JP2003113144A - Method for producing alkylaryl carbonate - Google Patents
Method for producing alkylaryl carbonateInfo
- Publication number
- JP2003113144A JP2003113144A JP2001309852A JP2001309852A JP2003113144A JP 2003113144 A JP2003113144 A JP 2003113144A JP 2001309852 A JP2001309852 A JP 2001309852A JP 2001309852 A JP2001309852 A JP 2001309852A JP 2003113144 A JP2003113144 A JP 2003113144A
- Authority
- JP
- Japan
- Prior art keywords
- reactor
- carbonate
- reaction
- column
- producing
- 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.)
- Pending
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
- Y02P20/10—Process efficiency
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ジアルキルカーボ
ネートと芳香族ヒドロキシ化合物とのエステル交換反応
により、アルキルアリールカーボネートを製造する方法
に関するものである。TECHNICAL FIELD The present invention relates to a method for producing an alkylaryl carbonate by a transesterification reaction between a dialkyl carbonate and an aromatic hydroxy compound.
【０００２】[0002]
【従来の技術】ジアルキルカーボネートと芳香族ヒドロ
キシ化合物とを、触媒の存在下にエステル交換反応させ
て、アルキルアリールカーボネートを製造することは公
知である。得られたアルキルアリールカーボネートは、
次いで不均化反応させてジアリールカーボネートにす
る。It is known to produce an alkylaryl carbonate by subjecting a dialkyl carbonate and an aromatic hydroxy compound to a transesterification reaction in the presence of a catalyst. The obtained alkyl aryl carbonate is
Then, a disproportionation reaction is performed to obtain a diaryl carbonate.
【０００３】ジアルキルカーボネートと芳香族ヒドロキ
シ化合物とのエステル交換反応は平衡反応であり、しか
も平衡はジアルキルカーボネート側に大きく偏ってお
り、かつ反応速度は一般に遅いので、このエステル交換
反応によりアルキルアリールカーボネートを効率よく製
造するため、触媒及びプロセスの双方について多くの検
討がなされている。このエステル交換反応でアルキルア
リールカーボネートの生成を促進する一つの方法は、特
開平６−１５７４１０号公報に記載されているように、
反応器に蒸留塔を付設し、反応器の気相部から抜出した
ガスをこの蒸留塔に導入して蒸留し、反応で副生したア
ルキルアルコールを蒸留塔の塔頂から系外に除去し、塔
底から流出するジアルキルカーボネートは反応器に戻し
て、反応器内のアルキルアルコールの濃度を低く保つこ
とである。The transesterification reaction between a dialkyl carbonate and an aromatic hydroxy compound is an equilibrium reaction, and the equilibrium is largely biased to the dialkyl carbonate side, and the reaction rate is generally slow. Many studies have been conducted on both the catalyst and the process for efficient production. One method for promoting the production of alkylaryl carbonate by this transesterification reaction is as described in JP-A-6-157410.
Attaching a distillation column to the reactor, the gas extracted from the gas phase part of the reactor is introduced into this distillation column for distillation, and the alkyl alcohol by-produced in the reaction is removed from the top of the distillation column to the outside of the system, The dialkyl carbonate flowing out from the bottom of the column is returned to the reactor to keep the concentration of alkyl alcohol in the reactor low.
【０００４】[0004]
【発明が解決しようとする課題】特開平６−１５７４１
０号公報に記載されている、付設されている蒸留塔によ
り副生したアルキルアルコールを系外に除去しながら行
う方法は、優れた方法ではあるが、工業的に実施するに
は、反応系内の副生アルキルアルコール濃度を更に低下
させるのが望ましい。また、当然のことながら、蒸留操
作はできるだけ経済的に有利になるように行うのが望ま
しい。本発明はこのような要望に応えようとするもので
ある。[Patent Document 1] Japanese Unexamined Patent Publication No. 6-15741
Although the method described in JP-A No. 0-096, which is carried out while removing the by-produced alkyl alcohol by an attached distillation column from the outside of the system is an excellent method, it can be carried out industrially in the reaction system. It is desirable to further reduce the concentration of by-product alkyl alcohol. In addition, as a matter of course, it is desirable to carry out the distillation operation so as to be economically advantageous as much as possible. The present invention seeks to meet these needs.
