JPH01226845A - Absorption of methacrolein - Google Patents
Absorption of methacroleinInfo
- Publication number
- JPH01226845A JPH01226845A JP5266488A JP5266488A JPH01226845A JP H01226845 A JPH01226845 A JP H01226845A JP 5266488 A JP5266488 A JP 5266488A JP 5266488 A JP5266488 A JP 5266488A JP H01226845 A JPH01226845 A JP H01226845A
- Authority
- JP
- Japan
- Prior art keywords
- methacrolein
- methacrylic acid
- reaction
- gas
- absorbent
- 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
- STNJBCKSHOAVAJ-UHFFFAOYSA-N Methacrolein Chemical compound CC(=C)C=O STNJBCKSHOAVAJ-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000010521 absorption reaction Methods 0.000 title description 12
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000000034 method Methods 0.000 claims abstract description 18
- 239000007787 solid Substances 0.000 claims abstract description 15
- AMIMRNSIRUDHCM-UHFFFAOYSA-N Isopropylaldehyde Chemical compound CC(C)C=O AMIMRNSIRUDHCM-UHFFFAOYSA-N 0.000 claims abstract description 7
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 5
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000002250 absorbent Substances 0.000 claims abstract description 5
- 230000002745 absorbent Effects 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 25
- 239000007795 chemical reaction product Substances 0.000 claims description 11
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 3
- 229910001882 dioxygen Inorganic materials 0.000 claims description 3
- 238000010574 gas phase reaction Methods 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 239000007864 aqueous solution Substances 0.000 abstract description 13
- 239000000126 substance Substances 0.000 abstract description 9
- 239000002904 solvent Substances 0.000 abstract description 6
- 238000006243 chemical reaction Methods 0.000 abstract description 4
- 230000007774 longterm Effects 0.000 abstract description 2
- 230000001590 oxidative effect Effects 0.000 abstract 2
- 239000000243 solution Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000011084 recovery Methods 0.000 description 7
- 229910001868 water Inorganic materials 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 4
- 230000008025 crystallization Effects 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- -1 17.72 mol% steam Chemical compound 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005580 one pot reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000007039 two-step reaction Methods 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、メタクロレインの吸収方法に関し、詳しくは
、反応生成ガスを凝縮し更に冷却することにより晶析す
るテレフタル酸等の高沸点物質を除去し、かくして得ら
れるメタクロレインを殆ど含まないメタクリル酸水溶液
をメタクロレインの吸収剤として用いる方法に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a method for absorbing methacrolein, and more specifically, the present invention relates to a method for absorbing methacrolein, and more specifically, a method for absorbing a high boiling point substance such as terephthalic acid, which is crystallized by condensing a reaction product gas and further cooling it. The present invention relates to a method of removing methacrylic acid and using the thus obtained aqueous methacrylic acid solution containing almost no methacrolein as an absorbent for methacrolein.
（従来の技術）
イソブチレン、第３級ブタノール、イソブチルアルデヒ
ドまたはメタクロレインを水蒸気の存在下に分子状酸素
で一段または二段の反応により接触酸化して、目的物で
あるメタクリル酸を得ると共に、メタクロレイン、酢酸
、−酸化炭素、二酸化炭素、水、酸素、窒素等を含有す
る反応生成ガスが得られる。反応生成ガスは、通常急冷
されてメタクリル酸、水等が凝縮し、大部分のメタクロ
レインと窒素、酸素等の非凝縮性ガスが塔頂より分離さ
れる。窒素、酸素等の非凝縮性ガスとメタクリル酸製造
の原料としても用いられるメタクロレインとを効率良く
分離回収する方法としては、溶剤を用いてメタクロレイ
ンを吸収し、吸収液を蒸留分離してメタクロレインを回
収する方法がある。このような吸収溶剤として、水（特
開昭５３−１４４５１５） 、酢酸（特開昭５４−４８
７０６） 、メタクロレインの除去されたメタクリル酸
水溶液（特開昭５４−５２０２７）などを用いる方法が
知られている。(Prior art) Isobutylene, tertiary butanol, isobutyraldehyde, or methacrolein is catalytically oxidized with molecular oxygen in the presence of water vapor in a one- or two-step reaction to obtain the target product, methacrylic acid. A reaction product gas containing rhein, acetic acid, carbon oxide, carbon dioxide, water, oxygen, nitrogen, etc. is obtained. The reaction product gas is usually rapidly cooled to condense methacrylic acid, water, etc., and most methacrolein and non-condensable gases such as nitrogen and oxygen are separated from the top of the column. A method for efficiently separating and recovering methacrolein, which is also used as a raw material for the production of methacrylic acid, from non-condensable gases such as nitrogen and oxygen is to absorb methacrolein using a solvent, and separate the absorbed liquid by distillation. There is a way to collect rain. As such absorption solvents, water (JP-A-53-144515), acetic acid (JP-A-54-48) are used.
