JPH05213816A - Production of aromatic carboxylic acid - Google Patents
Production of aromatic carboxylic acidInfo
- Publication number
- JPH05213816A JPH05213816A JP4021280A JP2128092A JPH05213816A JP H05213816 A JPH05213816 A JP H05213816A JP 4021280 A JP4021280 A JP 4021280A JP 2128092 A JP2128092 A JP 2128092A JP H05213816 A JPH05213816 A JP H05213816A
- Authority
- JP
- Japan
- Prior art keywords
- pressure steam
- carboxylic acid
- turbine
- aromatic carboxylic
- steam
- 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
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
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明はアルキル芳香族炭化水素
を酸化して芳香族カルボン酸を製造する方法に係り、特
に、製造工程における廃熱を有効利用して、エネルギー
効率の向上、エネルギーコストの低減を図る方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for producing an aromatic carboxylic acid by oxidizing an alkyl aromatic hydrocarbon, and more particularly, to effectively utilize waste heat in the production process to improve energy efficiency and energy cost. To reduce the amount of
【０００２】[0002]
【従来の技術】従来、酸化反応器内にて、アルキル芳香
族炭化水素、例えばパラキシレンを低級脂肪族カルボン
酸溶媒中において分子状酸素含有ガスにより酸化して芳
香族カルボン酸、例えばテレフタル酸を製造する方法は
よく知られている。2. Description of the Related Art Conventionally, an aromatic aromatic carboxylic acid such as terephthalic acid is oxidized by oxidizing an alkyl aromatic hydrocarbon such as paraxylene with a molecular oxygen-containing gas in a lower aliphatic carboxylic acid solvent in an oxidation reactor. The method of manufacture is well known.
【０００３】この方法において、酸化反応器から排出さ
れる高温高圧の反応排ガスには、溶媒蒸気及び水蒸気が
多量に含有されている。また、反応溶媒として用いられ
る低級脂肪族カルボン酸は、通常、生成物を分離後、蒸
留により回収されるが、この蒸留回収のための脱水塔か
らも多量の常圧ガスが放出される。In this method, the high temperature and high pressure reaction exhaust gas discharged from the oxidation reactor contains a large amount of solvent vapor and water vapor. The lower aliphatic carboxylic acid used as a reaction solvent is usually recovered by distillation after separating the product, but a large amount of atmospheric gas is also released from the dehydration column for this distillation recovery.
【０００４】従来、酸化反応器から排出される反応排ガ
スは蒸気発生器へ通して蒸気発生の熱源とし、次いで凝
縮器、吸収塔を経て、大気中に放出するか、更にこれを
ガスタービン等の動力として利用していた。Conventionally, the reaction exhaust gas discharged from the oxidation reactor is passed through a steam generator and used as a heat source for steam generation, and then is discharged into the atmosphere through a condenser and an absorption tower, or is further discharged to a gas turbine or the like. It was used as power.
【０００５】また、反応排ガスの廃熱をより効率良く利
用するために、反応排ガスを直接、ガスタービン等に供
給して廃熱利用する方法も知られている（特開昭５６−
４０６３６）。Further, in order to more efficiently use the waste heat of the reaction exhaust gas, a method of supplying the reaction exhaust gas directly to a gas turbine or the like and utilizing the waste heat is also known (Japanese Patent Laid-Open No. 56-56-56).
40636).
【０００６】[0006]
【発明が解決しようとする課題】従来、一般に行なわれ
ている反応排ガスを蒸気発生器へ導いて蒸気を発生させ
る方法では、蒸気発生器で発生させた蒸気は、通常、蒸
気を必要とする工場の各場所に分散供給し、余剰分につ
いては大気中に放出しており、蒸気の効率的利用という
点においては必ずしも充分ではなかった。In the conventional method of introducing reaction exhaust gas to a steam generator to generate steam, the steam generated by the steam generator is usually a factory that requires steam. It was dispersed and supplied to each place, and the surplus was released to the atmosphere, which was not always sufficient in terms of efficient use of steam.