【０００５】[0005]
【課題を解決するための手段】本発明によれば、反応器
に触媒、ジアルキルカーボネート及び芳香族ヒドロキシ
化合物を連続的に供給して、加圧下、かつ１２０℃以上
の温度でエステル交換反応させてアルキルアリールカー
ボネートを生成させるに際し、反応器の気相部からジア
ルキルカーボネート及び副生したアルキルアルコールを
含むガスを抜出し、これを熱交換器で熱交換させたのち
塔底部にリボイラーを備えた蒸留塔の中段に供給して蒸
留し、蒸留塔の塔頂からアルキルアルコールを留出さ
せ、塔底からジアルキルカーボネートを流出させて反応
器に戻すことにより、効率よくかつ経済的にも有利に、
アルキルアリールカーボネートを製造することができ
る。According to the present invention, a catalyst, a dialkyl carbonate and an aromatic hydroxy compound are continuously supplied to a reactor to carry out a transesterification reaction under pressure and at a temperature of 120 ° C. or higher. Upon producing the alkylaryl carbonate, a gas containing a dialkyl carbonate and a by-produced alkyl alcohol was withdrawn from the gas phase of the reactor, the heat of this gas was exchanged with a heat exchanger, and then the distillation column equipped with a reboiler at the bottom of the column was used. By supplying to the middle stage and distilling, distilling the alkyl alcohol from the top of the distillation column, and flowing out the dialkyl carbonate from the bottom of the column and returning it to the reactor, efficiently and economically advantageous,
Alkyl aryl carbonates can be produced.
【０００６】[0006]
【発明の実施の形態】本発明においては、反応に供する
ジアルキルカーボネート、芳香族ヒドロキシ化合物及び
両者を反応させてアルキルアリールカーボネートを生成
させるエステル交換触媒としては、従来からこの反応に
用い得ることが知られている任意のものを用いることが
できる。周知のように、このエステル交換反応によるア
ルキルアリールカーボネートの製造方法の最も重要な適
用対象は、ジメチルカーボネートとフェノールからのメ
チルフェニルカーボネートの製造なので、以下にこれに
ついて説明するが、他のアルキルアリールカーボネート
の製造にも同様に適用できる。BEST MODE FOR CARRYING OUT THE INVENTION In the present invention, it is known that a dialkyl carbonate, an aromatic hydroxy compound to be subjected to the reaction and an ester exchange catalyst for reacting the two with each other to produce an alkylaryl carbonate can be conventionally used in this reaction. Any of the above can be used. As is well known, the most important application target of the method for producing an alkylaryl carbonate by this transesterification reaction is the production of methylphenyl carbonate from dimethyl carbonate and phenol, which will be explained below. Can be similarly applied to the production of.
【０００７】このエステル交換反応は、反応器にジメチ
ルカーボネート、フェノール及び触媒を連続的に供給し
て反応させ、反応器から生成したメチルフェニルカーボ
ネート、ジフェニルカーボネート及び未反応のジメチル
カーボネートから成る反応液を連続的に抜き出すことに
より行われる。反応器としては攪拌槽、好ましくは複数
個の撹拌槽を直列に接続した連続式撹拌槽を用いる。最
も好ましいのは、特開平８−１８８５５８号公報に記載
されている、液相部が複数の反応区画に分割されてお
り、反応液が各区画を順次経て反応器から流出するよう
になっている反応器である。この反応器では、反応区画
の数が多いほど反応液の流れはプラグフローに近づく
が、反応器が高価となるので、反応区画数は２〜１５程
度が好ましい。また、各反応区画内では反応液を撹拌し
て反応を促進するのが好ましい。反応液の撹拌は、反応
区画から次の反応区画への反応液の移動や、蒸発に伴う
気泡の発生などに伴う自然撹拌で十分な場合もあるが、
一般には攪拌機による撹拌や、ポンプで強制循環するこ
とによる撹拌、更にはガスや蒸気などを吹込むことによ
る撹拌などの、人為的撹拌を行うのが好ましい。また、
反応器には加熱装置を設けるが、加熱装置は各反応区画
に個別に設けてもよく、また複数の反応区画毎、場合に
よっては反応器全体に共通する加熱装置を設けてもよ
い。反応器の気相部は、通常は分割せずに各反応区画に
共通のものとし、各反応区画から発生したガスが共通の
