JPS63107728A - Method and apparatus for recovering cyclohexanone - Google Patents
Method and apparatus for recovering cyclohexanoneInfo
- Publication number
- JPS63107728A JPS63107728A JP61251968A JP25196886A JPS63107728A JP S63107728 A JPS63107728 A JP S63107728A JP 61251968 A JP61251968 A JP 61251968A JP 25196886 A JP25196886 A JP 25196886A JP S63107728 A JPS63107728 A JP S63107728A
- Authority
- JP
- Japan
- Prior art keywords
- cyclohexanone
- absorption
- absorption liquid
- raw gas
- tower
- 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
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 title claims abstract description 86
- 238000000034 method Methods 0.000 title claims abstract description 11
- 238000010521 absorption reaction Methods 0.000 claims abstract description 57
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 238000004821 distillation Methods 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract 9
- 239000002918 waste heat Substances 0.000 claims abstract 2
- 239000007788 liquid Substances 0.000 claims description 37
- 238000011084 recovery Methods 0.000 claims description 15
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000003507 refrigerant Substances 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 abstract description 2
- 230000000630 rising effect Effects 0.000 abstract 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
- 239000002904 solvent Substances 0.000 description 11
- 238000001179 sorption measurement Methods 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- FWFSEYBSWVRWGL-UHFFFAOYSA-N cyclohex-2-enone Chemical compound O=C1CCCC=C1 FWFSEYBSWVRWGL-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- ZRJUCHNILNOEKV-UHFFFAOYSA-N hexan-2-one hydrate Chemical compound O.CCCCC(C)=O ZRJUCHNILNOEKV-UHFFFAOYSA-N 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000001256 steam distillation Methods 0.000 description 1
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
【発明の詳細な説明】
〔産業上の利用分野〕
本発明はシクロヘキサノン含有空気中からシクロヘキテ
ノンを回収する方法及びその装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a method and apparatus for recovering cyclohexenone from cyclohexanone-containing air.
〔従来の技術］ 従来は活性炭吸脱着方法により回収している。[Conventional technology] Conventionally, it has been recovered by activated carbon adsorption/desorption method.
第２図に従来のシクロヘキサノン回収プロセスを示す。Figure 2 shows a conventional cyclohexanone recovery process.
ここで原ガス１０１はガスプロア１０８によシ吸引され
、最初にガスフィルタ１０３により不純物（ダスト類他
）を除去した後ガスクーラ１０４で活性炭１０６の吸着
に適した温度（４０℃程度）Ｋ冷却される。ガスクーラ
１（１４の冷却はガスと冷却水（通常冷却水はクーリン
グタワで冷却し丸木を循環再利用している）の間接熱交
換により行う。吸着に適した温度に冷却された原ガス１
０１は吸Ｍ槽１０５に送られ、原ガス中の溶剤成分は吸
着槽内に充填する活性炭１０６に吸着される。溶剤成分
を除いた原ガスは吸着槽上部から大気に排出される。活
性炭１０６の溶剤吸着量が限界に近づき、排気側に溶剤
が流出する直前で吸着を停止する。次いで吸着槽に水蒸
気を導入して、活性炭に吸着している溶剤を脱離し、水
蒸気とともにフラッシュタンク１０８を経て、コンデン
サ１０９に導入して冷却凝縮する。この凝縮液はセパレ
ータ１１０で水と溶剤に分離する。分離された水はフラ
ッシュタンク１０８に戻し吸着槽１０５からの溶剤含有
水蒸気により簡易水蒸気蒸留し、水中の大部分の溶剤を
分離する。フラッシュタンク１０８の水は一担排水タン
ク１１１に溜めてから排水蒸留塔１１２に送られ、さら
に溶剤成分を分離した後排水される。排水蒸留塔１１２
で分離した溶剤成分はフラッシュタンク１０８からの流
出ガスと混合され、コンデンサ１０９に導入する。Here, the raw gas 101 is sucked in by a gas prower 108, first removes impurities (dust, etc.) by a gas filter 103, and then cooled by a gas cooler 104 to a temperature suitable for adsorption of activated carbon 106 (approximately 40°C). . Gas cooler 1 (14) is cooled by indirect heat exchange between gas and cooling water (normally cooling water is cooled in a cooling tower and logs are recycled and reused). Raw gas 1 is cooled to a temperature suitable for adsorption.