【０００７】また、特開昭５６−４０６３６記載の方法
では、実用上は、装置類を全てチタン等の耐食材料で構
成する必要があり、現実的に長期にわたり安定した廃熱
回収を行なうためには適当ではない。Further, in the method described in Japanese Patent Laid-Open No. 56-40636, it is necessary in practice to construct all the devices with a corrosion-resistant material such as titanium, and in order to recover waste heat stably over a long period of time in practice. Is not appropriate.
【０００８】本発明は上記従来の問題点を解決し、アル
キル芳香族炭化水素を酸化して芳香族カルボン酸を製造
する工程において、廃熱をより一層効率的に有効利用し
て、エネルギー効率の向上、エネルギーコストの低減を
図る芳香族カルボン酸の製造方法を提供することを目的
とする。The present invention solves the above-mentioned conventional problems, and in the process of producing an aromatic carboxylic acid by oxidizing an alkylaromatic hydrocarbon, waste heat is used more efficiently and energy efficiency is improved. It is an object of the present invention to provide a method for producing an aromatic carboxylic acid which improves the cost and reduces the energy cost.
【０００９】[0009]
【課題を解決するための手段】請求項１の芳香族カルボ
ン酸の製造方法は、酸化反応器内で、アルキル芳香族炭
化水素を低級脂肪族カルボン酸溶媒中で分子状酸素含有
ガスにより酸化して芳香族カルボン酸を製造する方法に
おいて、酸化反応器からの排ガスを高圧蒸気発生器に通
した後、ガスタービンに供給すると共に、該高圧蒸気発
生器で発生した高圧蒸気を蒸気タービンに供給し、該ガ
スタービンと該蒸気タービンとを稼動させて得た出力で
空気圧縮器を稼動させ、該空気圧縮器からの圧縮空気を
前記分子状酸素含有ガスとして使用することを特徴とす
る。A method for producing an aromatic carboxylic acid according to claim 1 oxidizes an alkyl aromatic hydrocarbon in a lower aliphatic carboxylic acid solvent with a molecular oxygen-containing gas in an oxidation reactor. In the method for producing an aromatic carboxylic acid, the exhaust gas from the oxidation reactor is passed through a high-pressure steam generator and then supplied to a gas turbine, and the high-pressure steam generated by the high-pressure steam generator is supplied to the steam turbine. An air compressor is operated with an output obtained by operating the gas turbine and the steam turbine, and compressed air from the air compressor is used as the molecular oxygen-containing gas.
【００１０】請求項２の芳香族カルボン酸の製造方法
は、請求項１の方法において酸化反応生成液から芳香族
カルボン酸を除去した後、脱水塔にて低級脂肪族カルボ
ン酸溶媒を回収するにあたり、該脱水塔から留去される
蒸気を低圧蒸気発生器を経て、系外に排出すると共に、
該低圧蒸気発生器で発生した低圧蒸気を前記高圧蒸気と
共に前記蒸気タービンに供給することを特徴とする。In the method for producing an aromatic carboxylic acid according to claim 2, the aromatic carboxylic acid is removed from the oxidation reaction product liquid in the method according to claim 1, and the lower aliphatic carboxylic acid solvent is recovered in a dehydration tower. , The steam distilled from the dehydration tower is discharged to the outside of the system through a low pressure steam generator,
The low-pressure steam generated by the low-pressure steam generator is supplied to the steam turbine together with the high-pressure steam.
【００１１】なお、本発明において、高圧蒸気とは常圧
よりもはるかに高い、例えば１．５ａｔｍ以上の蒸気を
指し、低圧蒸気とは常圧よりも低い、例えば０．９ａｔ
ｍ以下程度の蒸気を指し、また、常圧蒸気とは１〜１．
２ａｔｍ程度の蒸気を指す。In the present invention, the high-pressure steam means a steam much higher than the normal pressure, for example, 1.5 atm or more, and the low-pressure steam is lower than the normal pressure, for example, 0.9 atm.
m refers to steam of about m or less, and normal pressure steam is 1-1.
