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JPS6141342B2 - - Google Patents
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JPS6141342B2 - - Google Patents

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Publication number
JPS6141342B2
JPS6141342B2 JP10161778A JP10161778A JPS6141342B2 JP S6141342 B2 JPS6141342 B2 JP S6141342B2 JP 10161778 A JP10161778 A JP 10161778A JP 10161778 A JP10161778 A JP 10161778A JP S6141342 B2 JPS6141342 B2 JP S6141342B2
Authority
JP
Japan
Prior art keywords
copper salt
copper
benzophenone
liquid
imine
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
Application number
JP10161778A
Other languages
Japanese (ja)
Other versions
JPS5528931A (en
Inventor
Tomya Itsushiki
Tetsuo Tomita
Osamu Aoki
Mitsuo Abe
Takao Kondo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Gas Chemical Co Inc
Original Assignee
Mitsubishi Gas Chemical Co Inc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mitsubishi Gas Chemical Co Inc filed Critical Mitsubishi Gas Chemical Co Inc
Priority to JP10161778A priority Critical patent/JPS5528931A/en
Publication of JPS5528931A publication Critical patent/JPS5528931A/en
Publication of JPS6141342B2 publication Critical patent/JPS6141342B2/ja
Granted legal-status Critical Current

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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Description

【発明の詳細な説明】 本発明はベンゾフエノンイミン類を銅塩触媒の
存在下、ベンゾフエノン類を溶媒とし、分子状酸
素で酸化して、ベンゾフエノンアジン類を製造
し、次いで反応液に酸素ガス存在下、特定量のア
ンモニア水を連続的に添加して銅塩を沈澱させ、
この沈澱にベンゾフエノンイミン類を添加して銅
イミン錯体を形成させて回収し、ベンゾフエノン
イミン類の酸化触媒として使用する方法に関す
る。ベンゾフエノンイミンを塩化第1銅の存在
下、分子状酸素で酸化し、ベンゾフエノンアジン
を製造する方法は米国特許第2870206号に知られ
ている。そして該特許には、使用された触媒を反
応液から除去する方法について、反応液を加圧下
に110℃でアンモニア水で処理する方法と、反応
液と塩化アンモニウムの過飽和溶液とを110℃で
処理する方法とが記載されている。 上記方法によれば、確かに反応液から、銅塩を
取り除くことは出来るが、このようにして回収し
た銅塩は銅・アンミン錯体水溶液であり、それか
ら銅塩触媒を再生し使用するのは容易な事ではな
い。アンモニア水で処理する方法では銅塩の一部
が酸化銅に変化し、酸化銅から塩化第1銅を再生
するのは繁雑であること、およびアンモニア水溶
液からアンモニア水を留去しなければならず、こ
のようにして回収した銅塩にはアンモニアが強固
に結合しており、ベンゾフエノンイミンに溶解し
ない為に、再使用不能の銅塩が相当量生成するこ
とである。又、塩化アンモニウムの過飽和溶液で
処理する方法では、やはり水を留去しなければな
らず、又回収銅塩と塩化アンモニウムとを分離す
るという、やつかいな問題が生じ、回収率も若干
劣るため未回収の銅塩がベンゾフエノンアジン中
に残留すること、更に塩化アンモニウムによつ
て、ベンゾフエノンイミン及びベンゾフエノン類
の塩素化反応が起つて、塩化ベンゾフエノン類が
生成するという問題が生じることである。 本発明者らは、かかる欠点を解消する銅塩の回
収方法について鋭意検討した結果先に反応液に、
分子状酸素の存在下、または非存在下に少量の水
を添加して、銅塩を固体として回収する方法を、
特願昭51−147453号及び特願昭52−53445号とし
て出願した。 本発明者らは、更に深い検討を行なつた結果、
ベンゾフエノンを溶媒としてベンゾフエノンイミ
ンを酸化して、ベンゾフエノンアジンを連続製造
する操作を行なつた場合、第2銅塩の析出した反
応液の得られる事が多く、このような析出銅塩は
微小であつて、過操作によつて分離する事が著
しく困難である事が判明した。しかもこのような
反応液に対しては、水を添加しても、銅塩の回収
率が悪く、かつ又銅塩がスラツジ化(有機層との
分離が悪くかつ水分が多いため器壁に付着しやす
い状態)する事も判明した。 本発明は、このような銅塩の析出した反応液か
ら、銅塩を過し易い形態で凝集沈殿化するに
は、いかにすれば良いか種々検討した結果完成さ
れたものである。 すなわち本発明は、ベンゾフエノンイミン類を
銅塩触媒の存在下、分子状酸素で酸化してベンゾ
フエノンアジン類を製造し、反応液に酸素ガス存
在下アンモニアが銅塩の0.1〜4倍モル、水が銅
塩の0.5〜40倍モルとなる量のアンモニア水を連
続的に添加し接触させることにより銅塩を凝集沈
澱させ、上澄液を濾別し、当該凝集沈澱銅塩を含
むスラリー液をベンゾフエノンイミン類と混合し
て銅イミン錯体を形成させベンゾフエノンイミン
類酸化触媒として使用することを特徴とするベン
ゾフエノンアジン類の製造法である。 本発明において、銅塩を凝集沈殿させる為に添
加されるアンモニア水の量は前記の如く系内に存
在する銅塩に対してアンモニアは0.1〜4倍モル
比、水は0.5〜40倍モル比である。なお酸化終了
時に反応系中に析出している銅塩が存在する場合
には、未析出の銅に対して前述程度のアンモニア
水を添加すると凝集性の良好な銅塩が沈殿として
えられる。又、添加するアンモニア水の濃度範囲
は0.1〜28%、特に5〜20%が適当である。濃度
の低いものを用いると、沈殿がスラツジ化して、
過操作が困難になる。濃度の高いものを用いる
と、局部的にアンモニアが高濃度になる為に少量
ではあるが、酸化銅の生成を防止出来ない。更
に、反応したアンモニアの量は銅塩の0.1〜3倍
モル程度であることが好ましい。 本発明を行なうに際しての銅塩回収の為の操作
条件として、アンモニア水の添加温度は60〜250
℃、特に70〜140℃が適当である。一般的傾向と
して、温度の低い方が銅塩の析出、凝集の状態が
良く、回収率も高くなる。 本発明で用いられる触媒銅塩の形態は、特に銅
のハロゲン化物が適当であり、特に塩化第1銅、
塩化第2銅、オキシ塩化銅、臭化第1銅、臭化第
