JPH01299244A - Method for purifying acetone - Google Patents
Method for purifying acetoneInfo
- Publication number
- JPH01299244A JPH01299244A JP12912888A JP12912888A JPH01299244A JP H01299244 A JPH01299244 A JP H01299244A JP 12912888 A JP12912888 A JP 12912888A JP 12912888 A JP12912888 A JP 12912888A JP H01299244 A JPH01299244 A JP H01299244A
- Authority
- JP
- Japan
- Prior art keywords
- acetone
- aqueous solution
- alkali
- distillation column
- aldehydes
- 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.)
- Granted
Links
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000004821 distillation Methods 0.000 claims abstract description 34
- 239000007864 aqueous solution Substances 0.000 claims abstract description 31
- 150000001299 aldehydes Chemical class 0.000 claims abstract description 29
- 239000003513 alkali Substances 0.000 claims abstract description 27
- 150000001298 alcohols Chemical class 0.000 claims abstract description 13
- 238000005882 aldol condensation reaction Methods 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 238000000746 purification Methods 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 abstract description 7
- 238000011084 recovery Methods 0.000 abstract description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 239000011541 reaction mixture Substances 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 24
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 238000010992 reflux Methods 0.000 description 13
- 239000002994 raw material Substances 0.000 description 11
- 238000009835 boiling Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000005575 aldol reaction Methods 0.000 description 4
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- QTWJRLJHJPIABL-UHFFFAOYSA-N 2-methylphenol;3-methylphenol;4-methylphenol Chemical compound CC1=CC=C(O)C=C1.CC1=CC=CC(O)=C1.CC1=CC=CC=C1O QTWJRLJHJPIABL-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N butyric aldehyde Natural products CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 3
- 229930003836 cresol Natural products 0.000 description 3
- 238000010543 cumene process Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- QIGBRXMKCJKVMJ-UHFFFAOYSA-N Hydroquinone Chemical compound OC1=CC=C(O)C=C1 QIGBRXMKCJKVMJ-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical compound CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-M hydroperoxide group Chemical group [O-]O MHAJPDPJQMAIIY-UHFFFAOYSA-M 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- GHMLBKRAJCXXBS-UHFFFAOYSA-N resorcinol Chemical compound OC1=CC=CC(O)=C1 GHMLBKRAJCXXBS-UHFFFAOYSA-N 0.000 description 2
- 230000002441 reversible effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- FRIBMENBGGCKPD-UHFFFAOYSA-N 3-(2,3-dimethoxyphenyl)prop-2-enal Chemical compound COC1=CC=CC(C=CC=O)=C1OC FRIBMENBGGCKPD-UHFFFAOYSA-N 0.000 description 1
- AMIMRNSIRUDHCM-UHFFFAOYSA-N Isopropylaldehyde Chemical compound CC(C)C=O AMIMRNSIRUDHCM-UHFFFAOYSA-N 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 125000000217 alkyl group Chemical class 0.000 description 1
- -1 alkyl hydroperoxides Chemical class 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229930007927 cymene Natural products 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明はアルデヒド類、アルコール類等を含むアセトン
の精製方法、特にクメン法において生成するアセトンの
精製方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a method for purifying acetone containing aldehydes, alcohols, etc., and particularly to a method for purifying acetone produced in the cumene process.
アルキル基を核置換した（またはしない）芳香族炭化水
素を酸化して、アルキルヒドロペルオキシドを得、これ
を酸分解してケトンとフェノール類を製造する方法はク
メン法として知られている。The method of oxidizing aromatic hydrocarbons with (or without) nuclear substitution of alkyl groups to obtain alkyl hydroperoxides, which are then decomposed with acids to produce ketones and phenols, is known as the cumene method.
