JP2966650B2 - Method for producing methacrylic acid and its ester - Google Patents
Method for producing methacrylic acid and its esterInfo
- Publication number
- JP2966650B2 JP2966650B2 JP4157439A JP15743992A JP2966650B2 JP 2966650 B2 JP2966650 B2 JP 2966650B2 JP 4157439 A JP4157439 A JP 4157439A JP 15743992 A JP15743992 A JP 15743992A JP 2966650 B2 JP2966650 B2 JP 2966650B2
- Authority
- JP
- Japan
- Prior art keywords
- methacrylic acid
- formaldehyde
- catalyst
- raw material
- producing methacrylic
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、プロピオン酸をホルム
アルデヒド又はホルムアルデヒド誘導体と触媒の存在
下、気相で接触反応させて炭素数の一つ多いメタクリル
酸及び又はそのエステルを製造する方法に関する。The present invention relates to a presence of propionic acid formaldehyde or formaldehyde derivatives and the catalyst, by catalytic reaction in the gas phase larger one of the number of carbon methacrylic
The present invention relates to a method for producing an acid and / or an ester thereof.
【０００２】[0002]
【従来の技術】プロピオン酸とホルムアルデヒド又はホ
ルムアルデヒド誘導体からメタクリル酸及びそのエステ
ルを製造する反応の触媒に関しては種々提案されてい
る。例えば米国特許第３，２４７，２４８号明細書では
シリカゲルに水酸化カリウムを担持した触媒あるいはカ
ルシウムアルミノシリケートを触媒としてプロピオン酸
とホルムアルデヒドを反応させている。また特開昭５７
−１２３１３８号公報ではＳｉＯ2 −Ａｌ2 Ｏ3 にＫ、
Ｖ、Ｓｂを担持した触媒、特開昭６１−２２９８４０号
公報ではＺｒＯ2 −Ａｌ2 Ｏ3 にＶ、Ｐを担持した触
媒、特開昭６２−３６３４０号公報では活性Ａｌ2 Ｏ3
にアルカリ金属を担持した触媒が開示されている。2. Description of the Related Art Various catalysts for producing methacrylic acid and its esters from propionic acid and formaldehyde or formaldehyde derivatives have been proposed. For example, in U.S. Pat. No. 3,247,248, propionic acid and formaldehyde are reacted using potassium hydroxide supported on silica gel or calcium aluminosilicate as a catalyst. Also, Japanese Patent Laid-Open No. 57
K on SiO 2 -Al 2 O 3 is at -123138, JP-
V, catalyst supporting Sb, active Al 2 O 3 in ZrO 2 -Al 2 O 3 in JP-A-61-229840 V, catalyst carrying P, in JP-A-62-36340
Discloses an alkali metal-supported catalyst.
【０００３】[0003]
【発明が解決しようとする課題】しかしながら、これら
の触媒は多くの場合目的とする生成物の収率が十分でな
かった。また、プロピオン酸とホルムアルデヒド又はホ
ルムアルデヒド誘導体との反応では、反応を長時間行う
と、主としてホルムアルデヒドに由来する高沸点物や炭
素質が沈着し、触媒の活性を長時間安定に維持すること
が困難であった。However, these catalysts often have insufficient yields of the desired product. In addition, in the reaction between propionic acid and formaldehyde or a formaldehyde derivative, if the reaction is carried out for a long time, high-boiling substances and carbonaceous materials mainly derived from formaldehyde are deposited, and it is difficult to stably maintain the activity of the catalyst for a long time. there were.
【０００４】本発明の目的は、触媒の改良により目的と
する生成物を高収率、高選択率で得ること、及び原料ガ
ス中に酸素を加えることにより、前記欠点を解消し長時
間安定に反応を維持することにある。[0004] It is an object of the present invention to obtain the desired product in a high yield and a high selectivity by improving the catalyst, and to add oxygen to the raw material gas to eliminate the above-mentioned drawbacks and to stabilize for a long time. Is to maintain the reaction.