2銅、オキシ臭化銅、沃化銅等およびそれらの混
合物などに適用する事が出来る。 本発明における圧力は、常圧でも加圧でも特に
問題はない。 本発明方法におけるイミンの酸化反応の反応条
件として反応温度は60〜250℃であるが、特に70
〜230℃が好ましい。圧力は常圧でも加圧でも特
に制限はないが、酸素含有ガスとして純酸素を用
いた場合には1〜10気圧、空気を用いた場合には
1〜20気圧程度が適当である。触媒は原料イミン
化合物1モルに対し1/100〜1モル添加するのが
好ましい。 本発明の酸化反応及び銅塩回収方法においては
未反応ベンゾフエノン類が溶媒として働くので溶
媒は必ずしも添加する必要はないが、反応により
生成するベンゾフエノンアジン類の溶解溶媒とし
て用いるベンゾフエノン類の量は、ベンゾフエノ
ンイミン類の2〜6倍量が適当である。ベンゾフ
エノン類の量が少ないと、酸化によつて生成する
ベンゾフエノンアジンが高濃度となる為に、反応
液の粘度が非常に高くなり、かつ又反応液の融点
が高くなつて操作上甚だ不都合を来たす。又ベン
ゾフエノン類の量が多いとベンゾフエノンイミン
の濃度が低下する為に酸化速度が低下する事にな
る。 本発明反応において原料として使用されるベン
ゾフエノンイミン類とは次の一般式で示される化
合物である。 (但し上記式において、R1およびR2は水素、ハロ
ゲン、アルキル、アルコキシ又はニトロ基を示
す。R1とR2は互に同一でも異なつていても良
い。又m、nは1〜5の整数である。) 特にベンゾフエノンイミンの他、2−メチル、
3−メチル、4−メチル、4−クロル、4−ニト
ロ、4−メトキシベンゾフエノンイミンが好適に
用いられる。 又対象となる反応はベンゾフエノン類にアンモ
ニヤ及び酸素含有ガスを同時に加え反応させ、1
段でベンゾフエノンアジン類を製造する方法も本
発明の範囲に含まれる。 本発明方法によれば、銅塩は第1銅塩、第2銅
塩の区別なくいずれも固体として凝集沈澱し、こ
れはベンゾフエノンイミン類に速やかに溶解して
銅ベンゾフエノンイミン錯体を形成し、再びベン
ゾフエノンイミン類の酸化反応触媒として何等の
支障なく使用することができる。 実施例 1 上下フランジ式の内容積1.5のステンレス製
反応器に、原料液を毎時400g(液組成は原料液
1Kg中にベンゾフエノンイミン229.5g、ベンゾ
フエノン764g、塩化第1銅6.5gを含む)の割合
で供給し、反応器中の液温を120℃に保つ。次い
で、反応器の底部に位置するリングスパージヤー
から4気圧の加圧空気を常圧下での体積として毎
分3の流速で吹き込み、撹拌しながら連続反応
を行つた。液の平均滞留時間は2時間に保ち、反
応開始から約5時間で定常状態に達してから、以
後95時間連続的に反応を行なつた。反応率は95%
にほとんど安定していた。 反応液はオーバーフローによつて、一旦中間タ
ンクに連続的に抜き出した後、定時的に外部に取
り出すようにした。又廃ガスは冷却器で冷却して
同伴しているベンゾフエノンを回収した後、常圧
に戻して大気中に放出するようにした。 加圧中間タンクより抜き出された酸化反応液
は、保温された常圧の貯槽に貯液する。酸化反応
液を貯槽よりポンプを用いて、毎時400gの割合
で、内容積0.5の撹拌槽に送液し、同時に撹拌
槽へ濃度14%のアンモニア水を毎時5mlの割合で
供給し空気中激しく混合した。撹拌槽をオーバー
フローした液を静置槽に導き、析出した銅塩を沈
降分離した後、上澄液をテフロン布を通して外
部に抜き出した。この様にして、銅塩回収操作を
95時間連続的に行なつた。銅塩濃度100〜
200ppm(回収操作前の濃度6500ppm)に低下し
た液が得られるが、この液から更に15%のアンモ
ニア水を用いて加圧下に液々抽出を行なつて、銅
塩濃度を5〜20ppmまでにする事が出来るもの
であつた。 一方、静置槽の底部からは、濃度25〜35%に濃
縮された銅塩のスラリー液が得られた(回収率97
〜98.5%)。このスラリー液は、そのままベンゾ
フエノンイミン液と混合して、銅イミン錯体を製
造し、再び酸化反応に用いることができた。な
お、銅塩の組成は、ほぼCuCl2・Cu(OH)2
(NH3)m・(H2O)n(m=0.4〜1.4、n=0〜
1.0)のような組成であつた。 比較例 1、2 実施例1で得られた酸化液を用いて実施例1と
同様に該酸化液を毎時400gの割合で内容積0.5
の撹拌槽に送液し、同時に撹拌槽へ濃度14%のア
ンモニア水を表−1に示す流量で供給し空気中で
激しく混合した。撹拌槽をオーバーフローした液
を静置槽に導いた。条件及び結果を実施例1と対
比して表−1に示す。 【表】
DETAILED DESCRIPTION OF THE INVENTION The present invention produces benzophenoneazines by oxidizing benzophenone imines with molecular oxygen in the presence of a copper salt catalyst, using benzophenones as a solvent; In the presence of oxygen gas, a specific amount of ammonia water is continuously added to precipitate copper salts,
The present invention relates to a method of adding benzophenone imines to this precipitate to form a copper imine complex, which is recovered and used as an oxidation catalyst for benzophenone imines. A process for producing benzophenone azine by oxidizing benzophenone imine with molecular oxygen in the presence of cuprous chloride is known from US Pat. No. 2,870,206. The patent describes a method for removing the used catalyst from the reaction solution, including a method in which the reaction solution is treated with aqueous ammonia at 110℃ under pressure, and a method in which the reaction solution is treated with a supersaturated solution of ammonium chloride at 110℃. It describes how to do this. According to the above method, it is certainly possible to remove copper salt from the reaction solution, but the copper salt recovered in this way is an aqueous solution of copper/ammine complex, and it is easy to regenerate and use the copper salt catalyst from there. It's not a big deal. In the method of treatment with aqueous ammonia, part of the