この方法において、ヒドロペルオキシドを酸分解して得
られる生成物を蒸留により取得される粗アセトンには、
一般にアルデヒド類、アルコール類などの種々の不純物
が含有されている。このため酸分解生成物をトッピング
蒸留して得られた粗アセトンをそのまま精留してもアル
デヒド類やアルコール類が精製アセトンに混入し、アセ
トンの純度１品質が低下する。In this method, crude acetone obtained by distilling the product obtained by acid decomposition of hydroperoxide is
Generally, various impurities such as aldehydes and alcohols are contained. Therefore, even if the crude acetone obtained by topping distillation of the acid decomposition product is directly rectified, aldehydes and alcohols will be mixed into the purified acetone, and the purity 1 quality of the acetone will be degraded.
従来、クメンヒドロペルオキシドの接触分解によりフェ
ノールとアセトンを得る場合、生成する粗アセトンから
アルデヒド類等の不純物を除去するために、粗アセトン
にアルカリ水溶液を加え、アルデヒド類をアルドール縮
合させて高沸点物に転化した後、アセトンを蒸留回収す
る方法が採用されている（特公昭４９−２７５６５号）
。Conventionally, when phenol and acetone are obtained by catalytic cracking of cumene hydroperoxide, in order to remove impurities such as aldehydes from the crude acetone produced, an alkaline aqueous solution is added to the crude acetone, and the aldehydes are subjected to aldol condensation to produce high-boiling substances. A method has been adopted in which acetone is recovered by distillation after conversion to
.
第２図はこのような従来のアセトンの精製方法を示す系
統図である１図において、１は多段の蒸留塔で、内部に
多数の棚段Ｔ１〜Ｔ０を備えている。従来の精製方法は
、蒸留塔１の第１段Ｔ１より下に水蒸気を蒸気供給管２
から供給し、その７〜１０段上例えば第７段Ｔ７に粗ア
セトンを原料供給管３から供給し、塔底より１５〜２０
段上例えば第１７段Ｔ１７にアルカリ水溶液をアルカリ
供給管４から供給する。そして原料供給管３が接続する
第７段Ｔ、と、アルカリ供給管４が接続する第１７段Ｔ
１７との間に形成された反応域Ｒにおいて、アルデヒド
をアルドール縮合させて高沸点物に転化し、精製アセト
ンを塔頂配管５から蒸留回収するとともに、塔底配管６
から高沸点物を含むアルカリ水溶液を排出する。精製ア
セトンは凝縮器７で液化して回収管８から回収し、一部
を還流管９から塔頂へ還流する。FIG. 2 is a system diagram showing such a conventional acetone purification method. In FIG. 1, 1 is a multi-stage distillation column, which is equipped with a large number of trays T1 to T0. In the conventional purification method, water vapor is passed through a steam supply pipe 2 below the first stage T1 of the distillation column 1.
Crude acetone is supplied from the raw material supply pipe 3 to 7 to 10 stages above, for example, the seventh stage T7, and 15 to 20
An aqueous alkali solution is supplied from the alkali supply pipe 4 to the upper stage, for example, the 17th stage T17. and a seventh stage T to which the raw material supply pipe 3 is connected, and a seventeenth stage T to which the alkali supply pipe 4 is connected.
17, aldehyde is subjected to aldol condensation to convert it into a high-boiling point product, and purified acetone is distilled and recovered from the column top pipe 5, and the column bottom pipe 6
The alkaline aqueous solution containing high boiling point substances is discharged from the tank. The purified acetone is liquefied in the condenser 7 and recovered from the recovery tube 8, and a portion is refluxed to the top of the column through the reflux tube 9.
しかしながら、このような従来の精製方法では。However, such conventional purification methods.
アルドール反応が可逆反応であるため、蒸留条件、塔底
組成などにより逆反応が起こり、微量のアルデヒド類が
精製アセトン中に同伴することを防止できない欠点があ
った。Since the aldol reaction is a reversible reaction, the reverse reaction occurs depending on the distillation conditions, bottom composition, etc., and there is a drawback that it is not possible to prevent trace amounts of aldehydes from being entrained in purified acetone.
