separator 6, which will be described later, to evaporate and recover MIKt dissolved in the waste water. Further, the MIX vapor comes into gas-liquid contact with an aqueous solution of caustic soda from a separator 11, which will be described later, to decompose and remove diacetyl, which is an impurity in MIK. Flash tank 4t'' output f
t;-M I K vapor and water vapor flow into the condenser 5 and are condensed and cooled. This condensate flows into separator 6 and M
Gravity separation into IK and water. Since some MBK is dissolved in equilibrium in the water, it flows into the above-mentioned 7-lush tank 4.
Collect IX.
ＭＩＫも平衡溶解量の水分を含む九め、フィードポンプ
８によシ中関タンク７ｔ−経由して蒸留塔９に送る。蒸
留塔９でＭＩＫ中の水分は共沸組成のＭＪ！ｌＫととも
に蒸留塔々頂から出てリフラックスコンデンサ１０に流
れ凝縮された後分離器１１に流れる。ここで仁の分離器
１１に供給される苛性ソーダ水浴液によ？）、ｍｚｘに
＃！屏している水分が抽出し苛性ソーダ水浴液に溶解す
る。水が除去され九ＭＩＫは蒸留塔９に還流する。脱水
されたＭｆｆｉＫは蒸留塔々底から系外に回収される。MIK, which also contains an equilibrium dissolved amount of water, is sent to the distillation column 9 by the feed pump 8 via the Nakaseki tank 7t. The water in MIK in distillation column 9 has an azeotropic composition of MJ! It exits from the top of the distillation column together with lK, flows to a reflux condenser 10, is condensed, and then flows to a separator 11. Here, the caustic soda water bath liquid supplied to the separator 11 is used. ), # to mzx! The trapped water is extracted and dissolved in the caustic soda water bath. Water is removed and the 9MIK is refluxed to distillation column 9. The dehydrated MffiK is recovered outside the system from the bottom of the distillation columns.
一方分離器１１でＭＩＩＩＫ中の水を溶解した苛性ソー
ダ水溶液はフラッシュタック４に流れ、前記のとおｊｊ
）ＭＪＣ１Ｃ中のジアセチルを分解除去し排水とともに
系外に排出される。On the other hand, the caustic soda aqueous solution in which the water in MIIIK was dissolved in the separator 11 flows to the flash tack 4 and is
) Diacetyl in MJC1C is decomposed and removed and discharged from the system along with waste water.
１）純度の高いＭ８区か回収できる。（シクロヘキサン
等の抽出剤の混入がなりｈ）
２）ランニングコストが少なくなる。（１〜３割程度）
３）他の抽出剤（シクロヘキサン等〕に比べ運転制御か
容易。1) Highly pure M8 can be recovered. (No contamination with extractants such as cyclohexane.) 2) Running costs are reduced. (approximately 10% to 30%) 3) Easier to control operation compared to other extractants (cyclohexane, etc.).
第１図は本発明のＭＩＫ精製回収方法の一実施例を説明
する九めの図、第２図は従来法によるＭＫＩｍ精製回収
方法を説明するための図である。FIG. 1 is the ninth diagram for explaining an embodiment of the MIK purification and recovery method of the present invention, and FIG. 2 is a diagram for explaining the MKIm purification and recovery method according to the conventional method.