It means about 2 atm of steam.
【００１２】本発明で製造される芳香族カルボン酸とし
ては、テレフタル酸、イソフタル酸、フタル酸、パラト
ルイル酸、ナフタレンジカルボン酸等が例示され、各々
に対応するアルキル芳香族炭化水素が原料として使用さ
れる。Examples of the aromatic carboxylic acid produced in the present invention include terephthalic acid, isophthalic acid, phthalic acid, paratoluic acid, naphthalenedicarboxylic acid, etc., and the corresponding alkylaromatic hydrocarbons are used as raw materials. It
【００１３】また、溶媒として用いられる低級脂肪族カ
ルボン酸としては、酢酸、プロピオン酸等が挙げられる
が、通常は酢酸を用いる。Examples of the lower aliphatic carboxylic acid used as a solvent include acetic acid and propionic acid, but acetic acid is usually used.
【００１４】本発明の芳香族カルボン酸の製造方法によ
り、テレフタル酸を製造するには、例えばパラキシレン
を酢酸溶媒中、酢酸コバルト、酢酸マンガン及び臭素化
合物から成る触媒の存在下、分子状酸素により液相酸化
する。使用される臭素化合物としては臭化水素、臭化ナ
トリウム等が挙げられる。触媒の添加量としては、酢酸
コバルト、酢酸マンガンは、溶媒に対する各々の金属量
として、通常１００〜１０００ｐｐｍ、また、臭素化合
物は、溶媒に対する臭素量として、通常３００〜３００
０ｐｐｍである。To produce terephthalic acid by the method for producing an aromatic carboxylic acid of the present invention, for example, paraxylene is treated with molecular oxygen in the presence of a catalyst consisting of cobalt acetate, manganese acetate and bromine compound in an acetic acid solvent. Liquid phase oxidation. Examples of the bromine compound used include hydrogen bromide and sodium bromide. As the amount of the catalyst added, cobalt acetate and manganese acetate are usually 100 to 1000 ppm as the amount of each metal in the solvent, and the bromine compound is usually 300 to 300 as the amount of bromine in the solvent.
It is 0 ppm.
【００１５】溶媒である酢酸は、パラキシレン１重量部
に対し、通常１〜１０重量部用いられる。また、酢酸中
には約３０重量％までの水分を含んでいて良い。反応条
件としては、通常１５０〜２３０℃の温度、２〜１００
気圧の圧力で行ない、分子状酸素含有ガスとしては、通
常、空気が使用される。Acetic acid as a solvent is usually used in an amount of 1 to 10 parts by weight per 1 part by weight of paraxylene. Further, acetic acid may contain up to about 30% by weight of water. The reaction conditions are usually 150 to 230 ° C. and 2 to 100 ° C.
Air is used as the molecular oxygen-containing gas under atmospheric pressure.
【００１６】酸化反応によって生成したテレフタル酸
は、液状の酸化反応生成物から、通常、晶析又は遠心分
離等により分離される。テレフタル酸を分離した後の反
応母液の主成分は酢酸であるので、反応母液の一部はそ
のまま反応系に戻して再使用することができるが、通
常、大部分又は全量についてたき上げ処理を行ない、酢
酸溶媒、水分を蒸発分離する。たき上げられた含水酢酸
は蒸留脱水塔にて水分をある程度除去した後に再使用さ
れる。The terephthalic acid produced by the oxidation reaction is usually separated from the liquid oxidation reaction product by crystallization or centrifugation. Since the main component of the reaction mother liquor after separation of terephthalic acid is acetic acid, a part of the reaction mother liquor can be returned to the reaction system as it is and reused, but usually, most or all of it is lifted up. , Acetic acid solvent and water are separated by evaporation. The hydrous acetic acid thus pumped up is reused after removing some water in a distillation dehydration tower.