【０００５】[0005]
【課題を解決するための手段】すなわち本発明は、プロ
ピオン酸とホルムアルデヒド又はホルムアルデヒド誘導
体と気相接触反応しメタクリル酸及びそのエステルを製
造するにあたり、一般式 ＮｂａＣｓｂＸｃＯｄ （式中Ｎｂ、Ｃｓ及びＯはそれぞれニオブ、セシウム及
び酸素を示し、Ｘはタングステン、銀、マグネシウム、
ニッケル、亜鉛、モリブデン、クロム、アンチモン、チ
タン及び白金からなる群より選ばれた少なくとも１種の
元素を示す。但し、ａ、ｂ、ｃ及びｄは各元素の原子比
率を表わし、ａ＝１０のときｂ＝０．１〜１、ｃ＝０〜
１であり、ｄは上記各成分の原子価を満足するのに必要
な酸素原子数である。）で表わされる触媒を使用するこ
とを特徴とするメタクリル酸の製造方法にあり、また、
原料ガスに０．１〜１０容量％の分子状酸素を含有させ
ることにより反応を長時間安定に保つ方法、及び原料ガ
スに低級アルコールを含有させメタクリル酸とメタクリ
ル酸エステルを同時に製造する方法にある。That is, the present invention provides a method for producing methacrylic acid and its ester by reacting propionic acid with formaldehyde or a formaldehyde derivative in the gas phase to produce methacrylic acid and its ester, wherein Nb, Cs and O are each represented by the general formula: X represents tungsten, silver, magnesium, niobium, cesium and oxygen;
It represents at least one element selected from the group consisting of nickel, zinc, molybdenum, chromium, antimony, titanium and platinum. Here, a, b, c and d represent the atomic ratio of each element, and when a = 10, b = 0.1 to 1, and c = 0 to
1, and d is the number of oxygen atoms required to satisfy the valence of each component. ) Is a method for producing methacrylic acid, characterized by using a catalyst represented by the formula:
There is a method of keeping the reaction stable for a long time by containing 0.1 to 10% by volume of molecular oxygen in the raw material gas, and a method of simultaneously producing methacrylic acid and methacrylic acid ester by containing a lower alcohol in the raw material gas. .
【０００６】本発明反応の原料として使用するホルムア
ルデヒド又はホルムアルデヒド誘導体とは、ホルムアル
デヒドのメタノール溶液、メチラール、トリオキサン、
バラホルムアルデヒド等であり、これらはホルムアルデ
ヒド又はホルムアルデヒド水溶液と混合して使用しても
よい。ホルムアルデヒドとしてメタノール溶液などを用
いる場合は供給メタノール量に応じてメタクリル酸と共
にメタクリル酸エステルを生成させることができる。The formaldehyde or formaldehyde derivative used as a starting material for the reaction of the present invention includes a formaldehyde methanol solution, methylal, trioxane,
Roseformaldehyde and the like, which may be used by mixing with formaldehyde or an aqueous formaldehyde solution. When a methanol solution or the like is used as formaldehyde, methacrylic acid esters can be produced together with methacrylic acid according to the amount of methanol supplied.
【０００７】本発明の触媒の調製に用いる原料化合物と
しては、各元素の硝酸塩、炭酸塩、アンモニウム塩、ハ
ロゲン化物、酸化物等を組合せて使用することができ
る。本発明の方法で用いる触媒は無担体でも有効である
が、酸化マグネシウム、酸化チタン等の担体に担持させ
ることもできる。担持方法は特に限定されないが、含浸
法、混練法、共沈法等の種々の方法を用いることができ
る。また、触媒は一般には固定床で用いられるが流動床
でも使用できる。As the raw material compounds used for preparing the catalyst of the present invention, nitrates, carbonates, ammonium salts, halides, oxides and the like of each element can be used in combination. The catalyst used in the method of the present invention is effective without a carrier, but may be supported on a carrier such as magnesium oxide or titanium oxide. The supporting method is not particularly limited, but various methods such as an impregnation method, a kneading method, and a coprecipitation method can be used. The catalyst is generally used in a fixed bed, but can also be used in a fluidized bed.
