JPS6038341A - Purification of acrylic acid - Google Patents
Purification of acrylic acidInfo
- Publication number
- JPS6038341A JPS6038341A JP14564583A JP14564583A JPS6038341A JP S6038341 A JPS6038341 A JP S6038341A JP 14564583 A JP14564583 A JP 14564583A JP 14564583 A JP14564583 A JP 14564583A JP S6038341 A JPS6038341 A JP S6038341A
- Authority
- JP
- Japan
- Prior art keywords
- acrylic acid
- acetic acid
- column
- azeotropic
- water
- 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.)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【発明の詳細な説明】 本発明はアクリル酸の精製方法に関する。[Detailed description of the invention] The present invention relates to a method for purifying acrylic acid.
詳しく述べると本発明はプロピレンおよび/またはアク
[]レインを接触気相酸化してアクリル酸を含有する反
応ガスをえ、これを急冷し凝縮捕集しさらに冷却水によ
り吸収捕集し、えられる主としてアクリル酸、酢酸およ
び水を含有するアクリル酸水溶液を共沸剤により蒸留し
てアクリル酸および酢酸を含まず実質的に水と共沸剤ど
J:りなる共沸物を留去し、塔底缶液どして主としてア
クリル酸および酢酸とJ:りなる混合物をえ、この缶液
からアクリル酸を分離し、精製することを特徴とするア
クリル酸の精製法に関する。Specifically, the present invention involves catalytic gas phase oxidation of propylene and/or acrine to obtain a reaction gas containing acrylic acid, which is rapidly cooled, condensed and collected, and further absorbed and collected by cooling water. An aqueous acrylic acid solution containing mainly acrylic acid, acetic acid, and water is distilled using an azeotrope to remove acrylic acid and acetic acid and substantially water and the azeotrope. This invention relates to a method for purifying acrylic acid, characterized in that a mixture of acrylic acid and acetic acid is mainly obtained from the bottom liquid, and acrylic acid is separated and purified from the bottom liquid.
従来、アクリル酸の製造方法はプロピレンおよび/また
はアクロレインを接触気相酸化してえられるアクリル酸
水溶液を有機溶剤に−2−
より抽出処理しアクリル酸を抽出し精製する工程よりな
る。すなわち、水溶液から水を分離する工程として抽出
操作を1にとが一般的である(たとえば、特公昭46−
30493号公報明細書参照。)。Conventionally, methods for producing acrylic acid include the steps of extracting and purifying acrylic acid by extracting an aqueous acrylic acid solution obtained by catalytic gas phase oxidation of propylene and/or acrolein with an organic solvent. In other words, it is common to use an extraction operation as a step for separating water from an aqueous solution (for example,
See specification of Publication No. 30493. ).
しかしながら、この抽出T稈で排出される水は未回収の
アクリル酸や副生成物である有機酸、たとえばm酸、プ
ロピオン酸、マレイン酸やアルデヒド類、たとえば、ア
クロレイン、アセトアルデヒド、またこれら化合物の重
合物や縮合物さらにはアクリル酸2@体など高沸点物質
やタール状物質などを含み、廃水は、破棄するにしても
活性汚泥法や濃縮燃焼法などによる無害化処理を必要と
し、そのための設備やユーティリティーなどは、きわめ
てコストを要するものとならざるをえない。一方、その
ままアクリル酸捕集用の吸収水としてプロセスに使用す
るとしても該廃水中の酸分に帰因するプロセス内の酸分
の増加によりアクリル酸捕集装置でのアクリル酸の捕集
効率の低下をきたすことになり、かりにこの装置からの
排出ガスを原料ガスの不活性ガス源として再使用する場
合には、−3−
原料ガス中の酸分の増加をきたし、酸化反応にお(Jる
触媒活v1の劣化を早める原因ともなる。However, the water discharged from this extraction T culm contains unrecovered acrylic acid, by-product organic acids such as m-acid, propionic acid, maleic acid, aldehydes such as acrolein and acetaldehyde, and polymerization of these compounds. The wastewater contains high boiling point substances and tar-like substances such as 2@acrylic acid, condensates, etc., and even if it is to be disposed of, it must be detoxified by an activated sludge method or a concentrated combustion method, and equipment for this purpose is required. and utilities, etc., must be extremely costly. On the other hand, even if it is used as absorbed water for acrylic acid collection in the process, the acrylic acid collection efficiency of the acrylic acid collection device will decrease due to the increase in acid content in the process due to the acid content in the wastewater. However, if the exhaust gas from this equipment is reused as an inert gas source for the raw material gas, the acid content in the raw material gas will increase and the oxidation reaction (J It also causes accelerated deterioration of the catalyst activity v1.