copper salt changes to copper oxide, and it is complicated to regenerate cuprous chloride from copper oxide, and the aqueous ammonia must be distilled off from the aqueous ammonia solution. Since ammonia is strongly bound to the copper salt recovered in this way and is not dissolved in benzophenone imine, a considerable amount of copper salt that cannot be reused is produced. In addition, in the method of treatment with a supersaturated solution of ammonium chloride, water still has to be distilled off, and the recovery rate is also slightly lower due to the complicated problem of separating the recovered copper salt and ammonium chloride. The problem is that the recovered copper salt remains in the benzophenone azine, and ammonium chloride causes a chlorination reaction of benzophenone imine and benzophenones to produce benzophenones chloride. . The present inventors have conducted extensive studies on a method for recovering copper salts that overcomes these drawbacks.
A method for recovering copper salts as a solid by adding a small amount of water in the presence or absence of molecular oxygen is described.
The patent application was filed as Japanese Patent Application No. 147453/1983 and Japanese Patent Application No. 53445/1982. As a result of further in-depth study, the inventors found that
When benzophenone imine is oxidized using benzophenone as a solvent to continuously produce benzophenone azine, a reaction solution in which a cupric salt is precipitated is often obtained; It was found that the particles were so small that it was extremely difficult to separate them by over-manipulating them. Moreover, even if water is added to such a reaction solution, the recovery rate of the copper salt is poor, and the copper salt becomes a sludge (separation from the organic layer is poor and the water content is high, so it adheres to the vessel wall). It was also found that the condition is easy to do. The present invention was completed as a result of various studies on how to coagulate and precipitate copper salts from a reaction solution in which such copper salts are precipitated in a form that is easy to pass through. That is, the present invention produces benzophenoneazines by oxidizing benzophenone imines with molecular oxygen in the presence of a copper salt catalyst, and the reaction solution contains 0.1 to 4 times as much ammonia as the copper salt in the presence of oxygen gas. The copper salt is coagulated and precipitated by continuously adding and contacting aqueous ammonia in an amount such that the mole of water is 0.5 to 40 times the mole of the copper salt, and the supernatant liquid is filtered and contains the coagulated and precipitated copper salt. This is a method for producing benzophenoneazines, which is characterized in that a slurry liquid is mixed with benzophenoneimines to form a copper imine complex, which is used as a benzophenoneimine oxidation catalyst. In the present invention, the amount of ammonia water added to coagulate and precipitate the copper salt is as described above, with the amount of ammonia being 0.1 to 4 times the molar ratio and the amount of water being 0.5 to 40 times the amount of the copper salt present in the system. It is. If there is a precipitated copper salt in the reaction system at the end of the oxidation, adding aqueous ammonia in the amount described above to the unprecipitated copper will yield a well-coagulated copper salt as a precipitate. Further, the concentration range of the ammonia water to be added is preferably 0.1 to 28%, particularly 5 to 20%. If a low concentration is used, the precipitate will turn into sludge,