01 is sent to an M absorption tank 105, and the solvent component in the raw gas is adsorbed by activated carbon 106 filled in the adsorption tank. The raw gas excluding the solvent component is discharged into the atmosphere from the upper part of the adsorption tank. The adsorption is stopped just before the amount of solvent adsorbed by the activated carbon 106 approaches its limit and the solvent flows out to the exhaust side. Next, water vapor is introduced into the adsorption tank to desorb the solvent adsorbed on the activated carbon, and the water vapor is introduced together with the water vapor into a condenser 109 via a flash tank 108, where it is cooled and condensed. This condensate is separated into water and solvent by a separator 110. The separated water is returned to the flash tank 108 and subjected to simple steam distillation using solvent-containing steam from the adsorption tank 105 to separate most of the solvent in the water. The water in the flash tank 108 is stored in a single wastewater tank 111 and then sent to a wastewater distillation column 112, where the solvent component is further separated and then drained. Wastewater distillation column 112
The separated solvent components are mixed with the effluent gas from flash tank 108 and introduced into condenser 109 .
一方、セパレータ１１０で分離された溶剤は、平衡溶解
量の水分を含むので、さらに蒸留塔で脱水して再利用さ
れる。On the other hand, since the solvent separated by the separator 110 contains an equilibrium dissolved amount of water, it is further dehydrated in a distillation column and reused.
この回収プロセスでは、吸着槽の活性炭中でシクロヘキ
サノンが重縮合反応を起こし易い。In this recovery process, cyclohexanone tends to undergo a polycondensation reaction in the activated carbon of the adsorption tank.
この重合物は活性炭を劣化させるために、活性炭の早期
取り替えが必要と彦り、うｙニングコストが膨大となる
。This polymer deteriorates the activated carbon, requiring early replacement of the activated carbon, resulting in enormous costs.
本発明は、従来のシクロヘキサノン回収装置の欠点を解
消し、シクロヘキサノンの回収効率が高く、ランニング
コストを低減することができるシクロヘキサノン回収方
法及びその装置を提供しようとするものである。The present invention aims to provide a cyclohexanone recovery method and apparatus that can overcome the drawbacks of conventional cyclohexanone recovery devices, have high cyclohexanone recovery efficiency, and reduce running costs.
本発明は
（１） シクロヘキサノン含有原ガスを吸収液に吸収
させた後、該吸収液を蒸留してシクロヘキノンを濃縮回
収する方法において、蒸留工程で使用する水蒸気の廃熱
を吸収式冷凍機の熱源となし、この冷凍機により前記原
ガス及び吸収液を予じめ冷却してから吸収工程に導入す
ることを特徴とするシクロヘキサノン回収方法。The present invention provides (1) a method in which cyclohexanone-containing raw gas is absorbed into an absorption liquid, and then the absorption liquid is distilled to concentrate and recover cyclohexquinone; A method for recovering cyclohexanone, characterized in that the raw gas and absorption liquid are cooled in advance using the refrigerator as a heat source and then introduced into an absorption step.
（２） シクロヘキサノン含有原ガス導管を塔の下部
に接続し、塔の上部に吸収液導管を接続する吸収塔と、
吸収塔の塔底の吸収液を導入し、水蒸気を塔底に導入し
て吸収液からシクロヘキサノンを濃縮分離する蒸留塔と
を有し、蒸留塔の塔底を上記吸収液導管と接続して再生
吸収液を吸収塔に循環するようにし之シクロヘキサノン
回収装置において、蒸留塔の塔頂から流出する濃縮シク
ロヘキサノンの潜熱を利用して稼動する吸収式冷凍機を
、上記原ガス導管に設けたガスクーラ及び上記吸収液導
管に設けた吸収液クーラと冷媒導管で接続することを特
徴とするシクロヘキサノン回収装置。(2) an absorption tower in which a cyclohexanone-containing raw gas conduit is connected to the lower part of the tower and an absorption liquid conduit is connected to the upper part of the tower;
It has a distillation column that introduces the absorption liquid at the bottom of the absorption tower and introduces water vapor to the bottom of the column to concentrate and separate cyclohexanone from the absorption liquid, and the bottom of the distillation column is connected to the absorption liquid conduit for regeneration. In the cyclohexanone recovery device in which the absorption liquid is circulated to the absorption tower, an absorption chiller that operates by utilizing the latent heat of concentrated cyclohexanone flowing out from the top of the distillation column is installed in the raw gas conduit and the gas cooler and the above-mentioned gas cooler. A cyclohexanone recovery device characterized by connecting an absorption liquid cooler provided in an absorption liquid conduit with a refrigerant conduit.
である。It is.