【００１７】[0017]
【作用】請求項１の芳香族カルボン酸の製造方法によれ
ば、芳香族カルボン酸の製造工程での廃熱により蒸気タ
ービン及びガスタービンを稼動して、その出力を空気圧
縮器（コンプレッサー）の動力源として有効利用するこ
とができる。According to the method for producing an aromatic carboxylic acid of claim 1, the steam turbine and the gas turbine are operated by the waste heat in the production process of the aromatic carboxylic acid, and the output thereof is supplied to the air compressor (compressor). It can be effectively used as a power source.
【００１８】請求項２の芳香族カルボン酸の製造方法に
よれば、低級脂肪族カルボン酸溶媒を回収する脱水塔か
ら排出される多量の蒸気の熱エネルギーをも有効利用す
ることができる。According to the method for producing an aromatic carboxylic acid of claim 2, the thermal energy of a large amount of vapor discharged from the dehydration column for recovering the lower aliphatic carboxylic acid solvent can be effectively utilized.
【００１９】[0019]
【実施例】以下図面を参照して本発明の実施例について
詳細に説明する。Embodiments of the present invention will now be described in detail with reference to the drawings.
【００２０】図１は本発明の実施に好適なテレフタル酸
製造装置の一例を示す系統図である。FIG. 1 is a system diagram showing an example of a terephthalic acid production apparatus suitable for carrying out the present invention.
【００２１】本実施例の装置は、酸化反応器１の後段
に、２機の高圧蒸気発生装置２，３を有するものであっ
て、各々の高圧蒸気発生装置２，３は熱交換器２Ａ，３
Ａ及び蒸気発生器２Ｂ，３Ｂを備える。４は蒸気タービ
ン、５はガスタービン、６は低圧蒸気発生装置、７は脱
水塔、８はミストセパレーター、９はコンプレッサー、
１０は吸収塔、１１は加熱器、１２はモーター、１３は
凝縮水ポンプ、１４は真空ポンプ、１５，１６は圧力調
節器、１７は熱交換器、１８はバルブである。また、２
１〜４１の各符号は配管を示す。The apparatus of this embodiment has two high-pressure steam generators 2 and 3 in the latter stage of the oxidation reactor 1, and each high-pressure steam generator 2 and 3 has a heat exchanger 2A, Three
A and steam generators 2B and 3B are provided. 4 is a steam turbine, 5 is a gas turbine, 6 is a low-pressure steam generator, 7 is a dehydration tower, 8 is a mist separator, 9 is a compressor,
10 is an absorption tower, 11 is a heater, 12 is a motor, 13 is a condensed water pump, 14 is a vacuum pump, 15 and 16 are pressure regulators, 17 is a heat exchanger, and 18 is a valve. Also, 2
Each reference numeral 1 to 41 indicates piping.
【００２２】本実施例において、酸化反応器から排出さ
れた排ガスは、配管２１より高圧蒸気発生装置２の熱交
換器２Ａへ、更に配管２２を経て高圧蒸気発生装置３の
熱交換器３Ａへ導入され、それぞれ配管２３，２４を循
環する循環水に熱が伝達され、蒸気発生器２Ｂ，３Ｂか
ら高圧蒸気が発生する。In this embodiment, the exhaust gas discharged from the oxidation reactor is introduced into the heat exchanger 2A of the high pressure steam generator 2 through the pipe 21 and further into the heat exchanger 3A of the high pressure steam generator 3 through the pipe 22. The heat is transferred to the circulating water circulating through the pipes 23 and 24, respectively, and high-pressure steam is generated from the steam generators 2B and 3B.
【００２３】なお、この蒸気発生器２Ｂ，３Ｂには、そ
れぞれ配管２５，２６より、後述の蒸気タービン４の排
蒸気から熱交換器１７を経て生成された凝縮水が補給水
として供給されている。The steam generators 2B and 3B are supplied with the condensed water generated from the exhaust steam of the steam turbine 4 to be described later through the heat exchanger 17 as makeup water through the pipes 25 and 26, respectively. ..
