JP2003096025A - Method for producing glyoxylic acid monohydrate - Google Patents
Method for producing glyoxylic acid monohydrateInfo
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- JP2003096025A JP2003096025A JP2001287962A JP2001287962A JP2003096025A JP 2003096025 A JP2003096025 A JP 2003096025A JP 2001287962 A JP2001287962 A JP 2001287962A JP 2001287962 A JP2001287962 A JP 2001287962A JP 2003096025 A JP2003096025 A JP 2003096025A
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- glyoxylic acid
- weight
- acid monohydrate
- crystals
- aqueous solution
- Prior art date
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、グリオキシル酸水
溶液から白色、粉末状のグリオキシル酸１水塩を効率良
く、高純度で製造する方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for efficiently producing white and powdery glyoxylic acid monohydrate from an aqueous glyoxylic acid solution with high purity.
【０００２】[0002]
【従来の技術】グリオキシル酸は、通常４０〜５０重量
％程度の水溶液として生産、販売されているが、医薬
品、化粧品、染料の原料としての用途によっては水が不
純物とみなされることもあり粉末状のグリオキシル酸が
要求される場合がある。粉末状のグリオキシル酸として
はその１水塩か無水塩が知られているが、無水塩はその
製造方法に過酷な条件を必要とすることから、１水塩の
製造の方が現実的といえる。該１水塩は水中に投入した
時には、容易に水溶液となる性能のものであるので、水
溶液としての用途にも適合出来る上、水溶液に比べて輸
送費、貯蔵費の低減が図れるという利点がある。従来か
かる粉末状のグリオキシル酸塩を製造する方法として
は、グリオキシル酸水溶液を６５重量％程度にまで濃
縮し、これに種晶を添加してグリオキシル酸結晶を析出
させ、得られる結晶を媒体から分離しそれを乾燥する方
法や、グリオキシル酸水溶液を７０重量％以上になる
まで濃縮して、グリオキシル酸、グリオキザール、蓚酸
を特定の濃度にしたグリオキシル酸水溶液に種晶として
グリオキシル酸結晶を添加して、グリオキシル酸結晶を
析出させる粉末状グリオキシル酸の製造方法（特開昭５
３−７３５１７号公報）が知られている。2. Description of the Related Art Glyoxylic acid is usually produced and sold as an aqueous solution of about 40 to 50% by weight. However, depending on its use as a raw material for pharmaceuticals, cosmetics, and dyes, water may be regarded as an impurity, and powdery form. Glyoxylic acid may be required. As the powdery glyoxylic acid, its monohydrate or anhydrous salt is known. However, since the anhydrous salt requires severe conditions in its production method, it can be said that the production of monohydrate is more realistic. . Since the monohydrate has the property of easily becoming an aqueous solution when it is put into water, it is suitable for use as an aqueous solution and has an advantage that transportation cost and storage cost can be reduced as compared with the aqueous solution. . As a conventional method for producing such powdery glyoxylate salt, an aqueous glyoxylic acid solution is concentrated to about 65% by weight, seed crystals are added to this to precipitate glyoxylic acid crystals, and the obtained crystals are separated from the medium. Then, by drying it, or by concentrating the glyoxylic acid aqueous solution to 70% by weight or more, adding glyoxylic acid crystals as seed crystals to the glyoxylic acid aqueous solution in which glyoxylic acid, glyoxal, and oxalic acid have a specific concentration, Process for producing powdery glyoxylic acid by depositing glyoxylic acid crystals
No. 3-73517) is known.
【０００３】[0003]
【発明が解決しようとする課題】しかしながら、上記
の方法では、グリオキシル酸１水塩を製造することはで
きるが、結晶が析出した分散液が比較的高い粘度を有す
るので結晶を取得する際に濾過すると濾過性が悪くな
り、また遠心分離すると得られた結晶がブロッキングす
ることがある。また、の方法では、グリオキシル酸の
無水塩が主として生成し、高純度のグリオキシル酸１水
塩は得られないという問題がある。However, although the glyoxylic acid monohydrate can be produced by the above method, the dispersion in which crystals are precipitated has a relatively high viscosity, so filtration is performed when the crystals are obtained. Then, the filterability becomes poor, and the crystals obtained may be blocked by centrifugation. In addition, the method (1) has a problem that an anhydrous salt of glyoxylic acid is mainly produced and a highly pure glyoxylic acid monohydrate cannot be obtained.