【０００８】反応に当り原料のプロピオン酸の供給量
と、ホルムアルデヒドおよびその誘導体の合計の供給量
との比率は、ホルムアルデヒド誘導体をホルムアルデヒ
ドに換算したモル比として１：１０〜１０：１が適当で
あり、特に１：５〜５：１が好ましい。In the reaction, the ratio of the supply amount of the raw material propionic acid to the total supply amount of formaldehyde and its derivative is suitably from 1:10 to 10: 1 as a molar ratio of the formaldehyde derivative converted to formaldehyde. And particularly preferably 1: 5 to 5: 1.
【０００９】これらの原料は、混合ガスとして供給され
ガス状で触媒と接触される。この場合、原料ガスは窒
素、炭酸ガス等の不活性ガスを加えて希釈してもよく、
また水蒸気を含んでいてもよい。[0009] These raw materials are supplied as a mixed gas and are brought into contact with the catalyst in a gaseous state. In this case, the raw material gas may be diluted by adding an inert gas such as nitrogen or carbon dioxide gas,
It may also contain steam.
【０００１０】触媒上の空間速度（ＳＶ）は５０〜５０
００ｍｌ／ｈｒ／ｍｌ−ｃａｔ．の範囲で選ぶことがで
きるが、特に１００〜３０００ｍｌ／ｈｒ／ｍｌ−ｃａ
ｔ．が好ましい。反応温度は２００〜５００℃の範囲で
選ぶことができ、特に２５０〜４５０℃が好ましい。The space velocity (SV) on the catalyst is 50-50.
00 ml / hr / ml-cat. Can be selected in the range of 100 to 3000 ml / hr / ml-ca.
t. Is preferred. The reaction temperature can be selected in the range of 200 to 500 ° C, and particularly preferably 250 to 450 ° C.
【００１１】本発明に於て原料ガスに分子状酸素を加え
る場合は、０．１〜１０容量％、特に好ましくは１〜６
容量％となるように調節する。分子状酸素を添加するこ
とにより触媒の活性を長期間高く維持することができ
る。When molecular oxygen is added to the raw material gas in the present invention, it is preferably 0.1 to 10% by volume, particularly preferably 1 to 6% by volume.
Adjust so as to be% by volume. By adding molecular oxygen, the activity of the catalyst can be kept high for a long time.
【００１２】プロピオン酸とホルムアルデヒド又はホル
ムアルデヒド誘導体との反応では、反応を長時間行うと
炭素質状のものが触媒上に沈着するため、活性を長期間
安定に維持することが困難である。しかしながら、触媒
を反応器内又は反応器外で５００℃から６００℃程度の
温度で酸素含有ガス雰囲気下又は酸素含有ガス及び水蒸
気存在下において再生することが可能である。従って、
前記方法を適用することにより、反応を長期間行うこと
ができる。In the reaction between propionic acid and formaldehyde or a formaldehyde derivative, if the reaction is carried out for a long time, carbonaceous substances are deposited on the catalyst, so that it is difficult to maintain the activity stably for a long time. However, it is possible to regenerate the catalyst inside or outside the reactor at a temperature of about 500 ° C. to 600 ° C. in an oxygen-containing gas atmosphere or in the presence of an oxygen-containing gas and steam. Therefore,
By applying the above method, the reaction can be performed for a long period of time.
【００１３】本発明に於てメタクリル酸とメタクリル酸
エステルを同時に得ようとする場合は、原料ガスにメタ
ノール、エタノール等の低級アルコールを含有させる。
低級アルコールは定量ポンプで原料混合物中に供給する
ことができるが、ホルムアルデヒドと混合して供給して
もよい。In the present invention, when methacrylic acid and methacrylic acid ester are to be obtained at the same time, a lower alcohol such as methanol or ethanol is contained in the raw material gas.
The lower alcohol can be supplied into the raw material mixture by a metering pump, or may be supplied by mixing with formaldehyde.
【００１４】[0014]
【実施例】以下に実施例及び比較例を挙げて本発明を更
に詳しく説明する。実施例における「部」は重量部を意
味し、プロピオン酸の転化率、生成したメタクリル酸及
びそのエステルの選択率は以下のように定義される。The present invention will be described in more detail with reference to the following Examples and Comparative Examples. In the examples, "parts" means parts by weight, and the conversion of propionic acid and the selectivity of methacrylic acid and its ester formed are defined as follows.