It becomes difficult to over-operate. If a high concentration ammonia is used, the ammonia concentration will be high locally, so it will not be possible to prevent the production of copper oxide, although it may be a small amount. Further, the amount of reacted ammonia is preferably about 0.1 to 3 times the mole of the copper salt. As the operating conditions for copper salt recovery when carrying out the present invention, the addition temperature of ammonia water is 60 to 250.
℃, especially 70 to 140℃ is suitable. As a general tendency, the lower the temperature, the better the precipitation and aggregation of copper salts, and the higher the recovery rate. The form of the catalytic copper salt used in the present invention is particularly suitable as a copper halide, particularly cuprous chloride,
It can be applied to cupric chloride, copper oxychloride, cuprous bromide, cupric bromide, copper oxybromide, copper iodide, and mixtures thereof. The pressure in the present invention may be normal pressure or increased pressure without any particular problem. As a reaction condition for the imine oxidation reaction in the method of the present invention, the reaction temperature is 60 to 250°C, but especially 70°C.
~230°C is preferred. The pressure is not particularly limited, whether normal pressure or pressurization, but when pure oxygen is used as the oxygen-containing gas, 1 to 10 atm, and when air is used, about 1 to 20 atm is appropriate. The catalyst is preferably added in an amount of 1/100 to 1 mol per 1 mol of the raw material imine compound. In the oxidation reaction and copper salt recovery method of the present invention, unreacted benzophenones act as a solvent, so it is not necessarily necessary to add a solvent, but the amount of benzophenones used as a dissolving solvent for benzophenone azine produced by the reaction is , 2 to 6 times the amount of the benzophenone imine is suitable. If the amount of benzophenones is small, the concentration of benzophenone azine produced by oxidation will be high, resulting in a very high viscosity of the reaction solution and a high melting point of the reaction solution, which is extremely inconvenient for operation. will come. Furthermore, if the amount of benzophenones is large, the concentration of benzophenone imine decreases, resulting in a decrease in the oxidation rate. The benzophenoneimines used as raw materials in the reaction of the present invention are compounds represented by the following general formula. (However, in the above formula, R 1 and R 2 represent hydrogen, halogen, alkyl, alkoxy, or nitro group. R 1 and R 2 may be the same or different. Also, m and n are 1 to 5 ) In particular, in addition to benzophenoneimine, 2-methyl,
3-methyl, 4-methyl, 4-chloro, 4-nitro, 4-methoxybenzophenonimine are preferably used. The target reaction is to simultaneously add ammonia and oxygen-containing gas to benzophenones and react.