【０００４】[0004]
【課題を解決するための手段】そこで、本発明者らが、
上記問題点の解決のため鋭意検討を行った結果、グリオ
キシル酸の５０〜７０重量％水溶液に粉末のグリオキシ
ル酸塩を添加して系中にグリオキシル酸１水塩の結晶を
析出させ得られる分散液中の固形分濃度が２０〜４０重
量％になった時点で該結晶を分離することにより、上記
の問題を引き起すことなくグリオシキル酸１水塩が効率
良く製造できることを見いだし本発明を完成した。Therefore, the present inventors have
As a result of intensive studies for solving the above problems, a dispersion liquid obtained by adding powdered glyoxylate to a 50 to 70% by weight aqueous solution of glyoxylic acid to precipitate crystals of glyoxylic acid monohydrate in the system. The present invention has been completed by finding that by isolating the crystals when the solid content concentration in the medium reaches 20 to 40% by weight, glyoxylic acid monohydrate can be efficiently produced without causing the above problems.
【０００５】[0005]
【発明の実施の形態】以下本発明を詳細に説明する。本
発明では、グリオキシル酸の５０〜７０重量％水溶液を
まず調製する。工業的に得られるグリオキシル酸水溶液
は通常４０〜５０重量％程度のもので、例えばグリオキ
ザール水溶液を硝酸酸化する方法、蓚酸の硫酸溶液を水
銀陽極を用いて電解還元する方法、ジクロル酢酸に酢酸
カリウムを作用させて生ずるジアセチル化物を水と共に
加熱する方法により製造される。本発明では適宜該水溶
液を濃縮してグリオキシル酸を５０〜７０重量％水溶液
とすることが必要で、好ましく６０〜６８重量％水溶液
とする。なおグリオキシル酸水溶液がすでに５０重量％
以上の高濃度の場合は濃縮は必ずしも必要ないが、グリ
オキシル酸１水塩の収率を向上させるために濃縮して６
０〜６８重量％水溶液とするのが好ましい。濃縮は７０
℃以下、更には４０〜７０℃の温度で、減圧度は１０4
Ｐａ以下で実施するのが好ましく、減圧度１０4Ｐａを
越えると濃縮効率が悪く、一方温度が該温度が７０℃を
越えると濃縮液が着色して好ましくない。濃縮時間は特
に制限されないが、５〜２０時間が好ましい。BEST MODE FOR CARRYING OUT THE INVENTION The present invention will be described in detail below. In the present invention, a 50-70 wt% aqueous solution of glyoxylic acid is first prepared. The glyoxylic acid aqueous solution obtained industrially is usually about 40 to 50% by weight. For example, a method of nitric acid oxidation of an aqueous solution of glyoxal, a method of electrolytically reducing a sulfuric acid solution of oxalic acid using a mercury anode, potassium acetate to dichloroacetic acid It is produced by a method of heating the diacetylated product produced by the reaction with water. In the present invention, it is necessary to appropriately concentrate the aqueous solution to a glyoxylic acid aqueous solution of 50 to 70% by weight, preferably 60 to 68% by weight. The glyoxylic acid aqueous solution is already 50% by weight.
In the case of the above high concentration, concentration is not always necessary, but concentration is increased to improve the yield of glyoxylic acid monohydrate.
It is preferably a 0 to 68% by weight aqueous solution. 70 concentrated
Depressurization degree is 10 4 or less at a temperature of 40 ° C to 70 ° C.
It is preferably carried out at a pressure of not more than Pa, and when the degree of vacuum exceeds 10 4 Pa, the concentration efficiency is poor, while when the temperature exceeds 70 ° C., the concentrate is colored, which is not preferable. The concentration time is not particularly limited, but is preferably 5 to 20 hours.