第１図に本発明のシクロヘキサノンの回収プロセスを示
す。ここでシクロヘキサノン含有原ガス１はガスブロア
２により吸引され、最初ガスフィルタ３に入り不純物（
ダスト類他）を除去した後ガスクーラ４に導入され吸収
効率を上げるため、２５℃以下に冷却される。ガスクー
ラ４で冷却された原ガス１は吸収塔５下部から導入され
、上部から流入する吸収液と気液接触し原ガス１中のシ
クロヘキサノンを吸収液中に吸収する。FIG. 1 shows the cyclohexanone recovery process of the present invention. Here, the raw gas 1 containing cyclohexanone is sucked by the gas blower 2, and first enters the gas filter 3, which contains impurities (
After removing dust, etc.), the gas is introduced into a gas cooler 4 and cooled to 25° C. or lower to increase absorption efficiency. The raw gas 1 cooled by the gas cooler 4 is introduced from the lower part of the absorption tower 5, comes into gas-liquid contact with the absorption liquid flowing from the upper part, and cyclohexanone in the raw gas 1 is absorbed into the absorption liquid.
なお、吸収液は、２５℃以下に冷却された水を使用した
。Note that water cooled to 25° C. or lower was used as the absorption liquid.
シクロヘキサノンを吸収した吸収液は蒸留塔フィードポ
ンプ６によシ吸収液熱交換器７に送られて加熱した後蒸
留塔８に送られる。The absorption liquid that has absorbed cyclohexanone is sent to the absorption liquid heat exchanger 7 by the distillation column feed pump 6, heated, and then sent to the distillation column 8.
蒸留塔８では、下部に吹込まれる水蒸気にょシ吸収液中
のシクロヘキサノンが蒸留除去される。In the distillation column 8, cyclohexanone in the steam absorption liquid blown into the lower part is removed by distillation.
シクロヘキサノンを除去した吸収液は吸収液熱交換器７
に送られ前記のシクロヘキサノンを吸収した低温の吸収
液と間接熱交換される。その後吸収液クーラ９に流れ冷
水により２５℃以下に冷却され、吸収液ポンプ１０によ
シ再びシクロヘキサノンを吸収するための吸収液として
吸収塔５上部に送られる。The absorption liquid from which cyclohexanone has been removed is transferred to the absorption liquid heat exchanger 7.
The liquid is sent to the cyclohexanone and undergoes indirect heat exchange with the low-temperature absorption liquid that has absorbed the cyclohexanone. Thereafter, it flows into the absorption liquid cooler 9 and is cooled to 25° C. or lower with cold water, and is sent to the upper part of the absorption tower 5 by the absorption liquid pump 10 as an absorption liquid for absorbing cyclohexanone.
一方蒸留塔８で蒸留されたシクロヘキサノンは水との共
沸組成まで濃縮され蒸留塔８の塔頂から温水回収熱交換
器１１に送られる。ここで温水との間接熱交換によりシ
クロヘキサノン蒸気及び水蒸気の潜熱が温水の昇温に利
用される。On the other hand, cyclohexanone distilled in the distillation column 8 is concentrated to an azeotropic composition with water and sent from the top of the distillation column 8 to the hot water recovery heat exchanger 11. Here, the latent heat of the cyclohexanone vapor and water vapor is used to raise the temperature of the hot water through indirect heat exchange with the hot water.
温水は吸収式冷凍機１２に送られ熱を与えた後再び温水
ボ／プ１３により温水回収熱交換器１１に戻される。The hot water is sent to the absorption chiller 12, where it is given heat, and then returned to the hot water recovery heat exchanger 11 by the hot water pump 13.
吸収式冷凍機１２では、ガスクーラ４及び吸収液クーラ
９から昇温されて戻って来る冷水を冷却して、再び冷水
ポンプ１４によりガスクーラ４及び吸収液クー２９に送
り出す。The absorption chiller 12 cools the heated cold water returned from the gas cooler 4 and the absorption liquid cooler 9 and sends it out again to the gas cooler 4 and the absorption liquid cooler 29 by the cold water pump 14.
また温水回収熱交換器１１で温水に潜熱を与え大部分凝
縮したシクロヘキサノン及び水蒸気はりフラックスコン
デンサ１５に送られ、ここで完全に凝縮する。The hot water recovery heat exchanger 11 imparts latent heat to the hot water and most of the condensed cyclohexanone and water vapor are sent to the flux condenser 15, where they are completely condensed.
す７ラツクスコンデンサ１５を出たシクロヘキサノン及
び水は一部蒸留塔８に還流され残りは、セパレータ１６
に流れ、水とシクロヘキサノンに分離される。水は蒸留
塔８に戻され、シクロヘキサノンは平衡溶解分の水を含
むため、蒸留設備等に送られ脱水し再利用される。A portion of the cyclohexanone and water exiting the 7-lux condenser 15 is refluxed to the distillation column 8, and the remainder is sent to the separator 16.
is separated into water and cyclohexanone. The water is returned to the distillation column 8, and since the cyclohexanone contains equilibrium dissolved water, it is sent to a distillation facility or the like to be dehydrated and reused.