気相部を経て抜出されるようにする。In this transesterification reaction, dimethyl carbonate, phenol and a catalyst are continuously supplied to the reactor to cause reaction, and a reaction liquid composed of methylphenyl carbonate, diphenyl carbonate and unreacted dimethyl carbonate produced from the reactor is reacted. It is carried out by continuously extracting. As the reactor, a stirring tank, preferably a continuous stirring tank in which a plurality of stirring tanks are connected in series is used. Most preferably, the liquid phase portion described in JP-A-8-188558 is divided into a plurality of reaction compartments, and the reaction solution flows out of the reactor through each compartment in sequence. It is a reactor. In this reactor, the larger the number of reaction compartments, the closer the flow of the reaction liquid becomes to the plug flow, but since the reactor becomes expensive, the number of reaction compartments is preferably about 2 to 15. Further, it is preferable to stir the reaction solution in each reaction section to promote the reaction. In some cases, the stirring of the reaction solution may be performed by moving the reaction solution from one reaction section to the next reaction section or by spontaneous stirring accompanied by the generation of bubbles due to evaporation,
Generally, it is preferable to carry out artificial stirring such as stirring by a stirrer, forced circulation by a pump, and further stirring by blowing gas or steam. Also,
Although the reactor is provided with a heating device, the heating device may be provided individually in each reaction section, or may be provided for each of a plurality of reaction sections, and in some cases, a heating apparatus common to the entire reactor. The gas phase part of the reactor is not divided but is common to each reaction section, and the gas generated from each reaction section is extracted through the common gas phase section.
【０００８】反応器へのジメチルカーボネート及びフェ
ノールの供給比率は、通常はフェノール１モルに対しジ
メチルカーボネート０．５〜２０モルである。本発明で
は１２０℃以上、好ましくは１５０℃以上の温度でエス
テル交換反応を行わせる。反応温度がこれよりも低い
と、反応速度が小さく、かつ反応器の気相部から抜出し
たガスから熱交換器での熱交換により水蒸気を発生させ
ても、価値の比較的低い低温の水蒸気しか発生させるこ
とができない。本発明の利点を十分に発揮させるには１
８０℃以上で反応させるのが好ましい。反応温度が高い
ほど反応はすみやかに進行するが、他方においてメタノ
ール及びフェノールの脱水反応によるエーテル化合物の
生成などの副反応が増大するので、反応温度の上限は３
００℃、特に２５０℃以下とするのが好ましい。反応圧
力はジメチルカーボネートが液相に維持されるように設
定すればよい。The feeding ratio of dimethyl carbonate and phenol to the reactor is usually 0.5 to 20 mol of dimethyl carbonate per mol of phenol. In the present invention, the transesterification reaction is carried out at a temperature of 120 ° C. or higher, preferably 150 ° C. or higher. If the reaction temperature is lower than this, the reaction rate is low, and even if steam is generated from the gas extracted from the gas phase part of the reactor by heat exchange in the heat exchanger, only low-temperature steam of relatively low value is obtained. Cannot be generated. To make full use of the advantages of the present invention, 1
It is preferable to react at 80 ° C. or higher. The higher the reaction temperature, the faster the reaction proceeds, but on the other hand, the side reaction such as the formation of an ether compound due to the dehydration reaction of methanol and phenol increases, so the upper limit of the reaction temperature is 3
It is preferably set to 00 ° C, particularly 250 ° C or lower. The reaction pressure may be set so that dimethyl carbonate is maintained in the liquid phase.