【０００６】濃縮後の濃度が５０重量％未満では、グリ
オキシル酸１水塩が析出しないことがあり、７０重量％
を越えるとグリオキシル酸１水塩と共にグリオキシル酸
無水塩が析出するため、グリオキシル酸１水塩の純度が
低下するので好ましくない。When the concentration after concentration is less than 50% by weight, glyoxylic acid monohydrate may not be precipitated, and the concentration is 70% by weight.
When it exceeds, the glyoxylic acid monohydrate is precipitated together with the glyoxylic acid monohydrate, so that the purity of the glyoxylic acid monohydrate is reduced, which is not preferable.
【０００７】上記濃縮を行い、濃度５０〜７０重量％と
なったグリオキシル酸水溶液は、種晶としての粉末のグ
リオキシル酸塩の添加に先だって冷却されるのが好まし
く、かかる冷却温度は３０℃以下が好ましく、更には１
５〜２５℃である。冷却温度が３０℃を越えるとグリオ
キシル酸１水塩の析出が不充分となることがあり好まし
くない。冷却の時に撹拌を省略しても差支えないが、結
晶析出促進の点では撹拌しながら行うのが好ましい。It is preferable that the aqueous glyoxylic acid solution having a concentration of 50 to 70% by weight as described above is cooled prior to the addition of powdered glyoxylate as a seed crystal, and the cooling temperature is 30 ° C. or lower. Preferably 1
It is 5 to 25 ° C. If the cooling temperature exceeds 30 ° C., the precipitation of glyoxylic acid monohydrate may be insufficient, which is not preferable. The stirring may be omitted at the time of cooling, but it is preferable that stirring is performed from the viewpoint of promoting crystal precipitation.
【０００８】次に、冷却したグリオキシル酸水溶液に種
晶として粉末のグリオキシル酸塩を添加する。かかるグ
リオキシル酸塩としては、グリオキシル酸無水物、１／
２水塩、１水塩の少なくとも１種が用いられ、好ましく
はグリオキシル酸１水塩である。添加量は溶液に対して
０．０５〜５重量％、更には０．１〜２重量％の範囲か
ら選択され、かかる添加量が０．０５重量％未満では結
晶の析出効果に乏しく、一方５重量％を越えても析出効
果の向上は認められない。Next, powdered glyoxylate as seed crystals is added to the cooled aqueous glyoxylic acid solution. Examples of such glyoxylate include glyoxylic acid anhydride, 1 /
At least one of dihydrate and monohydrate is used, and glyoxylic acid monohydrate is preferred. The amount of addition is selected from the range of 0.05 to 5% by weight, more preferably 0.1 to 2% by weight with respect to the solution, and if the amount of addition is less than 0.05% by weight, the effect of crystal precipitation is poor. No improvement in the precipitation effect is observed even if it exceeds the weight percentage.
【０００９】種晶を添加すると結晶が析出し始めるが、
種晶添加後は撹拌を省略しても差支えないが、撹拌して
おく方がサラサラした粉末状のグリオキシル酸１水塩の
結晶が得られるので有利である。かかる析出操作におい
ては、液温を１５〜２８℃に維持しながら操作を行うと
有利に結晶が得られる。When seed crystals are added, crystals start to precipitate,
After the seed crystals have been added, the stirring may be omitted, but it is advantageous to stir the mixture because glyoxylic acid monohydrate crystals in the form of powder can be obtained. In such precipitation operation, crystals can be advantageously obtained by performing the operation while maintaining the liquid temperature at 15 to 28 ° C.
【００１０】本発明では得られる分散液の固形分濃度が
２０〜４０重量％になった時点で分散液から結晶を分離
することが必要で、好ましい固形分濃度としては２４〜
３５重量％である。該濃度が２０重量％未満ではグリオ
キシル酸１水塩の析出が不充分で非常に収率が低くな
り、一方４０重量％を越えると、析出液中で結晶のブロ
ッキングが起り、結晶形態が変るためか濾過性が非常に
悪くなり、グリオキシル酸１水塩の収率が悪くなるので
不適当である。尚、本発明で固形分濃度は、種晶を添加
してから一定時間、例えば１時間ごとに得られる分散液
を一定量サンプリングして、２５℃、１００００回転／
分、５分の条件下で遠心分離して、上澄み液を取除いた
沈殿重量を測定して、（沈殿重量／サンプリング重量）
×１００（重量％）の計算に基づいて把握する。In the present invention, it is necessary to separate crystals from the dispersion when the solid content of the obtained dispersion reaches 20 to 40% by weight.