また、近時1配酸化反応および捕集技術の向上により、
えられるアクリル酸水溶液の濃度もアクリル酸が50〜
80重量%にまで高められるJ:うになってきている。In addition, with recent improvements in coordination oxidation reactions and collection technology,
The concentration of the acrylic acid aqueous solution obtained is 50~
J: The sea urchin is becoming more and more 80% by weight.
従って、本発明はこのJ:つな高11度のアクリル酸水
溶液を使用して、従来のように抽出操作を施すことくT
く、直接、脱水操作としての共沸蒸留法を採用し、さら
にアクリル酸と酢酸の塔頂への留出を痕跡程度に抑える
方法を検討し完成に至ったものである。Therefore, the present invention uses this aqueous acrylic acid solution with a J: height of 11 degrees, and without performing an extraction operation as in the past.
This method was completed by adopting an azeotropic distillation method as a direct dehydration operation, and further investigating a method to suppress the distillation of acrylic acid and acetic acid to the top of the column to only a trace.
すなわち、本発明は以下の如く特定される。That is, the present invention is specified as follows.
〔1] プロピレンおJ:び/またはアクロレインを接
触気相酸化し【アクリル酸を製造するに際し、当該反応
ガスからえられる酢酸を含有するアクリル酸水溶液を、
その回収部の理論段数が少なくとも10である蒸留塔に
供給し、共沸剤の共存下に蒸留1ノ、jハ頂よりアクリ
ル酸および酢酸を含まない実質的に共沸剤と水とよりな
る共沸−4−
組成物を留出させ塔底にり水および共沸剤を含まない主
としてアクリル酸と酢酸との混合物をえることを特徴と
するアクリル酸の精製方法。[1] When producing acrylic acid by catalytic gas phase oxidation of propylene and/or acrolein, an aqueous acrylic acid solution containing acetic acid obtained from the reaction gas is
The recovery section is supplied to a distillation column with a theoretical plate number of at least 10, and is distilled from the top in the presence of an entrainer. Azeotrope-4- A method for purifying acrylic acid, characterized in that a composition is distilled out and a mixture of mainly acrylic acid and acetic acid, which is free of water and an azeotropic agent, is obtained at the bottom of the column.
〔2) 使用される共沸剤が、常圧で110〜130℃
の範囲の沸点を有するものであることを特徴とする上記
〔1)記載の方法。[2) The temperature of the azeotropic agent used is 110 to 130°C at normal pressure.
The method described in [1] above, wherein the boiling point is in the range of .
0) 蒸留塔に供給されるアクリル酸水溶液が、アクリ
ル酸を50〜80重量%の範囲、酢酸を2〜8重量%の
範囲含有することを特徴とする上記〔1)または(2)
記載の方法。0) The above [1) or (2), wherein the acrylic acid aqueous solution supplied to the distillation column contains acrylic acid in a range of 50 to 80% by weight and acetic acid in a range of 2 to 8% by weight.
Method described.
以下、本発明をさらに具体的に説明するが、それにより
本発明の目的もより明らかにされるであろう。The present invention will be explained in more detail below, and the purpose of the present invention will become clearer thereby.