706), a method using an aqueous methacrylic acid solution from which methacrolein has been removed (Japanese Patent Application Laid-Open No. 54-52027) is known.
〔発明が解決しようとするＸ！ｆｆ１）反応生成ガスの
急冷工程で凝縮しないメタクロレインを吸収する溶剤と
してメタクロレインの除去されたメタクリル酸水溶液を
用いる方法は、あらたに系外から吸収溶剤を導入するこ
となく、且つ吸収液からのメタクロレインの回収と急冷
工程で凝縮したメタクロレインを回収するような二系統
のメタクロレインの回収系を必要とせず、一つの蒸留塔
で行なえることから有利な方法と言える。しかしながら
、メタクロレインの吸収は、−般に低温はど効率が良い
ため、通常は低温で運転される。したがって副生じたテ
レフタル酸等の高沸点物質がメタクリル酸水溶液を冷却
することにより析出し、更には、これら析出物の堆積に
より県内を閉塞する等の重大な問題があった。[X that the invention attempts to solve! ff1) A method of using an aqueous methacrylic acid solution from which methacrolein has been removed as a solvent for absorbing methacrolein that does not condense in the step of rapidly cooling the reaction product gas is possible without introducing an additional absorbing solvent from outside the system and by absorbing the methacrolein from the absorption liquid. This method is advantageous because it can be carried out in one distillation column without requiring two methacrolein recovery systems, one for recovering methacrolein and the other for recovering methacrolein condensed in the quenching step. However, absorption of methacrolein is generally more efficient at lower temperatures, so it is usually operated at lower temperatures. Therefore, by-product high-boiling substances such as terephthalic acid were precipitated by cooling the methacrylic acid aqueous solution, and furthermore, there were serious problems such as the accumulation of these precipitates clogging the prefecture.
（課題を解決するための手段）
本発明者らは、上記の課題を解決するため鋭意検討した
結果、本発明を完成するに至ったものである。すなわち
、本発明のメタクロレインの吸収方法は、イソブチレン
、第３級ブタノール、イソブチルアルデヒドまたはメタ
クロレインを酸化触媒の存在下に分子状酸素を含有する
ガスと気相反応させて得られる反応生成ガスからメタク
ロレインを回収する方法において、該反応生成ガスを凝
縮して得られるメタクリル酸水溶液を３０℃以下に冷却
し、晶析する固形物を分離した後、メタクロレインの吸
収剤として用いることを特徴とするものである。(Means for Solving the Problems) The present inventors have completed the present invention as a result of intensive studies to solve the above problems. That is, the method for absorbing methacrolein of the present invention uses a reaction product gas obtained by subjecting isobutylene, tertiary butanol, isobutyraldehyde, or methacrolein to a gas phase reaction with a gas containing molecular oxygen in the presence of an oxidation catalyst. The method for recovering methacrolein is characterized in that the aqueous methacrylic acid solution obtained by condensing the reaction product gas is cooled to 30°C or less, and after separating solid matter to crystallize, it is used as an absorbent for methacrolein. It is something to do.