【００１５】[0015]
【数１】 (Equation 1)
【００１６】[0016]
【数２】 (Equation 2)
【００１７】[0017]
【数３】 (Equation 3)
【００１８】［実施例１］硝酸セシウム５．９部を純水
２００部に加熱溶解した。これに、五酸化ニオブ１００
部を撹拌しながら加えたのち、加熱して蒸発乾固した。
得られた固型物を１２０℃で１７時間乾燥後加圧成型
し、空気流通下に５００℃で５時間熱処理したものを触
媒として用いた。得られた触媒の酸素以外の元素の組成
（以下同じ）はＮｂ10Ｃｓ0.4 で、本触媒を反応器に充
填し、モル分率でプロピオン酸１０．０％、メタノール
を僅かに含有するホルムアルデヒド７．４％、窒素８
２．６％の原料ガスを反応温度３３０℃、空間速度８０
０ｍｌ／ｈｒ／ｍｌ−ｃａｔ．で供給した。１時間経過
後の生成物を捕集し、ガスクロマトグラフィーで分析し
たところ、プロピオン酸の転化率４０．０％、メタクリ
ル酸の選択率７９．８％、メタクリル酸メチルの選択率
２．６％であった。Example 1 5.9 parts of cesium nitrate was heated and dissolved in 200 parts of pure water. In addition, niobium pentoxide 100
After stirring, the mixture was heated and evaporated to dryness.
The obtained solid product was dried at 120 ° C. for 17 hours, molded under pressure, and heat-treated at 500 ° C. for 5 hours in an air stream to use as a catalyst. The obtained catalyst had a composition of elements other than oxygen (the same applies hereinafter) of Nb 10 Cs 0.4 , the catalyst was charged into a reactor, and a formaldehyde solution containing 10.0% by weight of propionic acid and slightly containing methanol was used. 0.4%, nitrogen 8
2.6% raw material gas is reacted at 330 ° C. and space velocity 80
0 ml / hr / ml-cat. Supplied with After 1 hour, the product was collected and analyzed by gas chromatography. As a result, the conversion of propionic acid was 40.0%, the selectivity of methacrylic acid was 79.8%, and the selectivity of methyl methacrylate was 2.6%. Met.
【００１９】［実施例２］実施例１に於て原料ガスに酸
素を４．６％加え、従って窒素のモル分率を７８．０％
とした原料ガスを用いて同様に反応を行ったところ、反
応開始後１時間経過した時点でのプロピオン酸の転化率
は４１．５％、メタクリル酸の選択率７４．６％、メタ
クリル酸メチルの選択率２．５％であったが、１０日間
経過後もプロピオン酸の転化率４１．５％、メタクリル
酸の選択率７４．６％、メタクリル酸メチルの選択率
２．５％であって反応初期と同じ活性を維持していた。Example 2 In Example 1, 4.6% of oxygen was added to the raw material gas, so that the molar fraction of nitrogen was 78.0%.
When the reaction was carried out in the same manner using the raw material gas, the conversion of propionic acid after 1 hour from the start of the reaction was 41.5%, the selectivity of methacrylic acid was 74.6%, and the conversion of methyl methacrylate was The selectivity was 2.5%, but after 10 days, the conversion of propionic acid was 41.5%, the selectivity of methacrylic acid was 74.6%, and the selectivity of methyl methacrylate was 2.5%. It maintained the same activity as in the beginning.
【００２０】［実施例３］硝酸セシウム５．９部及びパ
ラタングステン酸アンモニウム９．８部を純水２００部
に加熱混合した。これに五酸化ニオブ１００部を撹拌し
ながら加えたのち、加熱して蒸発乾固した。得られた固
型物を１２０℃で１７時間乾燥後加圧成型し、空気流通
下に５００℃で５時間熱処理したものを触媒として用い
た。得られた触媒の組成はＮｂ10Ｃｓ0.4 Ｗ0.5 であっ
た。実施例１と同じ条件で反応したところ、プロピオン
酸の転化率３８．５％、メタクリル酸の選択率８５．４
％、メタクリル酸メチルの選択率２．９％であった。Example 3 5.9 parts of cesium nitrate and 9.8 parts of ammonium paratungstate were mixed by heating with 200 parts of pure water. After 100 parts of niobium pentoxide was added thereto with stirring, the mixture was heated and evaporated to dryness. The obtained solid product was dried at 120 ° C. for 17 hours, molded under pressure, and heat-treated at 500 ° C. for 5 hours in an air stream to use as a catalyst. The composition of the resulting catalyst was Nb 10 Cs 0.4 W 0.5 . When the reaction was carried out under the same conditions as in Example 1, the conversion of propionic acid was 38.5% and the selectivity of methacrylic acid was 85.4.