【００２４】また、熱交換器３Ａの排ガスは、配管２７
を経て、吸収塔１０に導入され、吸収塔１０内で含有さ
れる溶媒（酢酸）成分が吸収除去される。吸収塔１０内
で酢酸含有量が数百ｐｐｍ以下とされたガスは、配管２
８より加熱器１１に導入され、加熱器１１で予熱された
後、配管２９よりガスタービン５に供給される。Exhaust gas from the heat exchanger 3A is connected to the pipe 27.
After passing through, the solvent (acetic acid) component introduced into the absorption tower 10 and contained in the absorption tower 10 is absorbed and removed. The gas whose acetic acid content is set to several hundred ppm or less in the absorption tower 10 is connected to the pipe 2
It is introduced into the heater 11 from 8 and preheated in the heater 11, and then supplied to the gas turbine 5 through the pipe 29.
【００２５】前記蒸気発生器２Ｂ，３Ｂで発生した蒸気
は、各々、配管３０，３１及び配管３２より、蒸気ター
ビン４に供給される。なお、配管３０には配管３３が分
岐しており、高圧蒸気発生装置２で発生した高圧蒸気
（通常の場合、６ａｔｍ程度）の約９０％が製造工場の
蒸気が必要とされる他の系統に供給され、残る約１０％
の高圧蒸気が蒸気タービン４に供給されるように構成さ
れている。一方、高圧蒸気発生装置３で発生した高圧蒸
気（通常の場合、１．５ａｔｍ程度）は、その全量が蒸
気タービン４に供給される。また、配管３０及び配管３
１には、それぞれ圧力調節器１５，１６が設けられてお
り、高圧蒸気はその圧力が一定に調節されて蒸気タービ
ン４に供給される。The steam generated in the steam generators 2B and 3B is supplied to the steam turbine 4 through pipes 30, 31 and 32, respectively. A pipe 33 is branched to the pipe 30 so that about 90% of the high-pressure steam generated by the high-pressure steam generator 2 (usually about 6 atm) is transferred to another system where steam at the manufacturing plant is required. Supplied, about 10% remaining
Of high-pressure steam is supplied to the steam turbine 4. On the other hand, the high-pressure steam generated by the high-pressure steam generator 3 (normally about 1.5 atm) is entirely supplied to the steam turbine 4. Also, the pipe 30 and the pipe 3
1, pressure regulators 15 and 16 are provided respectively, and the high-pressure steam is supplied to the steam turbine 4 with its pressure adjusted to a constant value.
【００２６】この蒸気タービン４には、後述の低圧蒸気
発生装置６で発生した低圧蒸気（通常の場合、０．７ａ
ｔｍ程度）も、配管３４、ミストセパレーター８、バル
ブ１８を備える配管３５を経て供給されている。This steam turbine 4 has a low pressure steam (0.7a
(about tm) is also supplied through the pipe 34, the mist separator 8, and the pipe 35 including the valve 18.
【００２７】低圧蒸気発生装置６には、酸化反応器１の
反応生成液から生成したテレフタル酸を除去した後の酢
酸を主成分とする母液から酢酸を回収するための脱水塔
７で発生したほぼ常圧の蒸気（通常の場合、１．１ａｔ
ｍ程度）が配管３６より供給され、配管３７から導入さ
れる補給水と熱交換されて低圧蒸気が発生する。発生し
た低圧蒸気は、上述の如く、配管３４よりミストセパレ
ーター８、配管３５を経て蒸気タービン４に供給され
る。一方、凝縮水は、配管３８より系外へ排出される。In the low-pressure steam generator 6, almost all of the water generated in the dehydration tower 7 for recovering acetic acid from the mother liquor containing acetic acid as a main component after removing terephthalic acid generated from the reaction product liquid of the oxidation reactor 1 is generated. Atmospheric pressure steam (normally 1.1 at
m) is supplied from the pipe 36 and heat-exchanged with makeup water introduced from the pipe 37 to generate low-pressure steam. The generated low pressure steam is supplied to the steam turbine 4 from the pipe 34 through the mist separator 8 and the pipe 35 as described above. On the other hand, the condensed water is discharged out of the system through the pipe 38.