本発明のメタクリル酸水溶液とは、反応生成ガスをｐめ
凝縮したメタクリル酸水溶液の一部と向流接触させ、大
部分のメタクロレインを含む非凝縮性ガスを分離し、小
量のメタクロレイン、メタクリル酸および高沸点物質を
含む水溶液から、３０℃以下の温度で晶析する固形物質
を除去したメタクリル酸水溶液を言う。The methacrylic acid aqueous solution of the present invention is produced by bringing the reaction product gas into countercurrent contact with a part of the condensed methacrylic acid aqueous solution, separating the non-condensable gas containing most of the methacrolein, and separating a small amount of methacrolein, An aqueous methacrylic acid solution obtained by removing solid substances that crystallize at temperatures below 30°C from an aqueous solution containing methacrylic acid and high-boiling substances.
晶析温度は、プロセス内のどの工程で晶析するかによっ
ても変るが、効率的かつ経済的に析出する好ましい温度
に設定すればよい。しかしながら、後述するメタクロレ
インを吸収する際の温度以下、すなわち、３０℃以下で
あることが必要であり、好ましくは１０℃以下で、更に
好ましくは５℃以下である。３０℃を越えるとメタクロ
レインのメタクリル酸水溶液による吸収効率が低下し採
用できない。Although the crystallization temperature varies depending on which step in the process the crystallization is performed, it may be set at a preferable temperature that allows the crystallization to occur efficiently and economically. However, the temperature needs to be below the temperature at which methacrolein is absorbed, which will be described later, that is, below 30°C, preferably below 10°C, and more preferably below 5°C. If the temperature exceeds 30°C, the efficiency of absorption of methacrolein by the methacrylic acid aqueous solution decreases, and it cannot be used.
本発明において反応生成ガスからメタクロレインを回収
する際のメタクロレイン含有ガスは、反応生成ガスが急
冷されてメタクリル酸、水等を凝縮させた際、急冷浴塔
頂より分離される大部分のメタクロレインと窒素、酸素
等の非凝縮性ガスよりなるものである。In the present invention, when methacrolein is recovered from the reaction product gas, most of the methacrolein-containing gas is separated from the top of the quenching bath when the reaction product gas is rapidly cooled to condense methacrylic acid, water, etc. It consists of rain and non-condensable gases such as nitrogen and oxygen.
メタクロレイン吸収に際し、供給するメタクリル酸水溶
液のメタクリル酸濃度は、酸化反応における反応条件に
より異なるが、好ましくは５重量％以上、更に好ましく
は１０重量％以上である。Upon methacrolein absorption, the methacrylic acid concentration of the methacrylic acid aqueous solution supplied varies depending on the reaction conditions in the oxidation reaction, but is preferably 5% by weight or more, more preferably 10% by weight or more.
また、供給するメタクリル酸水溶液量は、メタクロレイ
ンを含む非凝縮性ガス全そル量に対して、メタクリル酸
水溶液モル量としてモル比でＯＪ〜ＩＯ１好ましくは１
〜５の範囲である。In addition, the amount of methacrylic acid aqueous solution to be supplied is OJ to IO1, preferably 1 in molar ratio as the molar amount of methacrylic acid aqueous solution to the total amount of non-condensable gas containing methacrolein.
It is in the range of ~5.
メタクロレインを吸収する際の温度は、前述したように
３０℃以下、好ましくは１０℃以下、更に好ましくは５
℃以下である。As mentioned above, the temperature when absorbing methacrolein is 30°C or lower, preferably 10°C or lower, and more preferably 5°C or lower.
below ℃.
この様にしてメタクロレインを吸収したメタクリル酸水
溶液は、通常採用される蒸留等の手段によりメタクロレ
インとメタクリル酸水溶液とに分離して、メタクロレイ
ンを回収するかまたはメタクリル酸製造用原料として反
応器へ循還され、メタクリル酸水溶液は次のメタクリル
酸！１ｆＭ工程へ送られる。The aqueous methacrylic acid solution that has absorbed methacrolein in this way is separated into methacrolein and the aqueous methacrylic acid solution by commonly employed means such as distillation, and the methacrolein is recovered or used in a reactor as a raw material for producing methacrylic acid. The methacrylic acid aqueous solution is recycled to the next methacrylic acid! Sent to 1fM process.