35% by weight. If the concentration is less than 20% by weight, the precipitation of glyoxylic acid monohydrate will be insufficient and the yield will be very low. On the other hand, if it exceeds 40% by weight, the blocking of crystals will occur in the precipitation liquid and the crystal form will change. The filterability is very poor, and the yield of glyoxylic acid monohydrate is poor, which is not suitable. Incidentally, in the present invention, the solid content concentration is 25 ° C., 10,000 rotations /
Minutes, centrifuge under the condition of 5 minutes, and the weight of the precipitate after removing the supernatant liquid was measured (precipitate weight / sampling weight)
Grasp it based on the calculation of × 100 (% by weight).
【００１１】次いで分散液から結晶を分離するのである
が、結晶の分離方法としては、濾過、遠心分離等を単独
あるいはそれらを組合わせて実施する。濾過の場合は、
ヌッチェ、ガラスフィルター等の装置で、２００〜３０
０メッシュの濾布やフィルターを用いて行い、遠心分離
は、横型連続遠心分離機、スクリューデカンタ、高速遠
心分離機、ピラー型遠心分離機、デ・ラバル型遠心分離
機、ウエストファリア型遠心分離機、底部排出型遠心分
離機、上部排出型遠心分離機、連続式バスケット型遠心
分離機等の遠心分離機で、５００〜２０００回転／分の
遠心力を掛けて１０〜１２０分程度実施される。かかる
操作により結晶中の遊離水は３重量％未満まで脱水させ
ることが好ましく、通常遊離水を０．５〜１．５重量％
まで脱水して最終製品とする。かかる遊離水が３重量％
を越えると結晶がブロッキングすることがあり好ましく
ない。Next, the crystals are separated from the dispersion liquid. As a method for separating the crystals, filtration, centrifugation, etc. are carried out individually or in combination. For filtration,
With a device such as nutche or glass filter, 200 to 30
It is performed using a 0 mesh filter cloth and a filter, and centrifugation is performed by a horizontal continuous centrifuge, a screw decanter, a high speed centrifuge, a pillar centrifuge, a de Laval centrifuge, a Westfalia centrifuge, Centrifuge such as bottom discharge type centrifuge, top discharge type centrifuge, continuous basket type centrifuge or the like is applied for about 10 to 120 minutes by applying a centrifugal force of 500 to 2000 rpm. The free water in the crystals is preferably dehydrated to less than 3% by weight by such an operation, and the free water is usually 0.5 to 1.5% by weight.
Dehydrated to final product. 3% by weight of such free water
If it exceeds the range, crystals may be blocked, which is not preferable.
【００１２】本発明の製造方法において、グリオキシル
酸１水塩は４０〜５０％程度の収率で得られるが、グリ
オキシル酸１水塩を濾別した後の濾液中にはグリオキシ
ル酸が残存しているので、これをリサイクル使用するこ
とにより工業的に効率良くグリオキシル酸１水塩を得る
ことが可能である。In the production method of the present invention, glyoxylic acid monohydrate is obtained in a yield of about 40 to 50%, but glyoxylic acid remains in the filtrate after the glyoxylic acid monohydrate is filtered off. Therefore, by recycling this, glyoxylic acid monohydrate can be industrially efficiently obtained.