【０００９】本発明では反応器の気相部からガスを抜出
し、これを先ず熱交換器に導入して、その保有している
エネルギーを回収する。熱交換器としては常用の任意の
型式のものを用いることができる。反応器の気相部から
抜出したガスの主成分は、ジメチルカーボネートとメタ
ノールである。特に本発明のように反応液中のメタノー
ル濃度を低く保ってエステル交換反応を促進させる場合
には、気相部から抜出したガスの大部分はジメチルカー
ボネートである。メタノールの沸点は６４．７℃、ジメ
チルカーボネートの沸点は９１〜９２℃なので、熱交換
器では少なくとも、ガスの重量組成の大部分を占め、か
つ沸点の高いジメチルカーボネートを凝縮させることが
必要であり、かつ、これによりガスの保有する熱エネル
ギーの大部分を回収することができる。In the present invention, the gas is extracted from the gas phase portion of the reactor and is first introduced into the heat exchanger to recover the energy stored therein. As the heat exchanger, any conventional type can be used. The main components of the gas extracted from the gas phase part of the reactor are dimethyl carbonate and methanol. Particularly when the transesterification reaction is promoted by keeping the methanol concentration in the reaction solution low as in the present invention, most of the gas extracted from the gas phase is dimethyl carbonate. Since the boiling point of methanol is 64.7 ° C. and the boiling point of dimethyl carbonate is 91 to 92 ° C., it is necessary to condense at least most of the weight composition of the gas in the heat exchanger and dimethyl carbonate having a high boiling point. And, by doing so, most of the thermal energy possessed by the gas can be recovered.
【００１０】反応器の気相部から抜出したガスは、上述
の熱交換を行ったのち、リボイラーを備えた蒸留塔の中
段に供給して蒸留し、メタノールを塔頂から留出させ、
ジメチルカーボネートを塔底から流出させて反応器に戻
す。蒸留塔は反応器から蒸留塔までの間の不可避的圧力
損失による圧力低下は別にして、反応器の圧力と実質的
に同じ圧力で操作するのが好ましく、こうすることによ
り全体のエネルギー効率を高めることができる。すなわ
ち反応器から蒸留塔までの間では、減圧操作などを行う
ことなく、極力圧力低下を防ぐようにすべきである。蒸
留塔は塔底から流出するジメチルカーボネート中のメタ
ノール量をできるだけ低減するように操作すべきであ
り、通常はメタノール濃度が０．５重量％以下となるよ
うに操作する。メタノール濃度が０．２重量％以下、特
に０．１重量％以下となるように操作するのが好まし
く、蒸留塔への供給位置、すなわち蒸留塔の濃縮部と回
収部との段数の配分も、この点を考慮して行うべきであ
る。通常は回収部、濃縮部とも段数は５〜３０段、特に
８〜２５段とするのが好ましい。回収部の段数が５段未
満では塔底液中のメタノール量を低減させるために還流
比を高くすることが必要となり、リボイラーで供給すべ
き熱量が増加して不利である。逆に回収部の段数を３０
段より多くすることは設備費が嵩み、総合的にみて有利
とはいえない。蒸留塔の操作条件は、塔底から流出する
ジメチルカーボネート中のメタノール量を所定量以下に
することを前提に、塔頂から留出するメタノール中のジ
メチルカーボネートの許容量を考慮して適宜決定すれば
よい。なお、圧力は前述のように反応器と実質的に同じ
とするのが好ましい。圧力を低下させると分離効率は向
上するが回収熱量が減少する。温度は圧力に依存するが
１００〜３００℃、好ましくは１５０〜２５０℃であ
る。The gas withdrawn from the gas phase of the reactor is subjected to the above-mentioned heat exchange and then fed to the middle stage of the distillation column equipped with a reboiler for distillation to distill methanol from the top of the column,
Dimethyl carbonate is drained from the bottom of the column and returned to the reactor. The distillation column is preferably operated at a pressure substantially the same as the pressure of the reactor, apart from the pressure drop due to the unavoidable pressure loss between the reactor and the distillation column, which improves the overall energy efficiency. Can be increased. That is, the pressure drop should be prevented as much as possible between the reactor and the distillation column without depressurizing operation. The distillation column should be operated so that the amount of methanol in the dimethyl carbonate flowing out from the bottom of the distillation column is reduced as much as possible, and usually the concentration of methanol is 0.5% by weight or less. It is preferable to operate so that the concentration of methanol is 0.2% by weight or less, particularly 0.1% by weight or less, and the feeding position to the distillation column, that is, the distribution of the number of stages between the concentration section and the recovery section of the distillation column, This should be taken into consideration. Usually, the number of stages in both the recovery section and the concentration section is preferably 5 to 30, particularly 8 to 25. If the number of plates in the recovery section is less than 5, it is necessary to increase the reflux ratio in order to reduce the amount of methanol in the bottom liquid, which is disadvantageous because the amount of heat to be supplied by the reboiler increases. Conversely, the number of stages in the collection section is 30
If the number is larger than the number of steps, the equipment cost increases, and it cannot be said to be advantageous from the overall viewpoint. The operating conditions of the distillation column are appropriately determined in consideration of the allowable amount of dimethyl carbonate in methanol distilled from the top of the column, on the assumption that the amount of methanol in the dimethyl carbonate flowing out of the column bottom is set to a predetermined amount or less. Good. The pressure is preferably substantially the same as that of the reactor as described above. When the pressure is lowered, the separation efficiency is improved but the amount of heat recovered is reduced. The temperature depends on the pressure, but is 100 to 300 ° C, preferably 150 to 250 ° C.