例えば、アセトン回収率を上げることを目的として蒸留
温度を高めると、蒸留塔１で高沸点物が解縮合してアル
デヒドに戻り、精製アセトンにアルデヒドが混入するた
め、アルカリ水溶液の残留アセトン濃度を１０〜１５重
量％に保つ必要があった。For example, when the distillation temperature is raised to increase the acetone recovery rate, high-boiling substances decondense in distillation column 1 and return to aldehyde, and the aldehyde is mixed into purified acetone, reducing the residual acetone concentration in the alkaline aqueous solution to 10 It was necessary to keep it at ~15% by weight.
その結果、精製アセトンの回収率が低くなるとともに、
排水中のアセトン濃度が高くなるため、このアセトンを
回収する設備が必要となる。また、粗アセトン中のメタ
ノールはアセトンと共沸組成を作るため、そのまま蒸留
しても分離できないという欠点があった。As a result, the recovery rate of purified acetone becomes low, and
As the concentration of acetone in wastewater increases, equipment to recover this acetone is required. Furthermore, since methanol in crude acetone forms an azeotropic composition with acetone, it has the disadvantage that it cannot be separated by distillation.
本発明の目的は、上記問題点を解決するため。 The purpose of the present invention is to solve the above problems.
アルドール反応により生成する高沸点物の解縮合反応で
生成した微量のアルデヒド類の除去と、粗アセトン中に
含まれるメタノールの除去を同時に行うことができ、ア
ルデヒドおよびメタノール含有率の低い精製アセトンを
簡単なプロセスにより、容易に得ることができるアセト
ン精製方法を提案することである。It is possible to simultaneously remove trace amounts of aldehydes generated by the decondensation reaction of high-boiling substances generated by the aldol reaction and methanol contained in crude acetone, making it easy to produce purified acetone with low aldehyde and methanol content. The purpose of the present invention is to propose a method for purifying acetone that can be easily obtained through a process.
本発明は次のアセトン精製方法である。 The present invention is the following acetone purification method.
（１）アルデヒド類およびアルコール類を含有する粗ア
セトンとアルカリ水溶液とを混合して、アルドール縮合
反応を完結させた後、蒸留塔へ供給して蒸留し、その供
給段より高い位置にさらにアルカリ水溶液を供給して、
解縮合反応により生成するアルデヒド類およびアルコー
ル類を除去することを特徴とするアセトン精製方法。(1) After mixing crude acetone containing aldehydes and alcohols with an alkaline aqueous solution and completing the aldol condensation reaction, it is supplied to a distillation column for distillation, and an alkali aqueous solution is added at a position higher than the feed stage. by supplying
An acetone purification method characterized by removing aldehydes and alcohols produced by a decondensation reaction.
（２）蒸留塔から取出される精製アセトンを凝縮させ、
その一部を蒸留塔へ還流させるようにした上記（１）記
載の方法。(2) Condensing purified acetone taken out from the distillation column,
The method according to (1) above, wherein a part of the water is refluxed to the distillation column.
（３）蒸留塔から取出されるアルカリ水溶液の一部を加
熱して蒸留塔へ還流させるようにした上記（１）または
（２）記載の方法。(3) The method described in (1) or (2) above, wherein a part of the alkaline aqueous solution taken out from the distillation column is heated and refluxed to the distillation column.
本発明において精製の対象となる粗アセトンは、アルデ
ヒド類およびアルコール類を含むアセトンであり、クメ
ン法によりヒドロペルオキシドを酸分解して得られる粗
アセトンがある。このクメン法としては、アルキル置換
した（またはしない）芳香族炭化水素からフェノール、
クレゾール、ハイドロキノン、レゾルシン等のフェノー
ル類を得る場合のいずれにも適用できるが、特にクレゾ
ールを得る場合に適している。The crude acetone to be purified in the present invention is acetone containing aldehydes and alcohols, and includes crude acetone obtained by acid decomposition of hydroperoxide by the cumene method. This cumene process involves converting phenol from alkyl-substituted (or not) aromatic hydrocarbons.
Although it can be applied to any case of obtaining phenols such as cresol, hydroquinone, and resorcinol, it is particularly suitable for obtaining cresol.