【００１３】[0013]
【実施例】以下、本発明について実施例を挙げて具体的
に説明する。尚、例中「％」とあるのは特に断りのない
限り重量基準である。
実施例１
４０％グリオキシル酸水溶液（グリオキザール１．０
％、蓚酸１．５％含有）２０００ｋｇを反応缶に仕込み
内温を４５℃にした後、４×１０3Ｐａの圧力下で、脱
水を行い、グリオキシル酸濃度を６５％まで濃縮した。
該水溶液を２５℃に冷却した後、グリオキシル酸１水塩
を２ｋｇを添加して撹拌下に結晶を析出させた。１時間
おきに系内の分散液を２ｇ分取し、卓上遠心分離機〔ク
ボタ株式会社製（ＫＭ−１５２００）〕で２５℃で１０
０００回転／分の条件で５分間遠心分離して、その沈殿
重量を測定して、固形分濃度が２５％となった時点（撹
拌開始から１５時間）で結晶を２００メッシュの濾布で
濾過した。濾過性は良好で１時間で濾過が終了した。更
に、得られたケーキを田辺鉄工所製の横型遠心分離機
「Ｔ−４２」で１０００回転／分×２５分の遠心分離を
実施して脱水し、遊離水１．１％を含有する純度９９．
１％のグリオキシル酸１水塩５５０ｋｇ（蓚酸０．９％
含有）を得た〔収率４３％（対グリオキシル酸）〕。得
られた結晶はブロッキングはなく白色であった。EXAMPLES The present invention will be specifically described below with reference to examples. In the examples, "%" is based on weight unless otherwise specified. Example 1 40% glyoxylic acid aqueous solution (glyoxal 1.0
% Of oxalic acid (containing 1.5% of oxalic acid) was charged into a reaction vessel, the internal temperature was adjusted to 45 ° C., and then dehydration was performed under a pressure of 4 × 10 3 Pa to concentrate the glyoxylic acid concentration to 65%.
After cooling the aqueous solution to 25 ° C., 2 kg of glyoxylic acid monohydrate was added to precipitate crystals with stirring. Every 1 hour, 2 g of the dispersion liquid in the system was sampled, and a desktop centrifuge [Kubota Co., Ltd. (KM-15200)] was operated at 25 ° C. for 10 hours.
After centrifuging for 5 minutes under the condition of 000 rpm, the weight of the precipitate was measured, and when the solid content concentration reached 25% (15 hours from the start of stirring), the crystals were filtered with a 200-mesh filter cloth. . The filterability was good and the filtration was completed in 1 hour. Further, the obtained cake was dehydrated by performing centrifugation at 1000 rpm / 25 × 25 minutes with a horizontal centrifuge “T-42” manufactured by Tanabe Iron Works, and a purity of 99% containing 1.1% of free water. ．
550 kg of 1% glyoxylic acid monohydrate (0.9% oxalic acid)
Contained) (yield 43% (based on glyoxylic acid)). The obtained crystals were white without blocking.
【００１４】実施例２
実施例１において、冷却温度を２０℃に変更して、分散
液の固形分濃度が３０％となった時点（撹拌開始から１
５時間）で濾過を実施した以外は同様に処理したところ
濾過性は良好で１時間で濾過が終了し、遊離水１．３％
を含有する純度９９．３％のグリオキシル酸１水塩を６
００ｋｇ（蓚酸０．７％含有）得た〔収率４７％（対グ
リオキシル酸）〕。得られた結晶はブロッキングはなく
白色であった。Example 2 In Example 1, when the cooling temperature was changed to 20 ° C. and the solid content concentration of the dispersion became 30% (1 from the start of stirring).
The same treatment was carried out except that the filtration was carried out for 5 hours, and the filterability was good, and the filtration was completed in 1 hour.
Containing 99.3% pure glyoxylic acid monohydrate containing 6
00 kg (containing 0.7% oxalic acid) was obtained [yield 47% (to glyoxylic acid)]. The obtained crystals were white without blocking.
【００１５】実施例３
実施例１において、濾過操作を省略して遠心分離を繰返
して合計３回実施して、遊離水を１．１％含有する純度
９９．１％グリオキシル酸１水塩を５４０ｋｇ（蓚酸
０．９％含有）得た〔収率４３％（対グリオキシル
酸）〕。得られた結晶はブロッキングはなく白色であっ
た。Example 3 In Example 1, 540 kg of 99.1% pure glyoxylic acid monohydrate containing 1.1% of free water was obtained by repeating the centrifugation without filtration and repeating the centrifugation three times in total. (Containing 0.9% oxalic acid) Obtained [Yield 43% (vs. glyoxylic acid)]. The obtained crystals were white without blocking.