【００２８】蒸気タービン４からの排蒸気は、配管３９
を経て熱交換器１７に導入され、熱交換器１７で生成し
た凝縮水は凝縮水ポンプ１３を備える配管４０を経て、
配管２５，２６より前述の蒸気発生器２Ｂ，３Ｂの補給
水として、また、配管３７より上述の低圧蒸気発生装置
６の補給水として循環使用される。また、熱交換器１７
の未凝縮ガスは、配管４１、真空ポンプ１４を経て系外
へ排出される。The exhaust steam from the steam turbine 4 is supplied to the pipe 39.
The condensed water introduced into the heat exchanger 17 through the heat exchanger 17 passes through the pipe 40 equipped with the condensed water pump 13,
It is circulated and used as makeup water for the steam generators 2B and 3B described above through the pipes 25 and 26, and as makeup water for the low pressure steam generator 6 described above through the pipe 37. In addition, the heat exchanger 17
The uncondensed gas is discharged to the outside of the system through the pipe 41 and the vacuum pump 14.
【００２９】本発明の方法においては、このように、高
圧蒸気及び低圧蒸気の各エネルギーを入力して稼動させ
た蒸気タービン４と、高圧蒸気発生装置の排ガスのエネ
ルギーを入力して稼動させたガスタービン５とを、酸化
反応器１に酸素源として供給する圧縮空気を得るための
コンプレッサー９に直結させ、蒸気タービン４及びガス
タービン９をコンプレッサー９の動力源として機能させ
る。In the method of the present invention, as described above, the steam turbine 4 operated by inputting each energy of the high pressure steam and the low pressure steam and the gas operated by inputting the energy of the exhaust gas of the high pressure steam generator. The turbine 5 is directly connected to a compressor 9 for obtaining compressed air to be supplied to the oxidation reactor 1 as an oxygen source, and the steam turbine 4 and the gas turbine 9 function as a power source of the compressor 9.
【００３０】なお、通常の場合、蒸気タービン４とガス
タービン５の出力は同程度であり、各々、コンプレッサ
ー９の所要エネルギーの約４７％程度である。In the normal case, the outputs of the steam turbine 4 and the gas turbine 5 are about the same, which are about 47% of the required energy of the compressor 9, respectively.
【００３１】従って、蒸気タービン４及びガスタービン
５の出力のみではコンプレッサー９の稼動に必要なエネ
ルギーが不足するので、必要に応じて図１に示す如くモ
ーター１２を併設して、不足するエネルギー（約６％
（＝１００−４７×２））を補充する。Therefore, the energy required for the operation of the compressor 9 is insufficient only with the outputs of the steam turbine 4 and the gas turbine 5. Therefore, if necessary, a motor 12 is provided as shown in FIG. 6%
(= 100-47 × 2)).
【００３２】なお、図１に示す方法は、本発明の一実施
方法であって、本発明はその要旨を超えない限り、図示
の実施例に限定されるものではなく、各装置の設置態様
等において、他の様々な態様を採用し得る。例えば、高
圧蒸気発生装置の設置数については、２機に限らず、反
応器、脱水塔の規模や設定条件等に応じて、１機又は３
機以上とすることができる。The method shown in FIG. 1 is an embodiment of the present invention, and the present invention is not limited to the illustrated embodiment as long as it does not exceed the gist of the present invention. In, various other modes can be adopted. For example, the number of high-pressure steam generators installed is not limited to two, but one or three depending on the scale of reactors, dehydration towers, setting conditions, and the like.