アルカリ水溶液としては、水酸化ナトリウム、水酸化カ
リウムなど任意のアルカリの水溶液が使用できるが、特
に水酸化ナトリウムが好ましい。As the alkaline aqueous solution, any alkaline aqueous solution such as sodium hydroxide and potassium hydroxide can be used, but sodium hydroxide is particularly preferred.
クメン法において、例えばサイメンヒドロペルオキシド
を酸分解した場合には、生成物中にアセトン、クレゾー
ルの他に不純物としてアセトアルデヒド、プロピオンア
ルデヒド、ｎ−ブチルアルデヒド、ｉ−ブチルアルデヒ
ドおよびメタノールなどが含有されている。従って、こ
の生成物をトッピング蒸留して得られる粗アセトン中に
は、上記アルデヒド類、アルコール類等の不純物が含ま
れる。In the cumene process, for example, when cymene hydroperoxide is acid-decomposed, the product contains impurities such as acetaldehyde, propionaldehyde, n-butyraldehyde, i-butyraldehyde, and methanol in addition to acetone and cresol. . Therefore, the crude acetone obtained by topping distillation of this product contains impurities such as the above-mentioned aldehydes and alcohols.
本発明では、これらの不純物を除去するために、粗アセ
トンにアルカリ水溶液を２段階にわたって接触させてア
ルドール縮合反応を行う。In the present invention, in order to remove these impurities, crude acetone is brought into contact with an alkaline aqueous solution over two stages to carry out an aldol condensation reaction.
以下、本発明の好ましい精製方法を図面により説明する
。第１図は本発明の実施態様を示す系統図であり、第２
図と同一符号は同一または相当部分を示す。蒸留塔１は
５５段の棚段Ｔ１〜Ｔｓｓを有している。Hereinafter, a preferred purification method of the present invention will be explained with reference to the drawings. FIG. 1 is a system diagram showing an embodiment of the present invention, and FIG.
The same reference numerals as in the figures indicate the same or corresponding parts. The distillation column 1 has 55 plates T1 to Tss.
アセトンの精製方法は、原料供給管３から粗アセトンを
供給し、アルカリ供給管４ａからアルカリ水溶液を供給
し、原料供給管３内で混合してアルドール縮合反応を完
結させる。このときメタノール等のアルコール類もアル
カリ水溶液側に移行する。そして塔底配管６から取出さ
れるアルカリ水溶液を加熱器１１で加熱し、還流管１２
から原料供給管３に供給して反応液と混合し、蒸留塔１
の第２〜８段、例えば第６段Ｔ６に供給して蒸留を行う
。In the method for purifying acetone, crude acetone is supplied from the raw material supply pipe 3, an aqueous alkali solution is supplied from the alkali supply pipe 4a, and the mixture is mixed in the raw material supply pipe 3 to complete the aldol condensation reaction. At this time, alcohols such as methanol also move to the alkaline aqueous solution side. Then, the alkaline aqueous solution taken out from the tower bottom pipe 6 is heated by the heater 11, and the reflux pipe 12
is supplied to the raw material supply pipe 3, mixed with the reaction liquid, and then sent to the distillation column 1.
is supplied to the second to eighth stages, for example, the sixth stage T6, for distillation.
一方、その２〜２０段、好ましくは４〜８段上、例えば
第１０段Ｔ１゜に別のアルカリ供給管４ｂからアルカリ
水溶液を供給する。On the other hand, an alkali aqueous solution is supplied from another alkali supply pipe 4b to 2 to 20 stages, preferably 4 to 8 stages above, for example, the 10th stage T1°.