【００１６】比較例１
実施例１において、固形分濃度が１５％となった時点
（撹拌開始から５時間）で濾過を実施した以外は同様に
処理した。濾過性は良好で１時間で濾過でき、遊離水３
％を含有する純度９８．１％のグリオキシル酸１水塩を
１６０ｋｇ（蓚酸１．９％含有）得た。結晶は白色であ
ったが、収率は１２％（対グリオシキル酸）で極度に低
かった。Comparative Example 1 The same treatment as in Example 1 was carried out except that filtration was carried out when the solid content concentration reached 15% (5 hours from the start of stirring). It has good filterability and can be filtered in 1 hour.
% Of glyoxylic acid monohydrate having a purity of 98.1% (containing 1.9% oxalic acid) was obtained. The crystals were white, but the yield was 12% (vs. gliosic acid), which was extremely low.
【００１７】比較例２
実施例１において、固形分濃度が４５％となった時点
（撹拌開始から３０時間）で濾過を実施した以外は同様
に処理した。濾過性は悪く５時間を要し、遊離水１３％
を含有する純度８５％のグリオキシル酸１水塩を５５０
ｋｇ（蓚酸２％含有）を得た。得られた結晶はブロッキ
ングし、やや黄色となった。収率も３７％（対グリオキ
シル酸）と低かった。Comparative Example 2 The same treatment as in Example 1 was carried out except that filtration was carried out when the solid content concentration reached 45% (30 hours from the start of stirring). Filterability is poor and requires 5 hours, 13% free water
Glyoxylic acid monohydrate with a purity of 85% containing 550
kg (containing 2% oxalic acid) was obtained. The obtained crystals were blocked and turned slightly yellow. The yield was also low at 37% (to glyoxylic acid).
【００１８】比較例３
実施例１において、濃縮を省略して４０％グリオキシル
酸水溶液にグリオキシル酸１水塩を添加した以外は同様
に処理したが結晶の析出は認められなかった。Comparative Example 3 The same procedure as in Example 1 was carried out except that concentration was omitted and glyoxylic acid monohydrate was added to a 40% aqueous solution of glyoxylic acid, but no precipitation of crystals was observed.
【００１９】比較例４
実施例１において、濃縮条件を４５℃、１０3Ｐａに変
更してグリオキシル酸濃度を７５％に変更した以外は、
同様に処理した所、溶液全体が結晶化した。得られた結
晶４９２ｋｇはグリオキシル酸無水塩を主成分（グリオ
キシル酸無水物８５．５％、グリオキシル酸１水塩１０
％、蓚酸２％、遊離水２．５％含有）とするものであっ
た。Comparative Example 4 Except that in Example 1, the concentration conditions were changed to 45 ° C. and 10 3 Pa and the glyoxylic acid concentration was changed to 75%.
When treated in the same manner, the entire solution crystallized. The obtained crystals (492 kg) were mainly composed of glyoxylic acid anhydride (glyoxylic acid anhydride 85.5%, glyoxylic acid monohydrate 10%).
%, Oxalic acid 2%, free water 2.5%).