プロピレンおよび/またはアクロレインをモリブデンベ
ースの多元系触媒を用いて接触気相酸化してアクリル酸
を製造す、ることは現在工業的に行なわれている。また
最、近になって酸化反応およびアクリル酸捕集技術が長
足の進歩を示しえられる− 5 −
アクリル酸水溶液濃度が50〜80重量%と高濃度化す
ることが可能となついる。これは、従来法であるアクリ
ル酸水溶液の抽出処理によるアクリル酸および酢酸を水
と分離する操作とくらべこの水溶液から蒸留により直接
水を分離することを好都合ならしめることを意味する。Catalytic gas phase oxidation of propylene and/or acrolein using molybdenum-based multi-component catalysts to produce acrylic acid is currently practiced industrially. Recently, oxidation reaction and acrylic acid collection technology have shown great progress.-5-It has become possible to increase the concentration of acrylic acid aqueous solution to 50 to 80% by weight. This means that it is convenient to directly separate water from this aqueous solution by distillation, compared to the conventional method of separating acrylic acid and acetic acid from water by extraction of an aqueous acrylic acid solution.
しかも、アクリル酸水溶液から水のみを効率よく分離し
、実質的にアクリル酸と酢酸とが混合物として取得でき
れば、従来プロセスへの適用にも好都合である。本発明
はかかる目的に適合すべく開発されたものである。Moreover, if only water can be efficiently separated from an aqueous acrylic acid solution and essentially acrylic acid and acetic acid can be obtained as a mixture, it is convenient for application to conventional processes. The present invention was developed to meet this objective.
本発明で使用される共沸剤としては、水の搬出能の大き
い化合物、すなわち共沸組成において水の割合が大きく
なるような化合物であり、しかも沸点が高く、常圧下1
10〜130℃の範囲のものが好ましい。具体的には、
酢酸n−ブチル、酢酸イソブチル、酢酸5ea−ブチル
、メチルイソブチルケトンなどが挙げられる。The azeotropic agent used in the present invention is a compound that has a high water transport ability, that is, a compound that increases the proportion of water in the azeotropic composition, has a high boiling point, and has a high boiling point under normal pressure.
A temperature range of 10 to 130°C is preferred. in particular,
Examples include n-butyl acetate, isobutyl acetate, 5ea-butyl acetate, methyl isobutyl ketone, and the like.
もちろん、これらの共沸剤は酢酸と沸点が近接しており
、単に蒸留に供しただけでは、留出時酢−6−
酸をも水どともに留出せしめてしまうことにもなる(た
とえば、特公昭46−18967号公報明細由参照。Of course, these entrainers have boiling points close to that of acetic acid, and if they were simply subjected to distillation, acetic acid-6-acid would also be distilled out along with water (for example, See the specification of Japanese Patent Publication No. 18967/1983.
)。1−なわち、留出液組成が共沸剤−ホー酢酸という
組成となり再度類Hな分離操作を必要とする結果をもた
らしてしまう。). 1- That is, the composition of the distillate becomes an azeotropic agent-foracetic acid composition, which results in the need for a similar separation operation again.
ところが、本発明者らは、蒸留塔の塔頂蒸気を操作圧に
おける共沸組成となるように還流量を決めることにより
アクリル酸の留出が抑えられること、それだ1ノでなく
さらに蒸留塔の回収部の理論段数を少なくとも10に設
定すると留出側の酢酸が痕跡程度どなしうろことを知見
し、かく1ノで、共沸剤および水を含まない主として酢
酸およびアクリル酸とよりなる塔底液を取り出しうるこ
とを見出したのである。However, the present inventors have discovered that the distillation of acrylic acid can be suppressed by determining the reflux amount so that the vapor at the top of the distillation column has an azeotropic composition at the operating pressure. It was discovered that if the number of theoretical plates in the recovery section was set to at least 10, there would be traces of acetic acid on the distillate side. They discovered that it was possible to extract the bottom liquid.
」−記蒸留操作において、本発明者らは、酢酸の濃度ピ
ーク段ど水の濃度ピークρとが分離して存在することを
見出している。これは酢酸の留出を抑えるのに有効とな
っていると考えられる。また供給液中の酢酸量が増加す
ると醋酸の濃縮される段が広がり水の濃縮される段と接
近して重なり合一 7 −
ってさ、酢酸の留出が若干生じてくる。したがって、酢
酸濃度が上をしてくるに応じて回収部の理論段数も10
を越え15一段くらいにまで高める必要が生ずる。アク
リル酸水溶液中の酢酸Ii1度は2〜8重量%と疫化づ
るからである。In the distillation operation, the present inventors have discovered that the concentration peak of acetic acid and the concentration peak ρ of water exist separately. This is considered to be effective in suppressing the distillation of acetic acid. Furthermore, when the amount of acetic acid in the feed liquid increases, the stage where acetic acid is concentrated spreads out, approaches and overlaps the stage where water is concentrated, and some of the acetic acid is distilled out. Therefore, as the acetic acid concentration increases, the number of theoretical plates in the recovery section also increases to 10.