It can be more than a machine.
【００３３】また、高圧蒸気発生装置２で発生した高圧
蒸気の蒸気タービン４への供給割合を増加することによ
り、蒸気タービン４の出力を増加させ、モーター１２の
稼動を停止することもできる。The output of the steam turbine 4 can be increased and the operation of the motor 12 can be stopped by increasing the supply ratio of the high pressure steam generated by the high pressure steam generator 2 to the steam turbine 4.
【００３４】[0034]
【発明の効果】以上詳述した通り、本発明の芳香族カル
ボン酸の製造方法によれば、アルキル芳香族炭化水素を
酸化して芳香族カルボン酸を製造するにあたり、製造工
程で発生する廃熱を著しく効率的に有効利用することが
でき、エネルギー効率の向上、エネルギーコストの低減
を図ることができる。As described above in detail, according to the method for producing an aromatic carboxylic acid of the present invention, the waste heat generated in the production process in producing an aromatic carboxylic acid by oxidizing an alkyl aromatic hydrocarbon Can be effectively used effectively, and energy efficiency can be improved and energy cost can be reduced.
【００３５】請求項２の方法によれば、より一層効率的
な廃熱利用が可能とされる。According to the method of claim 2, it is possible to use waste heat more efficiently.
【図１】本発明の実施に好適なテレフタル酸製造装置の
一例を示す系統図である。FIG. 1 is a system diagram showing an example of a terephthalic acid production apparatus suitable for carrying out the present invention.
１ 酸化反応器 ２，３ 高圧蒸気発生装置 ４ 蒸気タービン ５ ガスタービン ６ 低圧蒸気発生装置 ７ 脱水塔 ８ ミストセパレーター ９ コンプレッサー １０ 吸収塔 １１ 加熱器 １２ モーター １３ 凝縮水ポンプ １４ 真空ポンプ １５，１６ 圧力調節器 １７ 熱交換器 １８ バルブ 1 Oxidation Reactor 2,3 High Pressure Steam Generator 4 Steam Turbine 5 Gas Turbine 6 Low Pressure Steam Generator 7 Dewatering Tower 8 Mist Separator 9 Compressor 10 Absorption Tower 11 Heater 12 Motor 13 Condensed Water Pump 14 Vacuum Pump 15, 16 Pressure Control Vessel 17 heat exchanger 18 valve
Claims (2)
素を低級脂肪族カルボン酸溶媒中で分子状酸素含有ガス
により酸化して芳香族カルボン酸を製造する方法におい
て、 酸化反応器からの排ガスを高圧蒸気発生器に通した後、
ガスタービンに供給すると共に、該高圧蒸気発生器で発
生した高圧蒸気を蒸気タービンに供給し、該ガスタービ
ンと該蒸気タービンとを稼動させて得た出力で空気圧縮
器を稼動させ、該空気圧縮器からの圧縮空気を前記分子
状酸素含有ガスとして使用することを特徴とする芳香族
カルボン酸の製造方法。1. A method for producing an aromatic carboxylic acid by oxidizing an alkylaromatic hydrocarbon with a molecular oxygen-containing gas in a lower aliphatic carboxylic acid solvent in an oxidation reactor, wherein exhaust gas from the oxidation reactor is used. Through the high pressure steam generator,
The high-pressure steam generated by the high-pressure steam generator is supplied to the gas turbine, and the high-pressure steam is supplied to the steam turbine. The air compressor is operated by the output obtained by operating the gas turbine and the steam turbine, and the air compression is performed. A method for producing an aromatic carboxylic acid, characterized in that compressed air from a vessel is used as the molecular oxygen-containing gas.