蒸留塔１ではアルドール縮合反応により生成する高沸点
物およびアルカリ水溶液は下向流で、アセトンおよび高
沸点物の解縮合により生成するアルデヒドは上向流で流
れる。従って原料供給管３が接続する第６段Ｔ６、およ
びアルカリ供給管４ｂが接続する第１０段Ｔ１゜の間に
形成される第２反応域Ｓにおいて、解縮合により生成す
るアルデヒドがアルドール反応により高沸点物となって
アルカリ水溶液とともに下°向流となって流下する。メ
タノール等のアルコール類もアルカリ水溶液側へ移行し
て流下する。In the distillation column 1, high boilers and aqueous alkaline solutions produced by the aldol condensation reaction flow downward, and acetone and aldehydes produced by the decondensation of high boilers flow upward. Therefore, in the second reaction zone S formed between the 6th stage T6 to which the raw material supply pipe 3 is connected and the 10th stage T1° to which the alkali supply pipe 4b is connected, the aldehyde produced by decondensation is increased by the aldol reaction. It becomes a boiling point and flows downward along with the aqueous alkali solution. Alcohols such as methanol also migrate to the alkaline aqueous solution side and flow down.
こうして、精製アセトンが塔頂配管５から取出される。In this way, purified acetone is taken out from the tower top pipe 5.
精製アセトンは凝縮器７で液化して回収管８から回収さ
れ、一部は還流管９から塔頂に還流する。還流したアセ
トンは比重が大きいため流下して再度蒸留に付され、残
留するアルデヒド、メタノール等の不純物が除去される
。このため塔頂配管５から取出されるアセトンの純度は
高くなる。The purified acetone is liquefied in the condenser 7 and recovered from the recovery tube 8, and a portion is refluxed to the top of the column through the reflux tube 9. Since the refluxed acetone has a high specific gravity, it flows down and is subjected to distillation again to remove remaining impurities such as aldehyde and methanol. Therefore, the purity of the acetone taken out from the tower top pipe 5 becomes high.
また塔底配管６から取出されるアルカリ水溶液の一部は
加熱器１１で加熱されて還流するが、これによりアルカ
リ水溶液に含まれる解縮合したアルデヒドやアセトン等
は蒸留により除去され、アセトン回収率は高くなる。Also, a part of the alkaline aqueous solution taken out from the bottom pipe 6 is heated by the heater 11 and refluxed, but decondensed aldehyde, acetone, etc. contained in the alkaline aqueous solution are removed by distillation, and the acetone recovery rate is reduced. It gets expensive.
上記の精製方法では、原料供給管３において。In the above purification method, in the raw material supply pipe 3.
粗アセトンと主要部のアルカリ水溶液を混合して、２０
〜６０℃、好ましくは３０〜５０℃の温度で１０秒〜１
０分、好ましくは１〜５分間接触させ、アルドール反応
を完結させた後、蒸留塔へ供給して蒸留を行う。この際
のアルカリ水溶液の濃度は０．１〜５重量％、好ましく
は０．５〜１重量％、混合液のＷ１０重量比（注１）は
、０．０５〜１、好ましくは０．０７〜０．６、最も好
ましくは０．０８〜０．２、アルカリ比率（注２）は０
．０５〜１、好ましくは０．０７〜０．３、最も好まし
くは０．０８〜０．１５重量％である。Mix crude acetone and main alkali aqueous solution,
10 seconds to 1 at a temperature of ~60°C, preferably 30-50°C
After contacting for 0 minutes, preferably 1 to 5 minutes to complete the aldol reaction, the mixture is supplied to a distillation column and distilled. The concentration of the alkaline aqueous solution at this time is 0.1 to 5% by weight, preferably 0.5 to 1% by weight, and the W10 weight ratio (Note 1) of the mixed liquid is 0.05 to 1, preferably 0.07 to 1. 0.6, most preferably 0.08-0.2, alkaline ratio (Note 2) is 0
．． 05-1, preferably 0.07-0.3, most preferably 0.08-0.15% by weight.
次にアルカリ供給管４ｂから供給する残りの少量部のア
ルカリ水溶液の濃度は０．Ｏ１〜０．５重量％、好まし
くは０．０３〜０．１重量％、アルカリ供給管４ａから
供給する主要部のアルカリ水溶液に対する重量比は０．
５〜１．６、好ましくは０．７〜０．９である。またこ
の希薄アルカリ水溶液の供給速度の還流速度に対する比
は １７３４〜１１５、好ましくは１／２０〜１／１０
である。Next, the concentration of the remaining small portion of the alkaline aqueous solution supplied from the alkali supply pipe 4b is 0. O1 to 0.5% by weight, preferably 0.03 to 0.1% by weight, and the weight ratio of the main portion supplied from the alkali supply pipe 4a to the alkaline aqueous solution is 0.