【００１１】本発明では、特開平６−１５７４１０号公
報に記載の方法とは異なり、反応器の気相部から抜出し
たガスを熱交換器で凝縮させて、その保有する潜熱を回
収したのち蒸留塔に供給するが、熱交換器での凝縮温度
は、蒸留塔の塔頂の凝縮器での凝縮温度よりも高温なの
で、塔頂の凝縮器で熱回収する場合に比してより高温、
すなわちより利用価値の大きい水蒸気を発生させること
ができる。また塔頂の凝縮器では凝縮温度が低くて有利
に熱回収が行えないような場合でも、利用価値の大きい
水蒸気を発生させることができる。また蒸留塔も特開平
６−１５７４１０号公報に記載のものとは異なり、塔底
にリボイラーを備え、かつ濃縮部と回収部の双方を有す
るものを用いるので、塔底から流出するジメチルカーボ
ネート中のメタノール濃度を大きく低下させることがで
きる。In the present invention, unlike the method described in JP-A-6-157410, the gas withdrawn from the gas phase of the reactor is condensed in a heat exchanger, the latent heat retained therein is recovered, and then distilled. Although it is supplied to the column, the condensation temperature in the heat exchanger is higher than the condensation temperature in the condenser at the top of the distillation column, so it is higher than in the case where heat is recovered in the condenser at the top,
That is, it is possible to generate steam having a greater utility value. Further, even when the condenser at the top of the tower has a low condensation temperature and cannot effectively recover heat, it is possible to generate steam having a high utility value. Further, unlike the one described in JP-A-6-157410, the distillation column is also equipped with a reboiler at the bottom and has both a concentrating section and a recovering section. The methanol concentration can be greatly reduced.
【００１２】反応器流出ガスから本発明方法により熱交
換器で熱回収したのち蒸留を行った場合と、特開平６−
１５７４１０号公報に記載の方法のように熱回収を行う
ことなく蒸留を行った場合との対比の１例を示すと次の
とおりである。
反応器から流出するガス；
組成：ジメチルカーボネート９７重量％、メタノール
１．５重量％、フェノール１．５重量％
温度：２０４℃
圧力：１２ｋｇ／ｃｍ2 Ｇ
蒸留塔；
段数：２０段
塔頂留出量：供給量の２．２％
塔頂温度：１４０℃（温度が低いので凝縮器では熱回収
を行わない）
本発明方法；ガスを熱交換器で全凝縮させて水蒸気を発
生させ、凝縮液を蒸留塔の上から９段目に供給して蒸留
する。蒸留は塔底流出液中のメタノールが０．１重量％
となるように還流比５で行う。In the case where the heat is recovered from the gas discharged from the reactor by the method of the present invention by the heat exchanger and then the distillation is carried out, the method described in JP-A-6-
An example of comparison with the case where distillation is performed without heat recovery as in the method described in Japanese Patent No. 157410 is as follows. Gas flowing out from reactor; Composition: 97% by weight of dimethyl carbonate, 1.5% by weight of methanol, 1.5% by weight of phenol Temperature: 204 ° C. Pressure: 12 kg / cm 2 G Distillation column; Number of plates: 20-stage overhead distillation Amount: 2.2% of the supply amount Column top temperature: 140 ° C. (heat is not recovered in the condenser because the temperature is low) The method of the present invention; The gas is totally condensed in the heat exchanger to generate steam, and the condensate is generated. Is fed to the ninth stage from the top of the distillation column and distilled. Distillation was performed with 0.1% by weight of methanol in the bottom effluent.