本発明でメタクリル酸水溶液から固形物を分離する方法
としては、熱交換器で温度を設定した後、例えば、充填
式フィルター、沈降槽なと効率的に固形物が除去できる
方法であれば特に制限なく採用される。また、晶析温度
を変えて二段階或は三段階以上に、またプロセスの要所
、例えばメタクロレイン回収塔缶出ラインなどにも設置
することも出来る。In the present invention, the method for separating solids from an aqueous methacrylic acid solution is particularly limited as long as it is a method that can efficiently remove solids after setting the temperature with a heat exchanger, such as a packed filter or a sedimentation tank. It is adopted without any problem. Furthermore, it can be installed in two or more stages by changing the crystallization temperature, or at important points in the process, such as the methacrolein recovery tower bottom line.
以下、実施例により本発明を更に詳細に説明する。 Hereinafter, the present invention will be explained in more detail with reference to Examples.
実施例１
第３級ブタノールを原料として、水蒸気、酸素、窒素と
気相接触酸化反応を行い、得られた組成がメタクロレイ
ン０．７２モル％、スチーム １７．７２モル％、窒素
、酸素等の非凝縮性ガス７８．７２モル％、メタクリル
酸１．９２モル％の２６０℃反応主反応スを、ｌ：１５
ｈ３７Ｈの割合で熱交換器で２０℃に制御されている予
め凝縮された凝縮液の一部と向流接触した。塔頂より、
メタクリル酸０．０５モル％を含むメタクロレイン１．
０１モル％、スチーム１．２５モル％の非凝縮性ガスを
１２４８ｍ３／Ｈの割合でメタクロレイン吸収塔へ供給
した。一方、凝縮したメタクロレイン０．３２冑し％を
含むメタクリル酸２５．６６ｗｔ％、水６４．５７ｗｔ
％、高沸点物質等９．５１ｗｔ％の組成を有するメタク
リル酸水溶液は、３４．ｚ９ｋｇ／Ｈの割合で５℃で操
作される熱交換器を介して冷却し、充填式フィルターを
用いた固形物分離器により晶析したメタクリル酸水溶液
中の高沸点物質等を濾別した。このメタクリル酸水溶液
はメタクロレイン吸収塔缶出液と合流して次のメタクロ
レイン回収塔に送った。この時、充填式フィルターで除
去された固形物量は１２ｇ／１１であった。Example 1 Using tertiary butanol as a raw material, a gas phase catalytic oxidation reaction was performed with water vapor, oxygen, and nitrogen, and the resulting composition was 0.72 mol% methacrolein, 17.72 mol% steam, nitrogen, oxygen, etc. The main reaction mixture of 78.72 mol% of non-condensable gas and 1.92 mol% of methacrylic acid at 260°C was heated to l:15
h37H was brought into countercurrent contact with a portion of the pre-condensed condensate, which was controlled at 20° C. in a heat exchanger. From the top of the tower,
Methacrolein containing 0.05 mol% methacrylic acid 1.
A non-condensable gas containing 1.25 mol% of steam and 1.25 mol% of steam was supplied to the methacrolein absorption tower at a rate of 1248 m3/H. On the other hand, 25.66 wt% of methacrylic acid containing 0.32% of condensed methacrolein, 64.57 wt% of water
%, and a methacrylic acid aqueous solution having a composition of 9.51 wt % such as high boiling point substances, 34. The mixture was cooled through a heat exchanger operated at 5° C. at a rate of 9 kg/H, and high-boiling substances and the like in the crystallized aqueous methacrylic acid solution were filtered out using a solid separator using a packed filter. This aqueous methacrylic acid solution was combined with the bottoms of the methacrolein absorption tower and sent to the next methacrolein recovery tower. At this time, the amount of solid matter removed by the packed filter was 12 g/11.