Claims (1)
溶剤回収装置によりメチルエチルケトンを回収する方法
において、活性炭に吸着したメチルエチルケトンを水蒸
気等で脱着し、凝縮回収したメチルエチルケトンを蒸留
塔に送りメチルエチルケトン中に溶解している水分を共
沸蒸留させ、この共沸液に苛性ソーダ又は苛性ソーダ水
溶液を注入することによりメチルエチルケトン中に溶解
している水分を抽出分解させ、水分を抽出されたメチル
エチルケトンは蒸留塔に還流させ、一方抽出した水分を
含む苛性ソーダ溶液は前記脱着工程で活性炭から脱着し
たメチルエチルケトン蒸気と気液接触させ、メチルエチ
ルケトン中に含まれる不純物を分解除去することを特徴
とするメチルエチルケトンの精製回収方法。In a method of recovering methyl ethyl ketone from air containing methyl ethyl ketone using an activated carbon adsorption solvent recovery device, the methyl ethyl ketone adsorbed on the activated carbon is desorbed with water vapor, etc., and the collected methyl ethyl ketone is sent to a distillation column to remove the water dissolved in the methyl ethyl ketone. is subjected to azeotropic distillation, and the water dissolved in methyl ethyl ketone is extracted and decomposed by injecting caustic soda or an aqueous solution of caustic soda into this azeotropic liquid, and the methyl ethyl ketone from which water has been extracted is refluxed to a distillation column. A method for purifying and recovering methyl ethyl ketone, characterized in that the caustic soda solution containing the above is brought into gas-liquid contact with the methyl ethyl ketone vapor desorbed from activated carbon in the desorption step to decompose and remove impurities contained in the methyl ethyl ketone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62023583A JPS63192737A (en) | 1987-02-05 | 1987-02-05 | Purification and recovery of methyl ethyl ketone |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62023583A JPS63192737A (en) | 1987-02-05 | 1987-02-05 | Purification and recovery of methyl ethyl ketone |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63192737A true JPS63192737A (en) | 1988-08-10 |
Family
ID=12114597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62023583A Pending JPS63192737A (en) | 1987-02-05 | 1987-02-05 | Purification and recovery of methyl ethyl ketone |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63192737A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040496A (en) * | 2010-12-29 | 2011-05-04 | 天津市康科德科技有限公司 | Purification method of high-purity organic solvent 4-methyl-2-pentanone |
| CN102040497A (en) * | 2010-12-29 | 2011-05-04 | 天津市康科德科技有限公司 | Purification method of high-purity organic solvent butanone |
| JP2019030826A (en) * | 2017-08-04 | 2019-02-28 | 東洋紡株式会社 | Organic solvent recovery system |
-
1987
- 1987-02-05 JP JP62023583A patent/JPS63192737A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102040496A (en) * | 2010-12-29 | 2011-05-04 | 天津市康科德科技有限公司 | Purification method of high-purity organic solvent 4-methyl-2-pentanone |
| CN102040497A (en) * | 2010-12-29 | 2011-05-04 | 天津市康科德科技有限公司 | Purification method of high-purity organic solvent butanone |
| JP2019030826A (en) * | 2017-08-04 | 2019-02-28 | 東洋紡株式会社 | Organic solvent recovery system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| MY141870A (en) | Extraction process for removal of impurities from mother liquor in the synthesis of carboxylic acid | |
| RU2007102276A (en) | METHOD FOR REMOVING IMPURITIES FROM MATTER LIQUID WHEN SYNTHESIS OF CARBOXYLIC ACID USING FILTERING UNDER PRESSURE | |
| JPH041147A (en) | Separation of impurities in aqueous solution of crude ethanol | |
| PT2292581E (en) | Extraction process for removal of impurities from mother liquor in the synthesis of terephthalic acid | |
| EP1405662A3 (en) | CO2 recovery process for supercritical extraction | |
| CN116444364A (en) | Treatment process for mother liquor extract of refined terephthalic acid oxidation unit | |
| JP4681192B2 (en) | Wastewater purification in the case of the manufacturing method of formic anhydride | |
| JPH041793B2 (en) | ||
| JP2002526462A5 (en) | ||
| CA1084527A (en) | Process for preparing guanidine | |
| CN103864689B (en) | A kind of method of the condensate liquid obtained in the evaporative crystallization steps of purification of aqueous ammonium sulfate phase | |
| JPS63192737A (en) | Purification and recovery of methyl ethyl ketone | |
| JP2965617B2 (en) | Purification method of waste gas with high chloride content | |
| JP2002526463A5 (en) | ||
| JPH10314530A (en) | Method for purifying gas loaded with dust | |
| US3965243A (en) | Recovery of sodium thiocyanate | |
| US4596587A (en) | Separation of a mixture which consists of organic compounds and water and is obtained in solvent recovery by adsorption and desorption | |
| US4049782A (en) | Process for producing pure concentrated ammonia | |
| WO2001027120A2 (en) | Method and apparatus for purifying low grade acetonitrile and other constituents from hazardous waste | |
| JPH01139124A (en) | Method for recovering and purifying ketone solvent | |
| JP4345082B2 (en) | Method for purifying high-purity dimethyl sulfoxide and a mixture of dimethyl sulfoxide and amines | |
| JPH0143380Y2 (en) | ||
| JPS634826A (en) | Azeotropic distilling plant | |
| JPH06228126A (en) | Synthesis of trioxane | |
| JP2510645B2 (en) | Method for removing wastewater from coke factory |