%, And the selectivity of methyl methacrylate was 2.9%.
【００２１】［実施例４］実施例１に於て同じ条件で、
ただし酸素を４．６％加え窒素を７８．０％として反応
を行ったところ、反応開始から１時間の時点におけるプ
ロピオン酸の転化率は４０．０％、メタクリル酸の選択
率８０．１％、メタクリル酸メチルの選択率２．７％で
あった。更に１０日間経過した時点でのプロピオン酸の
転化率４０．０％、メタクリル酸の選択率８０．１％、
メタクリル酸メチルの選択率２．７％であって反応初期
と同じ触媒活性を維持していた。[Embodiment 4] Under the same conditions as in Embodiment 1,
However, when the reaction was carried out with 4.6% oxygen and 78.0% nitrogen, the conversion of propionic acid at the time of 1 hour from the start of the reaction was 40.0%, the selectivity of methacrylic acid was 80.1%, The selectivity of methyl methacrylate was 2.7%. After a further 10 days, the conversion of propionic acid was 40.0%, the selectivity of methacrylic acid was 80.1%,
The selectivity of methyl methacrylate was 2.7%, and the same catalytic activity as in the initial stage of the reaction was maintained.
【００２２】［実施例５］実施例３の触媒を反応器に充
填し、モル分率でプロピオン酸１０．０％、ホルムアル
デヒド７．４％、窒素８２．６％の原料ガスを反応温度
３３０℃、空間速度８００ｍｌ／ｈｒ／ｍｌ−ｃａｔ．
で供給した。１時間経過後の生成物を捕集し、ガスクロ
マトグラフィーで分析したところ、プロピオン酸の転化
率３８．５％、メタクリル酸の選択率８８．５％であっ
た。EXAMPLE 5 The catalyst of Example 3 was charged into a reactor, and a raw material gas containing 10.0% by weight of propionic acid, 7.4% of formaldehyde and 82.6% of nitrogen was reacted at a reaction temperature of 330 ° C. , Space velocity 800 ml / hr / ml-cat.
Supplied with After 1 hour, the product was collected and analyzed by gas chromatography. As a result, the conversion of propionic acid was 38.5% and the selectivity of methacrylic acid was 88.5%.
【００２３】［実施例６］実施例３の触媒を反応器に充
填し、モル分率でプロピオン酸１０．０％、ホルムアル
デヒド７．４％、メタノール１０．０％、窒素７２．６
％の原料ガスを反応温度３３０℃、空間速度８００ｍｌ
／ｈｒ／ｍｌ−ｃａｔ．で供給した。１時間経過後の生
成物を捕集し、ガスクロマトグラフィーで分析したとこ
ろ、プロピオン酸の転化率４０．０％、メタクリル酸の
選択率２８．４％、メタクリル酸メチルの選択率５６．
８％であった。EXAMPLE 6 The catalyst of Example 3 was charged into a reactor, and 10.0% by weight of propionic acid, 7.4% of formaldehyde, 10.0% of methanol, and 72.6 of nitrogen were used.
% Raw material gas at a reaction temperature of 330 ° C and a space velocity of 800 ml
/ Hr / ml-cat. Supplied with After one hour, the product was collected and analyzed by gas chromatography. As a result, the conversion of propionic acid was 40.0%, the selectivity of methacrylic acid was 28.4%, and the selectivity of methyl methacrylate was 56.
8%.
