JP2009249373A - Method for recovering phenol from phenols-containing waste liquid - Google Patents
Method for recovering phenol from phenols-containing waste liquid Download PDFInfo
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- JP2009249373A JP2009249373A JP2008103468A JP2008103468A JP2009249373A JP 2009249373 A JP2009249373 A JP 2009249373A JP 2008103468 A JP2008103468 A JP 2008103468A JP 2008103468 A JP2008103468 A JP 2008103468A JP 2009249373 A JP2009249373 A JP 2009249373A
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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 title claims abstract description 105
- 239000007788 liquid Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000002699 waste material Substances 0.000 title claims abstract description 32
- 150000002989 phenols Chemical class 0.000 title abstract description 5
- 238000004062 sedimentation Methods 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 19
- 239000005011 phenolic resin Substances 0.000 claims abstract description 16
- 239000012260 resinous material Substances 0.000 claims abstract description 4
- 238000011084 recovery Methods 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 239000011347 resin Substances 0.000 claims description 2
- 229920005989 resin Polymers 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 238000001816 cooling Methods 0.000 description 7
- 238000012545 processing Methods 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 230000005856 abnormality Effects 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 229910002056 binary alloy Inorganic materials 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 239000002440 industrial waste Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 101100298225 Caenorhabditis elegans pot-2 gene Proteins 0.000 description 1
- 238000009529 body temperature measurement Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000012261 resinous substance Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
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Abstract
Description
本発明はフェノール樹脂製造工程から排出される廃液からフェノールを経済的に回収し、安定的に利用する方法に関するものである。 The present invention relates to a method for economically recovering phenol from waste liquid discharged from a phenol resin production process and using it stably.
フェノール樹脂製造において脱水、濃縮工程から排出される廃液には未反応フェノール分が含まれ、通常フェノール濃度5〜30重量%の廃液が排出される。従来、廃液の処理は、所定の処理を施した後、産業廃棄物取扱業者に引渡したり、工場内で生物による分解処理を行い放流をしていたが、産業廃棄物の処理には慎重を要すると共に、近年、特に処理費が高騰している。また、フェノールは有害な環境汚染物質であるので、水質汚濁防止法で定められた基準値以下の濃度に処理しなくてはならないため、処理コストが嵩む。そこで、フェノール成分を回収して再利用する方法が種々検討されている。
フェノール成分を回収する方法とすれば、例えば、特開昭60−6628号公報等が開示されている。フェノール樹脂の製造工程から排出される廃液をタンク1で不純物を沈降分離させて除去して後、30℃以下に冷却し、次いでタンク2でフェノールを沈降分離させて、フェノール濃度の低下した上澄み液をタンク1へ戻す工程と、フェノール濃度が向上した沈降液を回収する工程とを備える方法及び該方法を実施する処理装置が開示されているで。この方法で得られる回収フェノールのフェノール濃度は70重量%前後と高く、工業原料として再利用が可能であるが、タンク2とタンク3の温度条件が変動すると、更に分離してしまい、フェノール濃度も変化してしまう。そのため回収フェノールの使用に当たりフェノール濃度の再測定等が必要になる。このため保管された回収フェノールを直接プロセスで利用する点妨げとなってしまう。 As a method for recovering the phenol component, for example, JP-A-60-6628 is disclosed. After the waste liquid discharged from the phenol resin production process is removed by precipitation in the tank 1, the liquid is cooled to 30 ° C. or lower, and then the phenol is settled and separated in the tank 2. A method including a step of returning the liquid to the tank 1 and a step of recovering a sedimented liquid having an improved phenol concentration and a processing apparatus for carrying out the method are disclosed. The phenol concentration of the recovered phenol obtained by this method is as high as around 70% by weight and can be reused as an industrial raw material. However, when the temperature conditions of the tank 2 and the tank 3 fluctuate, they are further separated, and the phenol concentration is also high. It will change. Therefore, it is necessary to remeasure the phenol concentration when using the recovered phenol. As a result, the stored recovered phenol is prevented from being directly used in the process.
このような問題を解決するため、タンク1とタンク2の温度差を好ましくは、2〜30℃付ければよい。但し、30℃の温度差を付けるには大量の冷却水等が必要になり、エネルギー経済的に非常に不利になってくる。また、2℃以下の温度差になってしまうと保管タンクであるタンク3で、大量の分離が発生してしまう。これらの点よりタンク1とタンク2の温度差は、2〜15℃の冷却とする。 In order to solve such a problem, the temperature difference between the tank 1 and the tank 2 is preferably 2 to 30 ° C. However, in order to give a temperature difference of 30 ° C., a large amount of cooling water or the like is required, which is very disadvantageous in terms of energy economy. If the temperature difference is 2 ° C. or less, a large amount of separation occurs in the tank 3 which is a storage tank. From these points, the temperature difference between the tank 1 and the tank 2 is 2 to 15 ° C. cooling.
冷却が十分であった場合では、タンク2とタンク3では水とフェノールの分離は起きないが、外気温等でタンク2とタンク3で水とフェノールの分離が生じることがある。そこで、タンク2とタンク3のフェノール濃度と、水とフェノールの分離状況を簡易に測定できる方法を探索した。
本発明は、フェノール樹脂の製造工程から排出される廃液からフェノールを回収する方法において、そのプロセスで回収フェノールを迅速に使用する方法を提供することを目的とする。
When cooling is sufficient, separation of water and phenol does not occur in tank 2 and tank 3, but separation of water and phenol may occur in tank 2 and tank 3 due to outside air temperature or the like. Therefore, the inventors searched for a method that can easily measure the phenol concentration in tanks 2 and 3 and the separation status of water and phenol.