１０℃で操作されるメタクロレイン吸収塔において、供
給した非凝縮性ガスは、メタクロレイン回収塔でメタク
ロレインの除去されたメタクリル酸水溶液の一部と向流
接触せしめてメタクロレインを吸収した。該塔頂よりメ
タクロレインの除去された非凝縮性ガスを放出し、該塔
底部よりメタクロレイン１．６６ｗｔ％を含むメタクリ
ル酸２４．１２ｗｔ％、水６５．９０ｗｔ％、その他８
．３４ｗｔ％の組成を有するメタクリル酸水溶液１７８
．３ｋｇ／１１を缶出し、前述の凝縮せしめたメタクリ
ル酸水溶液と合流し、この２１２．６ｋｇ／Ｈをメタク
ロレイン回収塔中段に供給した。In the methacrolein absorption tower operated at 10° C., the supplied non-condensable gas was brought into countercurrent contact with a portion of the aqueous methacrylic acid solution from which methacrolein had been removed in the methacrolein recovery tower to absorb methacrolein. Non-condensable gas from which methacrolein has been removed is discharged from the top of the column, and from the bottom of the column 24.12 wt% of methacrylic acid containing 1.66 wt% of methacrolein, 65.90 wt% of water, and 8 others.
．． Methacrylic acid aqueous solution 178 having a composition of 34 wt%
．． 3 kg/11 was taken out from the can, combined with the aforementioned condensed aqueous methacrylic acid solution, and 212.6 kg/H of this was fed to the middle stage of the methacrolein recovery column.
メタクロレイン回収塔において、塔底温度８８℃、圧力
５００ｍｍ１１ｇで蒸留して、該塔頂よりメタクロレイ
ンを回収した。該塔底よりは、メタクロレインを含まな
いメタクリル酸２４．８８ｗｔ％、水６６．６８ｗｔ％
、その他８．４４ｗｔ％の組成を有するメタクリル酸水
溶液を得た。そのうちの１６８．０９ｋｇ／Ｈをメタク
ロレインの吸収溶剤としてメタクロレイン吸収塔に循環
し、残り ４０．１２ｋｇ／Ｈは、次工程のメタクリル
酸蹟製工稈へ送った。In the methacrolein recovery column, distillation was carried out at a bottom temperature of 88° C. and a pressure of 500 mm and 11 g, and methacrolein was recovered from the top of the column. From the bottom of the column, 24.88 wt% of methacrylic acid and 66.68 wt% of water, which do not contain methacrolein.
An aqueous methacrylic acid solution having a composition of 8.44 wt% was obtained. Of this amount, 168.09 kg/H was recycled to the methacrolein absorption tower as an absorption solvent for methacrolein, and the remaining 40.12 kg/H was sent to the methacrylic acid culm in the next step.
このようにして９０日間連続運転したが、各項および全
ライン共に圧力の変化は見られず、安定運転が可能とな
り、塔を解体し充填物および内壁への固形物の付着を調
べたが、殆ど付着は見られず、更なる連続運転が可能で
あることを認めた。After continuous operation for 90 days in this manner, no pressure changes were observed in any section or all lines, and stable operation was possible.The tower was dismantled and the adhesion of solids to the packing and inner walls was investigated. Almost no adhesion was observed, and it was confirmed that further continuous operation was possible.
比較例１
凝縮せしめたメタクリル酸水溶液の冷却および固形物分
離を行わない以外は実施例１と同様に運転したところ、
５日目位からメタクロレイン吸収塔の圧力に変動が生じ
始め、１０日目でフラッディングしたため運転を中止し
、該塔を解体点検したところ充填物にかなりの固形物が
付着しており塔内が閉塞気味であった。Comparative Example 1 The operation was carried out in the same manner as in Example 1 except that the condensed methacrylic acid aqueous solution was not cooled and the solid matter was not separated.
The pressure of the methacrolein absorption tower started to fluctuate from around the 5th day, and on the 10th day, due to flooding, the operation was stopped and when the tower was dismantled and inspected, a considerable amount of solid matter was attached to the packing material, and the inside of the tower was It felt like a blockage.
実施例２
熱交換器および固形物分離器の設置場所を、メタクロレ
イン回収塔缶出ラインに変更した以外は、実施例１と同
様に運転したところ、充填式フィルターには３０ｇ／１
１の固形物が得られ、９０日間の連続運転においても、
各項および全ライン共に圧力の変化は見られず、安定に
運転が行えた。また、塔を解体し充填物および内壁への
固形物の付着を調べたが、殆ど付着は見られず、更なる
連続運転が可能であることを認めた。Example 2 The operation was carried out in the same manner as in Example 1, except that the installation location of the heat exchanger and solids separator was changed to the bottom line of the methacrolein recovery column.