【００２０】[0020]
【発明の効果】本発明では、グリオキシル酸の５０〜７
０重量％水溶液に粉末のグリオキシル酸塩を添加してグ
リオキシル酸の１水塩の結晶を析出させ得られる分散液
中の固形分濃度が２０〜４０重量％になった時点で該結
晶を分離することにより、濾過性が良好で、高純度で白
色のグリオキシル酸１水塩を得ることができる。In the present invention, glyoxylic acid of 50 to 7
Powder glyoxylate is added to a 0% by weight aqueous solution to precipitate crystals of glyoxylic acid monohydrate, and the crystals are separated when the solid content concentration in the resulting dispersion becomes 20 to 40% by weight. Thus, white glyoxylic acid monohydrate with high filterability and high purity can be obtained.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 鈴木 秀昭 岐阜県大垣市本今町1530番地 大垣化成工 業株式会社内 (72)発明者 大下 彰尚 岐阜県大垣市本今町1530番地 大垣化成工 業株式会社内 Ｆターム(参考） 4H006 AA02 AD15 BB31 BC51 BQ10 BS10 ─────────────────────────────────────────────────── ─── Continued front page (72) Inventor Hideaki Suzuki 1530 Motoimamachi, Ogaki City, Gifu Prefecture Ogaki Chemical Industry Business (72) Inventor Akinoshita Oshita 1530 Motoimamachi, Ogaki City, Gifu Prefecture Ogaki Chemical Industry Business F-term (reference) 4H006 AA02 AD15 BB31 BC51 BQ10 BS10
Claims (4)
液に粉末のグリオキシル酸塩を添加して系中にグリオキ
シル酸１水塩の結晶を析出させ得られる分散液中の固形
分濃度が２０〜４０重量％になった時点で該結晶を分離
することを特徴とするグリオシキル酸１水塩の製造方
法。1. A solid content concentration of 20 to 40 in a dispersion obtained by adding powdered glyoxylate to an aqueous solution of 50 to 70% by weight of glyoxylic acid to precipitate crystals of glyoxylic acid monohydrate in the system. A method for producing gliosicyl acid monohydrate, characterized in that the crystals are separated at the time when the weight% is reached.
液を用いることを特徴とする請求項１記載のグリオキシ
ル酸１水塩の製造方法。2. The method for producing glyoxylic acid monohydrate according to claim 1, wherein a 60 to 68% by weight aqueous solution of glyoxylic acid is used.
液が、グリオキシル酸の５０重量％未満の水溶液を７０
℃以下で濃縮して製造されることを特徴とする請求項２
記載のグリオキシル酸１水塩の製造方法。3. A 60 to 68 wt% aqueous solution of glyoxylic acid is an aqueous solution of less than 50 wt% of glyoxylic acid.
It is manufactured by concentrating at a temperature of ℃ or below.
A method for producing the described glyoxylic acid monohydrate.
液がグリオキシル酸の５０重量％未満の水溶液を７０℃
以下で濃縮して製造され、次いで３０℃以下の温度で冷
却した後、粉末のグリオキシル酸塩を添加することを特
徴とする請求項２記載のグリオキシル酸１水塩の製造方
法。4. A 60 to 68% by weight aqueous solution of glyoxylic acid is an aqueous solution containing less than 50% by weight of glyoxylic acid at 70 ° C.
3. The method for producing glyoxylic acid monohydrate according to claim 2, wherein the glyoxylic acid monohydrate is added after adding the powdered glyoxylate after being concentrated and produced at the following temperature and then cooled at a temperature of 30 [deg.] C. or less.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001287962A JP2003096025A (en) | 2001-09-21 | 2001-09-21 | Method for producing glyoxylic acid monohydrate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001287962A JP2003096025A (en) | 2001-09-21 | 2001-09-21 | Method for producing glyoxylic acid monohydrate |
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|---|---|
| JP2003096025A true JP2003096025A (en) | 2003-04-03 |
Family
ID=19110683
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009221234A (en) * | 2009-07-09 | 2009-10-01 | Takasago Internatl Corp | Method of manufacturing glyoxylic acid ester dimer, and novel glyoxylic acid ester dimer |
| CN105669433A (en) * | 2016-03-04 | 2016-06-15 | 武汉科技大学 | Preparation method of glyoxalic acid monohydrate crystals |
-
2001
- 2001-09-21 JP JP2001287962A patent/JP2003096025A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009221234A (en) * | 2009-07-09 | 2009-10-01 | Takasago Internatl Corp | Method of manufacturing glyoxylic acid ester dimer, and novel glyoxylic acid ester dimer |
| CN105669433A (en) * | 2016-03-04 | 2016-06-15 | 武汉科技大学 | Preparation method of glyoxalic acid monohydrate crystals |
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