It will be necessary to exceed this level and raise it to about 15 steps. This is because 1 degree of acetic acid II in an acrylic acid aqueous solution is 2 to 8% by weight, which is extremely high.
本発明方法により、水搬出能力の大きい共沸剤を用いつ
つアクリル酸のみならず酢酸も留出させない蒸留方法が
確立され、これまで留出水は共沸剤を分1Il11後廃
水処理とか酢酸の分離回収操作等によって無公害化処理
を必要としていたのに対し、留出液は共沸剤回収後アク
リル酸捕集用の吸収水として再使用することが可能とな
り、無公害のりI]−ズドシステム化プr+ t?スに
とってきわめて有用どなった。By the method of the present invention, a distillation method that does not distill out not only acrylic acid but also acetic acid while using an entrainer with a large water carrying capacity has been established. Whereas pollution-free treatment was required through separation and recovery operations, the distillate can now be reused as absorption water for collecting acrylic acid after collecting the entrainer, and the Systemization pr + t? It has become extremely useful for
1メ下に実施例お。1.び比較例を示し、本発明をさら
に具体的に31明づる。Example below. 1. The present invention will be explained in more detail by showing comparative examples and comparative examples.
実施例 1
プ1]ピ1ノンをモリブデンベース多元系触媒にJ:す
2段酸化反応に供し、えられたアクリル酸66.8重量
%、耐M2.1重量%、水28.8重量%、−8−
残りアl? +−アルデヒド、アクロレイン、マレイン
酸などにりなるアクリル酸水溶液を、100mmφの無
理多孔板48段(理論段数19)を有する蒸留塔の23
段目に11KLJ/Hrで供給した。共沸剤としてメチ
ルイソブチルケトン(MIBK>を、塔頂操作圧110
n+m1−1<1(絶対圧)かつ温度46℃での塔頂共
沸組成21重量%(残りは主として水)となるように塔
頂に供給した。また、重合禁止剤としてハイドロキノン
を塔頂から供給アクリル酸に対し0.1重量%となるJ
:うに、塔底から空気を10(1/l−1rの割合で供
給した。蒸留がほぼ定常状態になったとき塔内の各成分
の81度分布を測定したところ、表1の如くであった。Example 1 A two-stage oxidation reaction was carried out using a molybdenum-based multi-component catalyst to give 66.8% by weight of acrylic acid, 2.1% by weight of M resistance, and 28.8% by weight of water. , -8- What's left? + - An aqueous solution of acrylic acid consisting of aldehyde, acrolein, maleic acid, etc. was added to a distillation column with 48 forced perforated plates (19 theoretical plates) of 100 mm diameter.
It was supplied to each stage at a rate of 11 KLJ/Hr. Methyl isobutyl ketone (MIBK) was used as an entrainer at an overhead operating pressure of 110
It was supplied to the top of the column so that the azeotropic composition at the top of the column at n+m1-1<1 (absolute pressure) and a temperature of 46° C. was 21% by weight (the remainder was mainly water). In addition, hydroquinone was supplied from the top of the tower as a polymerization inhibitor at a concentration of 0.1% by weight based on acrylic acid.
: Air was supplied from the bottom of the column at a rate of 10 (1/l-1r). When the distillation reached a nearly steady state, the 81 degree distribution of each component in the column was measured, and the results were as shown in Table 1. Ta.
塔底液として7.7に9/Hrをえたが、酢M3.1重
邑%。The bottom liquid was 7.7 to 9/Hr, but the vinegar M was 3.1%.