Also included within the scope of the present invention is a method for producing benzophenoneazines in steps. According to the method of the present invention, both copper salts, cuprous salts and cupric salts, coagulate and precipitate as solids, which are quickly dissolved in benzophenone imines to form copper benzophenone imine complexes. It can be used again as a catalyst for the oxidation reaction of benzophenone imines without any problems. Example 1 400 g of raw material liquid was fed per hour into a stainless steel reactor with an upper and lower flange type and an internal volume of 1.5 (liquid composition: 1 kg of raw material liquid contained 229.5 g of benzophenone imine, 764 g of benzophenone, and 6.5 g of cuprous chloride). The liquid temperature in the reactor is maintained at 120℃. Next, pressurized air of 4 atmospheres was blown into the reactor from a ring spargeer located at the bottom of the reactor at a flow rate of 3 per minute based on the volume under normal pressure, and a continuous reaction was carried out with stirring. The average residence time of the liquid was maintained at 2 hours, and after reaching a steady state approximately 5 hours after the start of the reaction, the reaction was continued for the next 95 hours. Response rate is 95%
was almost stable. The reaction solution was first drawn out continuously into an intermediate tank by overflow, and then taken out to the outside at regular intervals. In addition, the waste gas was cooled with a cooler to recover the accompanying benzophenone, and then returned to normal pressure and released into the atmosphere. The oxidation reaction liquid extracted from the pressurized intermediate tank is stored in a heated storage tank at normal pressure. The oxidation reaction liquid was sent from the storage tank using a pump at a rate of 400 g per hour to a stirring tank with an internal volume of 0.5, and at the same time, aqueous ammonia with a concentration of 14% was supplied to the stirring tank at a rate of 5 ml per hour and mixed vigorously in the air. did. The liquid that overflowed the stirring tank was led to a static tank, and the precipitated copper salt was separated by sedimentation, and then the supernatant liquid was extracted to the outside through a Teflon cloth. In this way, the copper salt recovery operation is carried out.
This was done continuously for 95 hours. Copper salt concentration 100~
A liquid with a concentration of 200 ppm (concentration 6,500 ppm before the recovery operation) is obtained, but this liquid is further subjected to liquid-liquid extraction under pressure using 15% aqueous ammonia to reduce the copper salt concentration to 5 to 20 ppm. It was something I could do. On the other hand, a copper salt slurry solution with a concentration of 25-35% was obtained from the bottom of the static tank (recovery rate 97%).
~98.5%). This slurry liquid was mixed with the benzophenone imine liquid as it was to produce a copper imine complex, which could be used again in the oxidation reaction. The composition of the copper salt is approximately CuCl 2・Cu(OH) 2
( NH3 )m・( H2O )n(m=0.4~1.4, n=0~
1.0). Comparative Examples 1 and 2 Using the oxidizing liquid obtained in Example 1, the oxidizing liquid was added at a rate of 400 g/hour to an internal volume of 0.5 in the same manner as in Example 1.
At the same time, aqueous ammonia with a concentration of 14% was supplied to the stirring tank at the flow rate shown in Table 1 and mixed vigorously in air. The liquid that overflowed the stirring tank was led to a static tank. The conditions and results are shown in Table 1 in comparison with Example 1. 【table】