1 solid was obtained, and even in continuous operation for 90 days,
No change in pressure was observed in each section or in all lines, and stable operation was possible. In addition, the tower was dismantled and the adhesion of solid matter to the packing material and inner walls was examined, but almost no adhesion was observed, confirming that further continuous operation is possible.
（発明の効果〕
本発明により極めて効率良くメタクロレインの回収がで
き、長期の運転を可能にすることができ産業上利用価値
が高い。(Effects of the Invention) According to the present invention, methacrolein can be recovered extremely efficiently, long-term operation is possible, and the present invention has high industrial utility value.
特許出願人 三井東圧化学株式会社 協和ガス化学工業株式会社Patent applicant: Mitsui Toatsu Chemical Co., Ltd. Kyowa Gas Chemical Industry Co., Ltd.
Claims (1)
ルデヒドまたはメタクロレインを酸化触媒の存在下に分
子状酸素を含有するガスと気相反応させて得られる反応
生成ガスからメタクロレインを回収する方法において、
該反応生成ガスを凝縮して得られるメタクリル酸水溶液
を３０℃以下に冷却し、晶析する固形物を分離した後、
メタクロレインの吸収剤として用いることを特徴とする
メタクロレインの吸収方法。(1) In a method for recovering methacrolein from a reaction product gas obtained by subjecting isobutylene, tertiary butanol, isobutyraldehyde or methacrolein to a gas phase reaction with a gas containing molecular oxygen in the presence of an oxidation catalyst,
After cooling the aqueous methacrylic acid solution obtained by condensing the reaction product gas to 30° C. or lower and separating the solid matter to be crystallized,
A method for absorbing methacrolein, characterized by use as an absorbent for methacrolein.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5266488A JPH0764775B2 (en) | 1988-03-08 | 1988-03-08 | How to absorb methacrolein |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5266488A JPH0764775B2 (en) | 1988-03-08 | 1988-03-08 | How to absorb methacrolein |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01226845A true JPH01226845A (en) | 1989-09-11 |
| JPH0764775B2 JPH0764775B2 (en) | 1995-07-12 |
Family
ID=12921136
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5266488A Expired - Lifetime JPH0764775B2 (en) | 1988-03-08 | 1988-03-08 | How to absorb methacrolein |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0764775B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0847978A1 (en) * | 1996-12-16 | 1998-06-17 | Nippon Shokubai Co., Ltd. | Process for producing (meth)acrylic acid |
| WO1999006348A1 (en) * | 1997-07-30 | 1999-02-11 | Mitsubishi Rayon Co., Ltd. | Process for the purification of (meth)acrylic acid |
| JP2014532039A (en) * | 2011-09-16 | 2014-12-04 | エボニック レーム ゲゼルシャフト ミット ベシュレンクテル ハフツングＥｖｏｎｉｋ Ｒｏｅｈｍ ＧｍｂＨ | Production of methacrylic acid |
-
1988
- 1988-03-08 JP JP5266488A patent/JPH0764775B2/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0847978A1 (en) * | 1996-12-16 | 1998-06-17 | Nippon Shokubai Co., Ltd. | Process for producing (meth)acrylic acid |
| KR100371759B1 (en) * | 1996-12-16 | 2003-05-22 | 니폰 쇼쿠바이 컴파니 리미티드 | Process for producing (meth)acrylic acid |
| WO1999006348A1 (en) * | 1997-07-30 | 1999-02-11 | Mitsubishi Rayon Co., Ltd. | Process for the purification of (meth)acrylic acid |
| US6380427B1 (en) | 1997-07-30 | 2002-04-30 | Mitsubishi Rayon Co., Ltd. | Process for purification of (meth)acrylic acid |
| JP2014532039A (en) * | 2011-09-16 | 2014-12-04 | エボニック レーム ゲゼルシャフト ミット ベシュレンクテル ハフツングＥｖｏｎｉｋ Ｒｏｅｈｍ ＧｍｂＨ | Production of methacrylic acid |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0764775B2 (en) | 1995-07-12 |
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