5 to 1.6, preferably 0.7 to 0.9. The ratio of the supply rate of this dilute aqueous alkali solution to the reflux rate is 1734 to 115, preferably 1/20 to 1/10.
It is.
さらに還流管９からのアセトンの還流比は１〜３、好ま
しくは１．５〜２．５．また還流管１２からのアルカリ
水溶液の還流比は０．８〜６．８、好ましく３．０〜４
．０程度で、十分アルデヒド、アルコール類を除去する
ことができる。Further, the reflux ratio of acetone from the reflux pipe 9 is 1 to 3, preferably 1.5 to 2.5. Further, the reflux ratio of the alkaline aqueous solution from the reflux tube 12 is 0.8 to 6.8, preferably 3.0 to 4.
．． At about 0, aldehydes and alcohols can be sufficiently removed.
本発明によれば、粗アセトンとアルカリ水溶液とをアル
ドール縮合反応の完結後に蒸留塔に供給し、その供給段
より高い位置にさらにアルカリ水溶液を供給して、解縮
合により生成するアルデヒドを除去するようにしたので
、アセトン中のアルデヒド濃度を低くすることができる
。According to the present invention, crude acetone and an aqueous alkali solution are supplied to a distillation column after completion of the aldol condensation reaction, and an aqueous alkali solution is further supplied to a position higher than the supply stage to remove aldehydes produced by decondensation. , the aldehyde concentration in acetone can be lowered.
以下、本発明の実施例について説明する。各例中、％、
ｐｐｍは重量基準である。Examples of the present invention will be described below. In each example, %,
ppm is by weight.
実施例１
第１図に示すように、塔頂に凝縮装置のついた直径４０
ｍ■のガラス製オルダーショウ型５５段の蒸留塔１の第
６段Ｔ６に、サイメンヒドロペルオキシドの酸開裂によ
って生成したアルデヒド類、メタノール類を含有する粗
アセトンと水酸化ナトリウムの１％水溶液を、１１０重
量比０．０９、アルカリ比率０．０９％の割合で混合し
た原料を原料供給管３から２４０＋ｍＱ／Ｈｒで供給し
た。一方、水酸化ナトリウムの０．１％水溶液をアルカ
リ供給管４ｂから前記混合原料の供給段より４段高い第
１Ｏ段Ｔ１゜に６θａｎ／Ｈｒの割合で供給し、還流管
９からの還流比２．５、還流管１２からの還流比２．５
で連続的に２４時間運転した。塔底液は約１５ｍＱ／Ｈ
ｒの割合で抜き出し、塔頂からは２１０ｍＱ／）ｌｒの
割合で精製アセトンを得た。Example 1 As shown in FIG.
A 1% aqueous solution of crude acetone and sodium hydroxide containing aldehydes and methanol produced by acid cleavage of cymen hydroperoxide was added to the sixth stage T6 of a 55-stage Aldershaw-type glass distillation column 1 of 110 m Raw materials mixed at a weight ratio of 0.09 and an alkali ratio of 0.09% were supplied from the raw material supply pipe 3 at a rate of 240+mQ/Hr. On the other hand, a 0.1% aqueous solution of sodium hydroxide is supplied from the alkali supply pipe 4b to the first O stage T1°, which is four stages higher than the supply stage of the mixed raw materials, at a rate of 6θan/Hr, and the reflux ratio from the reflux pipe 9 is 2. .5, reflux ratio from reflux tube 12 2.5
It was operated continuously for 24 hours. The bottom liquid is approximately 15mQ/H
The purified acetone was extracted from the top of the column at a rate of 210 mQ/)lr.