から芳香族カルボン酸を除去した後、脱水塔にて低級脂
肪族カルボン酸溶媒を回収するにあたり、該脱水塔から
留去される蒸気を低圧蒸気発生器を経て、系外に排出す
ると共に、該低圧蒸気発生器で発生した低圧蒸気を前記
高圧蒸気と共に前記蒸気タービンに供給することを特徴
とする芳香族カルボン酸の製造方法。2. The method according to claim 1, wherein after the aromatic carboxylic acid is removed from the oxidation reaction product solution, when the lower aliphatic carboxylic acid solvent is recovered in the dehydration tower, the vapor distilled off from the dehydration tower is used. A method for producing an aromatic carboxylic acid, characterized in that the low pressure steam is discharged to the outside of the system via a low pressure steam generator and the low pressure steam generated in the low pressure steam generator is supplied to the steam turbine together with the high pressure steam.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02128092A JP3291749B2 (en) | 1992-02-06 | 1992-02-06 | Method for producing aromatic carboxylic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02128092A JP3291749B2 (en) | 1992-02-06 | 1992-02-06 | Method for producing aromatic carboxylic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05213816A true JPH05213816A (en) | 1993-08-24 |
| JP3291749B2 JP3291749B2 (en) | 2002-06-10 |
Family
ID=12050727
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP02128092A Expired - Lifetime JP3291749B2 (en) | 1992-02-06 | 1992-02-06 | Method for producing aromatic carboxylic acid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3291749B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5723656A (en) * | 1994-10-14 | 1998-03-03 | Amoco Corporation | Process for preparing aromatic carboxylic acids with efficient energy recovery |
| EP0962442A1 (en) * | 1998-06-05 | 1999-12-08 | Mitsui Chemicals, Inc. | Process for producing aromatic carboxylic acid |
| US7213540B2 (en) | 2004-02-05 | 2007-05-08 | Eastman Chemical Company | Steam recompression in carboxylic acid processes |
| WO2007133377A1 (en) * | 2006-05-10 | 2007-11-22 | Eastman Chemical Company | Process for driving gas blowers or fans in a solid-state polymerization process using steam from a terephthalic acid plant |
| JP2020509015A (en) * | 2017-02-28 | 2020-03-26 | グルポ、ペトロテメックス、ソシエダッド、アノニマ、デ、カピタル、バリアブレＧｒｕｐｏ Ｐｅｔｒｏｔｅｍｅｘ，Ｓ．Ａ． Ｄｅ Ｃ．Ｖ． | Integrated energy and environment method for producing aromatic dicarboxylic acids by oxidation |
-
1992
- 1992-02-06 JP JP02128092A patent/JP3291749B2/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5723656A (en) * | 1994-10-14 | 1998-03-03 | Amoco Corporation | Process for preparing aromatic carboxylic acids with efficient energy recovery |
| EP0962442A1 (en) * | 1998-06-05 | 1999-12-08 | Mitsui Chemicals, Inc. | Process for producing aromatic carboxylic acid |
| US6143925A (en) * | 1998-06-05 | 2000-11-07 | Mitsui Chemicals, Inc. | Process for producing aromatic carboxylic acid |
| US7213540B2 (en) | 2004-02-05 | 2007-05-08 | Eastman Chemical Company | Steam recompression in carboxylic acid processes |
| JP2007526915A (en) * | 2004-02-05 | 2007-09-20 | イーストマン ケミカル カンパニー | Vapor recompression in aromatic carboxylic acid processes. |
| WO2007133377A1 (en) * | 2006-05-10 | 2007-11-22 | Eastman Chemical Company | Process for driving gas blowers or fans in a solid-state polymerization process using steam from a terephthalic acid plant |
| JP2020509015A (en) * | 2017-02-28 | 2020-03-26 | グルポ、ペトロテメックス、ソシエダッド、アノニマ、デ、カピタル、バリアブレＧｒｕｐｏ Ｐｅｔｒｏｔｅｍｅｘ，Ｓ．Ａ． Ｄｅ Ｃ．Ｖ． | Integrated energy and environment method for producing aromatic dicarboxylic acids by oxidation |
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| Publication number | Publication date |
|---|---|
| JP3291749B2 (en) | 2002-06-10 |
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