アクリル酸96.2重量%であり、M I B Kおよ
び水は検出できなかった。なお留出液中には酢酸および
アクリル酸は痕跡程度であった。Acrylic acid was 96.2% by weight, and M I B K and water were not detectable. The distillate contained trace amounts of acetic acid and acrylic acid.
比較例 1
実施例1における操作において、アクリル酸水溶液の供
給を31段目から行ない、あとは同様に= 9 −
したところ、Jハ頂からの留出液中に酢酸が1.9重量
%、アクリル酸は痕跡程度含有されていた。酢酸の留出
率は3210t1%にも達した。また塔底液中にはM
r B K iJ’3よび水は痕跡含まれていた。蒸留
が定常状態になったときの塔内での各成分の濃度分布は
、表1に示寸とおりであった。Comparative Example 1 In the operation in Example 1, the acrylic acid aqueous solution was supplied from the 31st stage, and the rest was carried out in the same manner as = 9 -. Trace amounts of acrylic acid were contained. The distillation rate of acetic acid reached 3210t1%. In addition, there is M in the bottom liquid.
Traces of r B K iJ'3 and water were present. The concentration distribution of each component in the column when the distillation reached a steady state was as shown in Table 1.
表 1
10−
実施例 2
実施例1で用いたと同じ蒸留塔に、実施例1で用いたの
と同じアクリル酸水溶液を21段目に供給し、共沸剤と
して酢酸n−ブチルを操作It 130mlHg(絶対
圧)かつ温度50℃で共沸組成28重量%(残りは水)
となるように塔頂から投入し、あとは実施例1における
と同様に蒸留処理した。Table 1 10- Example 2 The same acrylic acid aqueous solution used in Example 1 was fed to the 21st stage of the same distillation column as used in Example 1, and n-butyl acetate was used as an entrainer.It 130 mlHg (absolute pressure) and temperature 50°C, azeotropic composition 28% by weight (remaining water)
The mixture was charged from the top of the column so that
塔底液として酢酸3.0重量%、アクリル酸96.2重
量%、酢酸n−ブチルおよび水は痕跡Pi!iの組成物
がえられた。また留出液中の酢酸おJ:びアクリル酸は
合計で0.07fi量%含まれていた。The bottom liquid contained 3.0% by weight of acetic acid, 96.2% by weight of acrylic acid, n-butyl acetate and water with traces of Pi! A composition of i was obtained. In addition, acetic acid, J: and acrylic acid in the distillate were contained in a total amount of 0.07% by weight.
実施例 3
実施例1で用いたと同じ蒸留塔に、実施例1で用いたど
同じアクリル酸水溶液を23段目に供給し、共沸剤とし
て酢酸イソブチルを操作圧130+no+Ha (絶対
圧)かつ温度47℃で共沸組成19.2重間%(残り水
)となるように塔頂から投入し、あとは実施例1におけ
ると同様に蒸留処理した。Example 3 To the same distillation column as used in Example 1, the same aqueous acrylic acid solution as used in Example 1 was fed to the 23rd stage, and isobutyl acetate was added as an entrainer at an operating pressure of 130+no+Ha (absolute pressure) and a temperature of 47%. C. and the azeotropic composition was 19.2% by weight (residual water) from the top of the column, and the rest was distilled in the same manner as in Example 1.
塔底液として酢酸31重量%、アクリル酸96.1重量
%、酢酸イソブチルおよび水は痕跡程度の組−11−
成物がえられた。また留出液中の酢酸およびアクリル酸
は痕跡程度含まれていた。As a bottom liquid, 31% by weight of acetic acid, 96.1% by weight of acrylic acid, and only traces of isobutyl acetate and water were obtained. In addition, trace amounts of acetic acid and acrylic acid were contained in the distillate.
比較例 2
実施例3においてアクリル酸水溶液を33段目に供給す
るほかは同様に行ない、塔底液として酢酸2.5重量%
、アクリルI!196.8重量%、11)酸イソブチル
および水は痕跡程度の組成物がえられた。Comparative Example 2 The same procedure as in Example 3 was carried out except that the acrylic acid aqueous solution was supplied to the 33rd stage, and 2.5% by weight of acetic acid was used as the bottom liquid.