【００２４】［実施例７〜１４］実施例１に準じて表１
に示した各触媒を調製し、実施例１と同一条件（モル分
率でプロピオン酸１０．０％、メタノールを僅かに含有
するホルムアルデヒド７．４％、窒素８２．６％の原料
ガス）で反応した。表１に示す結果を得た。[Examples 7 to 14] Table 1 in accordance with Example 1
Were prepared and reacted under the same conditions as in Example 1 (a raw material gas containing 10.0% by weight of propionic acid, 7.4% of formaldehyde containing a small amount of methanol, and 82.6% of nitrogen). did. The results shown in Table 1 were obtained.
【００２５】[0025]
【表１】 [Table 1]
【００２６】［比較例１］実施例１に於て、硝酸セシウ
ムを添加しない、従ってＮｂだけからなる比較触媒を調
製した。この触媒を用い実施例１と同じ条件で反応した
ところ、プロピオン酸の転化率１０．０％、メタクリル
酸の選択率１０．０％でメタクリル酸メチルは殆ど生成
していなかった。Comparative Example 1 A comparative catalyst was prepared in the same manner as in Example 1 except that cesium nitrate was not added. Therefore, a comparative catalyst consisting only of Nb was prepared. When the reaction was carried out under the same conditions as in Example 1 using this catalyst, the conversion of propionic acid was 10.0% and the selectivity of methacrylic acid was 10.0%, and almost no methyl methacrylate was produced.
【００２７】［実施例１５］ 実施例１の触媒を用い、原料ガスに酸素を加えることな
しに、１０日間反応を続行した。その結果、プロピオン
酸の転化率３８．９％、メタクリル酸の選択率７８．５
％、メタクリル酸メチルの選択率２．５％で、触媒性能
が僅かながら低下していた。[ Example 15 ] Using the catalyst of Example 1, the reaction was continued for 10 days without adding oxygen to the raw material gas. As a result, the conversion of propionic acid was 38.9%, and the selectivity of methacrylic acid was 78.5.
% And a selectivity of methyl methacrylate of 2.5%, the catalyst performance was slightly reduced.
【００２８】[0028]
【発明の効果】本発明は、新規な触媒を用いることによ
ってメタクリル酸の収率の向上及び反応の長期間安定保
持が可能となり、又、原料ガスに低級アルコールを含有
させることによりメタクリル酸エステルを併産すること
ができる。According to the present invention, it is possible to improve the yield of methacrylic acid and to stably maintain the reaction for a long period of time by using a novel catalyst, and to convert a methacrylic acid ester by adding a lower alcohol to a raw material gas. Can be co-produced .
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｂ０１Ｊ 23/68 Ｃ０７Ｃ 51/353 23/847 67/08 Ｃ０７Ｃ 51/353 69/54 Ｚ 67/08 Ｃ０７Ｂ 61/00 ３００ 69/54 Ｂ０１Ｊ 23/64 １０２Ｘ // Ｃ０７Ｂ 61/00 ３００ 23/84 ３０１Ｘ (58)調査した分野(Int.Cl.6，ＤＢ名) C07C 57/05 C07C 51/353 C07C 67/08 C07C 69/54 ＣＡＰＬＵＳ（ＳＴＮ) ＲＥＧＩＳＴＲＹ（ＳＴＮ) ＷＰＩＤＳ（ＳＴＮ)──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 6 Identification code FI B01J 23/68 C07C 51/353 23/847 67/08 C07C 51/353 69/54 Z 67/08 C07B 61/00 300 69 / 54 B01J 23/64 102X // C07B 61/00 300 23/84 301X (58) Fields surveyed (Int.Cl. 6 , DB name) C07C 57/05 C07C 51/353 C07C 67/08 C07C 69/54 CAPPLUS (STN) REGISTRY (STN) WPIDS (STN)
Claims (3)
ルムアルデヒド誘導体と気相接触反応しメタクリル酸を
製造するにあたり、一般式 ＮｂａＣｓｂＸｃＯｄ （式中Ｎｂ、Ｃｓ及びＯはそれぞれニオブ、セシウム及
び酸素を示し、Ｘはタングステン、銀、マグネシウム、
ニッケル、亜鉛、モリブデン、クロム、アンチモン、チ
タン及び白金からなる群より選ばれた少なくとも１種の
元素を示す。但し、ａ、ｂ、ｃ及びｄは各元素の原子比
率を表わし、ａ＝１０のときｂ＝０．１〜１、ｃ＝０〜
１であり、ｄは上記各成分の原子価を満足するのに必要
な酸素原子数である。）で表わされる触媒を使用するこ
とを特徴とするメタクリル酸の製造方法。In producing methacrylic acid by reacting propionic acid with formaldehyde or a formaldehyde derivative in the gas phase, a general formula NbaCsbXcOd (wherein Nb, Cs and O represent niobium, cesium and oxygen, respectively, X represents tungsten, Silver, magnesium,
It represents at least one element selected from the group consisting of nickel, zinc, molybdenum, chromium, antimony, titanium and platinum. Here, a, b, c and d represent the atomic ratio of each element, and when a = 10, b = 0.1 to 1, and c = 0 to
1, and d is the number of oxygen atoms required to satisfy the valence of each component. A method for producing methacrylic acid, comprising using a catalyst represented by the following formula:
酸素を含有させることを特徴とする請求項１のメタクリ
ル酸の製造方法。2. The method for producing methacrylic acid according to claim 1, wherein the raw material gas contains 0.1 to 10% by volume of molecular oxygen.