実施例２
実施例１において、供給原料のり１０重量比、アルカリ
比率をそれぞれ０．０５．０．０５％ヤした以外は実施
例１と同様に実施した。Example 2 Example 1 was carried out in the same manner as in Example 1, except that the weight ratio of the feed material paste and the alkali ratio were changed to 0.05% and 0.05%, respectively.
比較例１
実施例１において、水酸化ナトリウム水溶液をすべてア
ルカリ供給管４ｂから供給した以外は実施例１と同様に
実施した。Comparative Example 1 The same procedure as in Example 1 was carried out except that all the sodium hydroxide aqueous solution was supplied from the alkali supply pipe 4b.
以上の結果をまとめて表１に示す。The above results are summarized in Table 1.
第１図は本発明の実施態様を示す系統図、第２図は従来
法の系統図である。
各図中、同一符号は同一または相当部分を示し。
１は蒸留塔、３は原料供給管、４．４ａ、４ｂはアルカ
リ供給管、５は塔頂配管、６は塔底配管、７は凝縮器、
９．１２は還流管、１１は加熱器、Ｔ１・・・は棚段で
ある。
代理人 弁理士 柳 原 成FIG. 1 is a system diagram showing an embodiment of the present invention, and FIG. 2 is a system diagram of a conventional method. In each figure, the same reference numerals indicate the same or corresponding parts. 1 is a distillation column, 3 is a raw material supply pipe, 4.4a, 4b is an alkali supply pipe, 5 is a top pipe, 6 is a bottom pipe, 7 is a condenser,
9.12 is a reflux tube, 11 is a heater, T1... is a tray. Agent Patent Attorney Sei Yanagihara
Claims (3)
セトンとアルカリ水溶液とを混合して、アルドール縮合
反応を完結させた後、蒸留塔へ供給して蒸留し、その供
給段より高い位置にさらにアルカリ水溶液を供給して、
解縮合反応により生成するアルデヒド類およびアルコー
ル類を除去することを特徴とするアセトン精製方法。(1) After mixing crude acetone containing aldehydes and alcohols with an alkaline aqueous solution and completing the aldol condensation reaction, it is supplied to a distillation column for distillation, and an alkali aqueous solution is added at a position higher than the feed stage. by supplying
An acetone purification method characterized by removing aldehydes and alcohols produced by a decondensation reaction.
その一部を蒸留塔へ還流させるようにした請求項（１）
記載の方法。(2) Condensing purified acetone taken out from the distillation column,
Claim (1) wherein a part of it is refluxed to the distillation column.
Method described.
熱して蒸留塔へ還流させるようにした請求項（１）また
は（２）記載の方法。(3) The method according to claim (1) or (2), wherein a part of the alkaline aqueous solution taken out from the distillation column is heated and refluxed to the distillation column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63129128A JP2560784B2 (en) | 1988-05-26 | 1988-05-26 | Acetone purification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63129128A JP2560784B2 (en) | 1988-05-26 | 1988-05-26 | Acetone purification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01299244A true JPH01299244A (en) | 1989-12-04 |
| JP2560784B2 JP2560784B2 (en) | 1996-12-04 |
Family
ID=15001787
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63129128A Expired - Lifetime JP2560784B2 (en) | 1988-05-26 | 1988-05-26 | Acetone purification method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2560784B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009515967A (en) * | 2005-11-14 | 2009-04-16 | スノコ， インコーポレイテッド（アール アンド エム） | Recovery of cumene hydroperoxide decomposition products by distillation |
| CN111995510A (en) * | 2020-09-11 | 2020-11-27 | 吉化集团油脂化工有限公司 | Fine acetone tower treatment method for improving acetone product quality |
-
1988
- 1988-05-26 JP JP63129128A patent/JP2560784B2/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009515967A (en) * | 2005-11-14 | 2009-04-16 | スノコ， インコーポレイテッド（アール アンド エム） | Recovery of cumene hydroperoxide decomposition products by distillation |
| CN111995510A (en) * | 2020-09-11 | 2020-11-27 | 吉化集团油脂化工有限公司 | Fine acetone tower treatment method for improving acetone product quality |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2560784B2 (en) | 1996-12-04 |
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