, Acrylic I! A composition containing 196.8% by weight, 11) isobutyl acid and trace amounts of water was obtained.
また留出液中の酢酸は1.2重量%、アクリル酸0.2
重量%含まれており、酢酸の留出率は18重石%であっ
た。 、
特許出願人 口本触媒化学工業株式会社−12−
手続補正書(自発)
昭和59年11月2日
特許庁長官 志 賀 学 殿
1、事件の表示
昭和58年特許願第145645号
2、発明の名称
アクリル酸の精製方法
3、補正をする者
特許出願人
大阪府大阪市東区高麗橋5丁目1番地
(462) 日本触媒化学工業株式会社代表取締投石川
三部
置 03−502−1651
5、補正の対象
出願明紳1畳の発明の詳細な説明の項
6、補正の自答
(1)明細書第9頁第4行において
「留塔の23段目に・・・・・・」とあるのを、「留塔
の上から23段目に・・・・・・」と補正する。In addition, acetic acid in the distillate was 1.2% by weight, and acrylic acid was 0.2% by weight.
The distillation rate of acetic acid was 18% by weight. , Patent applicant Kusumoto Shokubai Kagaku Kogyo Co., Ltd. -12- Procedural amendment (voluntary) November 2, 1980 Manabu Shiga, Commissioner of the Patent Office1, Indication of case Patent application No. 145645 of 19812, Invention Name of acrylic acid purification method 3, Person making the amendment Patent applicant: 5-1 Koraibashi, Higashi-ku, Osaka, Osaka Prefecture (462) Nippon Shokubai Chemical Co., Ltd. Representative Director: Mibeki Toshikawa 03-502-1651 5. Amendment Section 6 of the detailed description of the invention of the subject application of Meishin 1 Tatami, self-answer of the amendment (1) In the 4th line of page 9 of the specification, it says "In the 23rd step of the tower..." Correct that to "23rd step from the top of the tower..."
(2)同第9頁第7〜8行において
「・・・・・・塔頂共沸組成21重量qb(残シ紘主と
して水)・・・・・・」とあるのを、[・・・・・・塔
頂共沸組成(水2111L1i1%、MIBK79重量
%)・・・・・・」と補正する。(2) On page 9, lines 7-8 of the same page, the statement ``...Azeotropic composition at the top of the column: 21 qb (residual residue is mainly water)...'' has been replaced with [... ...Top azeotrope composition (2111L1i1% water, 79% by weight MIBK)..." is corrected.
(3)同第9真下から第1行において
「・・・・・・供給を31段目・・・・・・」とあるの
を、「・・・・・・供給を上がら31段目・・・・・・
」と補正する。(3) In the first line from the bottom of No. 9, the phrase "...supply to the 31st stage..." has been changed to "...supply to the 31st stage..."・・・・・・
” he corrected.
(4)同第11頁第5〜6行において
「・・・・・・共沸組成28重量優(残少社水)・・・
・・・」とあるのを
[・・・・・・共沸組成(水28重量係、酢@! n
−ブチル72重−it%)・・・・・・」と補正する。(4) On page 11, lines 5 and 6, “...Azeotropic composition 28% by weight (Zanshoshasui)...”
``...'' means [...Azeotropic composition (Water 28 weight section, Vinegar @! n
-Butyl 72 weight-it%)...'' is corrected.
(5)同第11貞丁から第5〜4行において「・・・・
・・共沸組成19.2重量%(残シ水)・・・・・・」
とあるのを、
「・・・・・・共沸組成(水19.21i量係、酢酸イ
ソブチル80.8重量%)・・・・・・」と補正する。(5) In lines 5 and 4 from the 11th Teicho, “...
...Azeotropic composition 19.2% by weight (residual water)..."
The statement has been corrected to "...Azeotropic composition (19.21i of water, 80.8% by weight of isobutyl acetate)...".