アルコールを含有させることを特徴とするメタクリル酸
及びそのエステルの製造方法。3. The method for producing methacrylic acid and its ester according to claim 1, wherein the raw material gas contains a lower alcohol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4157439A JP2966650B2 (en) | 1992-05-25 | 1992-05-25 | Method for producing methacrylic acid and its ester |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4157439A JP2966650B2 (en) | 1992-05-25 | 1992-05-25 | Method for producing methacrylic acid and its ester |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05331097A JPH05331097A (en) | 1993-12-14 |
| JP2966650B2 true JP2966650B2 (en) | 1999-10-25 |
Family
ID=15649677
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4157439A Expired - Fee Related JP2966650B2 (en) | 1992-05-25 | 1992-05-25 | Method for producing methacrylic acid and its ester |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2966650B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012001394A1 (en) * | 2010-07-01 | 2012-01-05 | Lucite International Uk Limited | A mixed oxide catalyst and a process for the production of ethylenically unsaturated carboxylic acids or esters |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| MY120051A (en) | 1997-07-30 | 2005-08-30 | Mitsubishi Rayon Co | Process for purification of (meth)acrylic acid |
| US5998657A (en) * | 1998-04-15 | 1999-12-07 | Eastman Chemical Company | Process for the generation of α, β-unsaturated carboxylic acids and esters using niobium catalyst |
| JP5832678B1 (en) * | 2015-02-25 | 2015-12-16 | 日本ケッチェン株式会社 | Fatty acid alkyl ester production catalyst, production method thereof, and production method of fatty acid alkyl ester using the catalyst |
-
1992
- 1992-05-25 JP JP4157439A patent/JP2966650B2/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012001394A1 (en) * | 2010-07-01 | 2012-01-05 | Lucite International Uk Limited | A mixed oxide catalyst and a process for the production of ethylenically unsaturated carboxylic acids or esters |
| CN102985177A (en) * | 2010-07-01 | 2013-03-20 | 璐彩特国际英国有限公司 | A mixed oxide catalyst and a process for the production of ethylenically unsaturated carboxylic acids or esters |
| US8940924B2 (en) | 2010-07-01 | 2015-01-27 | Lucite International Uk Limited | Mixed oxide catalyst and a process for the production of ethylenically unsaturated carboxylic acids or esters |
| RU2579516C2 (en) * | 2010-07-01 | 2016-04-10 | ЛУСАЙТ ИНТЕРНЭШНЛ ЮКей ЛИМИТЕД | Mixed oxide based catalyst and method of producing ethylenically unsaturated carboxylic acids or esters |
| CN102985177B (en) * | 2010-07-01 | 2016-06-08 | 璐彩特国际英国有限公司 | Mixed oxide catalyst and the method for producing ethylenic unsaturated carboxylic acid or ester |
| KR101873036B1 (en) * | 2010-07-01 | 2018-07-02 | 루사이트 인터내셔널 유케이 리미티드 | A mixed oxide catalyst and a process for the production of ethylenically unsaturated carboxylic acids or esters |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH05331097A (en) | 1993-12-14 |
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