At a reflux ratio of 5 so that
【００１３】熱交換器での回収熱量；フィード１ｋｇ当
り９４．５ｋｃａｌ
熱交換器での発生水蒸気；１３ｋｇ／ｃｍ2
蒸留塔リボイラーへの供給熱量：フィード１ｋｇ当り４
０ｋｃａｌ
回収熱量：フィード１ｋｇ当り５４．５ｋｃａｌ
塔頂組成：ジメチルカーボネート４０重量％、メタノー
ル６０重量％
塔底組成：メタノール０．１重量％、その他はジメチル
カーボネートとフェノール
特開平６−１５７４１０号公報に記載の方法；ガスをそ
のまま蒸留塔の塔底に供給して蒸留する。供給熱量が多
いため還流比は結果的に２５となる。
塔頂組成：ジメチルカーボネート５３重量％、メタノー
ル４７重量％
塔底組成：メタノール０．４重量％、その他はジメチル
カーボネートとフェノールHeat recovered in heat exchanger: 94.5 kcal per kg of feed Steam generated in heat exchanger: 13 kg / cm 2 Heat supplied to distillation column reboiler: 4 per kg of feed
0 kcal Recovery heat amount: 54.5 kcal per 1 kg of feed Column top composition: 40 wt% dimethyl carbonate, 60 wt% methanol Bottom composition: 0.1 wt% methanol, Others are dimethyl carbonate and phenol Described in JP-A-6-157410 Method: The gas is directly supplied to the bottom of the distillation column for distillation. Since the amount of heat supplied is large, the reflux ratio eventually becomes 25. Column top composition: 53% by weight of dimethyl carbonate, 47% by weight of methanol Column bottom composition: 0.4% by weight of methanol, others are dimethyl carbonate and phenol
【００１４】すなわち、本発明方法によれば、反応器流
出ガスから５４．５ｋｃａｌ／ｋｇの熱エネルギーを高
圧水蒸気として回収できるので、特開平６−１５７４１
０号公報記載の方法に比して、有利である。また、蒸留
塔への供給を最適位置で行えるので、塔底液中のメタノ
ール量を特開平６−１５７４１０号公報記載の方法に比
して１／４に低減でき、かつ塔頂から留出するジメチル
カーボネート量も低減させることができる。That is, according to the method of the present invention, since thermal energy of 54.5 kcal / kg can be recovered as high-pressure steam from the gas discharged from the reactor, JP-A-6-15741.
It is advantageous as compared with the method described in JP-A-0. Further, since the supply to the distillation column can be carried out at the optimum position, the amount of methanol in the bottom liquid can be reduced to 1/4 as compared with the method described in JP-A-6-157410, and distillation from the top of the column is possible. The amount of dimethyl carbonate can also be reduced.
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Claims (5)
ト及び芳香族ヒドロキシ化合物を連続的に供給して、加
圧下かつ１２０℃以上の温度でエステル交換反応させて
アルキルアリールカーボネートを生成させるに際し、反
応器の気相部からジアルキルカーボネート及び副生した
アルキルアルコールを含むガスを抜出し、これを熱交換
器で熱交換させたのち塔底部にリボイラーを備えた蒸留
塔の中段に供給して蒸留し、塔頂からアルキルアルコー
ルを留出させ、塔底からジアルキルカーボネートを流出
させて反応器に循環することを特徴とするアルキルアリ
ールカーボネートの製造方法。1. When a catalyst, a dialkyl carbonate and an aromatic hydroxy compound are continuously supplied to a reactor and a transesterification reaction is carried out under pressure and at a temperature of 120 ° C. or more to produce an alkyl aryl carbonate, the reactor A gas containing a dialkyl carbonate and a by-produced alkyl alcohol is withdrawn from the gas phase part of the product, heat-exchanged with a heat exchanger, and then supplied to the middle stage of a distillation column equipped with a reboiler at the bottom part of the column for distillation and distillation. A process for producing an alkylaryl carbonate, which comprises distilling alkyl alcohol from the column, distilling the dialkyl carbonate from the bottom of the column, and circulating the dialkyl carbonate in the reactor.