本発明は上記構成を採用することによプ、大巾なランニ
ングコストの低減を可能とした。特に、蒸留塔の塔頂ガ
スの潜熱により吸収式冷凍機を稼動させ、原ガス及び循
環吸収液を冷却することができ、換言すると、蒸留塔に
導入する水蒸気の廃熱に利用することにより上記冷却を
可能とし、吸収効率を向上させたもので、原ガス中のシ
クロヘキサン濃度が高くなるほどランニングコストの低
減率は大きくなる。濃度が２０００ ｐｐｍの場合従来
法に比べて４〜５割程度ランニングコストを低減できる
。By employing the above configuration, the present invention has made it possible to significantly reduce running costs. In particular, it is possible to operate an absorption refrigerator using the latent heat of the top gas of the distillation column to cool the raw gas and the circulating absorption liquid.In other words, by using the latent heat of the steam introduced into the distillation column as It enables cooling and improves absorption efficiency, and the higher the cyclohexane concentration in the raw gas, the greater the rate of reduction in running costs. When the concentration is 2000 ppm, the running cost can be reduced by about 40 to 50% compared to the conventional method.
第１図は本発明のシクロヘキサノン回収プロセスを示し
た図、第２図は従来の吸着式シクロヘキサノン回収プロ
セスを示した図である。
復代理人 内 １） 明
復代理人 萩 原 亮 −
復代理人 安 西 篤 夫FIG. 1 is a diagram showing the cyclohexanone recovery process of the present invention, and FIG. 2 is a diagram showing the conventional adsorption type cyclohexanone recovery process. Sub-Agents 1) Meifuku Agent Ryo Hagiwara − Sub-Agent Atsuo Anzai
Claims (2)
た後該吸収液を蒸留してシクロヘキノンを濃縮回収する
方法において、蒸留工程で使用する水蒸気の廃熱を吸収
式冷凍機の熱源となし、この冷凍機により前記原ガス及
び吸収液を予じめ冷却してから吸収工程に導入すること
を特徴とするシクロヘキサノン回収方法。(1) In a method of absorbing raw gas containing cyclohexanone into an absorption liquid and then distilling the absorption liquid to concentrate and recover cyclohexquinone, waste heat of water vapor used in the distillation process is used as a heat source for an absorption refrigerator, A method for recovering cyclohexanone, characterized in that the raw gas and absorption liquid are cooled in advance by this refrigerator before being introduced into an absorption step.
続し、塔の上部に吸収液導管を接続する吸収塔と、吸収
塔の塔底の吸収液を導入し、水蒸気を塔底に導入して吸
収液からシクロヘキサノンを濃縮分離する蒸留塔とを有
し、蒸留塔の塔底を上記吸収液導管と接続して再生吸収
液を吸収塔に循環するようにしたシクロヘキサノン回収
装置において、蒸留塔の塔頂から流出する濃縮シクロヘ
キサノンの潜熱を利用して稼動する吸収式冷凍機を、上
記原ガス導管に設けたガスクーラ及び上記吸収液導管に
設けた吸収液クーラと冷媒導管で接続することを特徴と
するシクロヘキサノン回収装置。(2) An absorption tower in which a cyclohexanone-containing raw gas pipe is connected to the bottom of the tower and an absorption liquid pipe is connected to the top of the tower, the absorption liquid is introduced at the bottom of the absorption tower, and water vapor is introduced to the bottom of the tower. In a cyclohexanone recovery apparatus, the distillation column has a distillation column that concentrates and separates cyclohexanone from the absorption liquid, and the bottom of the distillation column is connected to the absorption liquid conduit to circulate the regenerated absorption liquid to the absorption column. An absorption chiller operated by utilizing the latent heat of concentrated cyclohexanone flowing out from the top is connected to a gas cooler provided in the raw gas conduit and an absorption liquid cooler provided in the absorption liquid conduit through a refrigerant conduit. Cyclohexanone recovery equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61251968A JPH0738933B2 (en) | 1986-10-24 | 1986-10-24 | Cyclohexanone recovery method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61251968A JPH0738933B2 (en) | 1986-10-24 | 1986-10-24 | Cyclohexanone recovery method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63107728A true JPS63107728A (en) | 1988-05-12 |
| JPH0738933B2 JPH0738933B2 (en) | 1995-05-01 |
Family
ID=17230673
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61251968A Expired - Lifetime JPH0738933B2 (en) | 1986-10-24 | 1986-10-24 | Cyclohexanone recovery method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0738933B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105254486B (en) * | 2015-11-09 | 2017-06-06 | 山东寿光巨能金玉米开发有限公司 | A kind of D lactic acid decoloration process |
-
1986
- 1986-10-24 JP JP61251968A patent/JPH0738933B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0738933B2 (en) | 1995-05-01 |
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