Claims (1)

【特許請求の範囲】[Claims] 1 ベンゾフエノンイミン類を銅塩触媒の存在
下、分子状酸素で酸化してベンゾフエノンアジン
類を製造し、反応液に酸素ガス存在下アンモニア
が銅塩の0.1〜4倍モル、水が銅塩の0.5〜40倍モ
ルとなる量のアンモニア水を連続的に添加し接触
させることにより銅塩を凝集沈澱させ、上澄液を
濾別し、当該凝集沈澱銅塩を含むスラリー液をベ
ンゾフエノンイミン類と混合して銅イミン錯体を
形成させベンゾフエノンイミン類酸化触媒として
使用することを特徴とするベンゾフエノンアジン
類の製造法。
1. Oxidize benzophenoneimines with molecular oxygen in the presence of a copper salt catalyst to produce benzophenoneazines, and in the presence of oxygen gas, the reaction solution contains ammonia of 0.1 to 4 times the mole of copper salt and water. The copper salt is coagulated and precipitated by continuously adding and contacting aqueous ammonia in an amount of 0.5 to 40 times the mole of the copper salt, the supernatant liquid is filtered, and the slurry containing the coagulated and precipitated copper salt is subjected to benzodilation. 1. A method for producing benzophenone azines, which comprises mixing them with phenone imines to form a copper imine complex and using the complex as a benzophenone imine oxidation catalyst.
JP10161778A 1978-08-21 1978-08-21 Preparation of benzophenoneazine Granted JPS5528931A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP10161778A JPS5528931A (en) 1978-08-21 1978-08-21 Preparation of benzophenoneazine

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP10161778A JPS5528931A (en) 1978-08-21 1978-08-21 Preparation of benzophenoneazine

Publications (2)

Publication Number Publication Date
JPS5528931A JPS5528931A (en) 1980-02-29
JPS6141342B2 true JPS6141342B2 (en) 1986-09-13

Family

ID=14305356

Family Applications (1)

Application Number Title Priority Date Filing Date
JP10161778A Granted JPS5528931A (en) 1978-08-21 1978-08-21 Preparation of benzophenoneazine

Country Status (1)

Country Link
JP (1) JPS5528931A (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS6059900B2 (en) * 1982-08-25 1985-12-27 三菱瓦斯化学株式会社 Process for producing benzophenoneazines

Also Published As

Publication number Publication date
JPS5528931A (en) 1980-02-29

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