ボネートであり、ヒドロキシ芳香族化合物がフェノール
であることを特徴とする請求項１記載のアルキルアリー
ルカーボネートの製造方法。2. The method for producing an alkylaryl carbonate according to claim 1, wherein the dialkyl carbonate is dimethyl carbonate and the hydroxyaromatic compound is phenol.
する請求項１又は２記載のアルキルアリールカーボネー
トの製造方法。3. The method for producing an alkylaryl carbonate according to claim 1, wherein the reaction is carried out at 150 ° C. or higher.
に分割されており、反応液が各区画を順次経て反応器か
ら流出する構造のものを用いることを特徴とする請求項
１ないし３のいずれかに記載のアルキルアリールカーボ
ネートの製造方法。4. A reactor having a structure in which a liquid phase portion is divided into a plurality of reaction compartments, and a reaction liquid flows out of the reactor through each compartment in sequence is used. 4. The method for producing an alkylaryl carbonate according to any one of 3 above.
作することを特徴とする請求項１ないし４のいずれかに
記載のアルキルアリールカーボネートの製造方法。5. The method for producing an alkylaryl carbonate according to claim 1, wherein the distillation column is operated at substantially the same pressure as the reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001309852A JP2003113144A (en) | 2001-10-05 | 2001-10-05 | Method for producing alkylaryl carbonate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001309852A JP2003113144A (en) | 2001-10-05 | 2001-10-05 | Method for producing alkylaryl carbonate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2003113144A true JP2003113144A (en) | 2003-04-18 |
Family
ID=19128931
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2001309852A Pending JP2003113144A (en) | 2001-10-05 | 2001-10-05 | Method for producing alkylaryl carbonate |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2003113144A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7777067B2 (en) | 2004-07-13 | 2010-08-17 | Asahi Kasei Chemicals Corporation | Industrial process for production of an aromatic carbonate |
| US7812189B2 (en) | 2004-08-25 | 2010-10-12 | Asahi Kasei Chemicals Corporation | Industrial process for production of high-purity diphenyl carbonate |
| US7884251B2 (en) | 2004-09-17 | 2011-02-08 | Asahi Kasei Chemicals Corporation | Industrial process for separating out by-produced alcohols |
| JP2011105717A (en) * | 2009-11-14 | 2011-06-02 | Bayer Materialscience Ag | Method for purifying dialkyl carbonate |
| US8044167B2 (en) | 2004-10-14 | 2011-10-25 | Asahi Kasei Chemicals Corporation | Process for production of high-purity diaryl carbonate |
| JP2015040187A (en) * | 2013-08-21 | 2015-03-02 | 三菱瓦斯化学株式会社 | Continuous manufacturing method of diaryl carbonate |
-
2001
- 2001-10-05 JP JP2001309852A patent/JP2003113144A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7777067B2 (en) | 2004-07-13 | 2010-08-17 | Asahi Kasei Chemicals Corporation | Industrial process for production of an aromatic carbonate |
| US7812189B2 (en) | 2004-08-25 | 2010-10-12 | Asahi Kasei Chemicals Corporation | Industrial process for production of high-purity diphenyl carbonate |
| US7884251B2 (en) | 2004-09-17 | 2011-02-08 | Asahi Kasei Chemicals Corporation | Industrial process for separating out by-produced alcohols |
| US8044167B2 (en) | 2004-10-14 | 2011-10-25 | Asahi Kasei Chemicals Corporation | Process for production of high-purity diaryl carbonate |
| US8044226B2 (en) | 2004-10-14 | 2011-10-25 | Asahi Kasei Chemicals Corporation | Process for production of high-purity diaryl carbonate |
| JP2011105717A (en) * | 2009-11-14 | 2011-06-02 | Bayer Materialscience Ag | Method for purifying dialkyl carbonate |
| JP2015040187A (en) * | 2013-08-21 | 2015-03-02 | 三菱瓦斯化学株式会社 | Continuous manufacturing method of diaryl carbonate |
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