3− 289−3- 289-
Claims (1)
気相酸化してアクリル酸を製造するに際し、当該反応ガ
スからえられる酢酸を含有するアクリル酸水溶液を、そ
の回収部の理論段数が少なくとも10である蒸留塔に供
給し、共沸剤の共存下に蒸留し、塔頂よりアクリル酸お
よび酢酸を含まない実質的に共沸剤と水とよりなる共沸
組成物を留出させ、塔底より水および共沸剤を含まない
主としてアクリル酸と酢酸との混合物をえることを特徴
とするアクリル酸の精製方法。 〔2) 使用される共沸剤が、常圧で110〜130℃
の範囲の沸点を有するものであることを特徴とする特許
請求の範囲(1〕記載の方法。 0〕 蒸留塔に供給されるアクリル酸水溶液が、−1− アクリル酸を50〜80重用%の範囲、醋酸を2〜8重
M%の範囲含有することを特徴とする特γ[請求の範囲
0)または〔2〕記載の方法。[Scope of Claims] [1] When producing acrylic acid by catalytic gas phase oxidation of propylene and/or acrolein, an aqueous acrylic acid solution containing acetic acid obtained from the reaction gas is 10, and distilled in the coexistence of an azeotropic agent, distilling an azeotropic composition substantially consisting of an azeotropic agent and water and not containing acrylic acid and acetic acid from the top of the column; A method for purifying acrylic acid, characterized in that a mixture of mainly acrylic acid and acetic acid is obtained from the bottom of the column without containing water or an entrainer. [2) The temperature of the azeotropic agent used is 110 to 130°C at normal pressure.
The method according to claim (1), characterized in that the aqueous solution of acrylic acid supplied to the distillation column has a boiling point in the range of 50 to 80% by weight of -1- acrylic acid. The method according to claim 0 or [2], characterized in that acetic acid is contained in an amount of 2 to 8% by weight.
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP58145645A JPH0615495B2 (en) | 1983-08-11 | 1983-08-11 | Acrylic acid purification method |
GB08420153A GB2146636B (en) | 1983-08-11 | 1984-08-08 | Process for producing acrylic acid |
DE19843429391 DE3429391A1 (en) | 1983-08-11 | 1984-08-09 | METHOD FOR PRODUCING ACRYLIC ACID |
KR1019840004818A KR900006901B1 (en) | 1983-08-11 | 1984-08-10 | Process for producing acyulic acid |
MX202336A MX161562A (en) | 1983-08-11 | 1984-08-10 | PROCEDURE TO PRODUCE ACRYLIC ACID |
FR8412731A FR2554809B1 (en) | 1983-08-11 | 1984-08-13 | PROCESS FOR THE PREPARATION OF ACRYLIC ACID |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP58145645A JPH0615495B2 (en) | 1983-08-11 | 1983-08-11 | Acrylic acid purification method |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS6038341A true JPS6038341A (en) | 1985-02-27 |
JPH0615495B2 JPH0615495B2 (en) | 1994-03-02 |
Family
ID=15389796
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP58145645A Expired - Lifetime JPH0615495B2 (en) | 1983-08-11 | 1983-08-11 | Acrylic acid purification method |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPH0615495B2 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6038342A (en) * | 1983-08-12 | 1985-02-27 | Nippon Shokubai Kagaku Kogyo Co Ltd | Production of acrylic acid |
JPS61265410A (en) * | 1985-05-20 | 1986-11-25 | Tokyo Gas Co Ltd | Method of controlling combustion device |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5690034A (en) * | 1979-12-25 | 1981-07-21 | Mitsubishi Petrochem Co Ltd | Purification of acrylic acid |
-
1983
- 1983-08-11 JP JP58145645A patent/JPH0615495B2/en not_active Expired - Lifetime
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5690034A (en) * | 1979-12-25 | 1981-07-21 | Mitsubishi Petrochem Co Ltd | Purification of acrylic acid |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6038342A (en) * | 1983-08-12 | 1985-02-27 | Nippon Shokubai Kagaku Kogyo Co Ltd | Production of acrylic acid |
JPS61265410A (en) * | 1985-05-20 | 1986-11-25 | Tokyo Gas Co Ltd | Method of controlling combustion device |
JPH0454133B2 (en) * | 1985-05-20 | 1992-08-28 | Tokyo Gas Co Ltd |
Also Published As
Publication number | Publication date |
---|---|
JPH0615495B2 (en) | 1994-03-02 |
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