An object of the present invention is to provide a method of quickly using recovered phenol in a process for recovering phenol from waste liquid discharged from a phenol resin production process.
本発明は、フェノール樹脂の製造工程から排出される廃液からフェノールを回収する方法において、該廃液を静置分離した後、温度測定及び導電率測定を行うことにより、フェノール濃度を計算で求め、プロセスで回収フェノールを迅速に使用する方法を提供する。本発明により回収フェノールの温度と電気導電率を測定すれば、濃度が決定された回収フェノールを簡易に回収し、使用できることを見出し、本発明を完成するに至った。 The present invention relates to a process for recovering phenol from waste liquid discharged from a phenol resin production process, and after standing and separating the waste liquid, by performing temperature measurement and conductivity measurement, the phenol concentration is calculated and calculated. Provides a method for rapid use of recovered phenol. By measuring the temperature and electrical conductivity of the recovered phenol according to the present invention, it was found that the recovered phenol whose concentration was determined could be easily recovered and used, and the present invention was completed.
すなわち、本発明の詳細を以下に述べる。
(1)フェノール樹脂製造工程から排出されるフェノール類含有廃液(以下、廃液と略す)からフェノールを回収する方法において、該廃液を第1沈降分離槽(以下、タンク1と略す)で樹脂状物を沈降分離させて除去した後、30℃以下に冷却し、次いで第2沈降分離槽(以下、タンク2と略す)で、第1沈降分離槽(タンク1)との温度差を2〜15℃にして、フェノールを沈降分離させてから回収フェノールタンク(以下、タンク3と略す)に保管し、樹脂製造プロセスへ使用することを特徴とするフェノールの回収方法。
(2)フェノール樹脂製造工程から排出される廃液を処理する第1沈降分離槽(タンク1)と、熱交換器の後工程に位置する第2沈降分離槽(タンク2)と、回収フェノールタンク(タンク3)のフェノール回収系に設置される温度計と電気導電率計を備えることで、簡易にフェノール濃度を測定することを特徴とする(1)記載のフェノールの回収方法。
That is, details of the present invention will be described below.
(1) In a method for recovering phenol from a phenol-containing waste liquid (hereinafter abbreviated as waste liquid) discharged from a phenol resin manufacturing process, the waste liquid is resin-like in a first sedimentation separation tank (hereinafter abbreviated as tank 1). Is removed by sedimentation, and then cooled to 30 ° C. or lower. Then, in the second sedimentation separation tank (hereinafter abbreviated as tank 2), the temperature difference from the first sedimentation tank (tank 1) is 2 to 15 ° C. Then, the phenol is precipitated and separated, stored in a recovered phenol tank (hereinafter abbreviated as tank 3), and used in a resin manufacturing process.
(2) a first sedimentation / separation tank (tank 1) for treating the waste liquid discharged from the phenol resin production process, a second sedimentation / separation tank (tank 2) located in a post-process of the heat exchanger, and a recovered phenol tank ( The phenol recovery method according to (1), wherein the phenol concentration is easily measured by providing a thermometer and an electrical conductivity meter installed in the phenol recovery system of the tank 3).
本発明により、廃液をタンク1で不純物を沈降分離させて除去して後、30℃以下に冷却し、次いでタンク2でフェノールを沈降分離させて、フェノール濃度が向上した沈降液を、タンク3へ回収する場合、通常、フェノール濃度は70重量%前後と高いが、保管時においても温度条件が変動すると再び分離するため、フェノール濃度がばらつく。このときタンク2とタンク3の回収フェノール温度と、電気導電率を簡易且つ迅速に測定することで、フェノール濃度を把握することができ、安定したフェノール濃度の回収フェノールをプロセスで使用することが可能となった。 According to the present invention, the waste liquid is removed by sedimentation and separation in the tank 1, and then cooled to 30 ° C. or lower, and then the phenol is sedimented and separated in the tank 2, so that the precipitation liquid with improved phenol concentration is supplied to the tank 3 In the case of recovery, the phenol concentration is usually as high as about 70% by weight, but the phenol concentration varies because it is separated again when the temperature condition fluctuates even during storage. At this time, by simply and quickly measuring the recovered phenol temperature and electrical conductivity of tank 2 and tank 3, the phenol concentration can be grasped, and the recovered phenol having a stable phenol concentration can be used in the process. It became.
本発明のフェノールの回収方法は、例えば、樹脂状物を沈降分離させて除去する工程(タンク1)、30℃以下に冷却し沈降分離槽でフェノールを沈降分離させる工程(タンク2)、それらを回収し保管する工程(タンク3)、およびフェノール濃度を簡易に測定することを組み合わせる。タンク1及びタンク2の温度は低温である方が回収フェノールの濃度が高くなり、使用においては有効である。そのためタンク1では、空冷によりある程度温度を下げ、更にタンク2に移送する段階で2〜30℃温度を下げるのが好ましい。2℃以下の場合には、冷却の実質的効果が少なく装置費用が無駄に終わる可能性があり、30℃以上の場合には大量の冷却水等が必要になり、エネルギー経済的に非常に不利になってくる。更に好ましくは5〜15℃の温度差が生じるように冷却することが好ましい。これにより、エネルギー消費はあまり必要とせず、安定した濃度のフェノールを回収できるため、工業的利点が高い。冷却が十分であった場合では、タンク2とタンク3では水とフェノールの分離は起きないが、外気温等でタンク2とタンク3で水とフェノールの分離が生じることがある。そこで、タンク2とタンク3のフェノール濃度と、水とフェノールの分離状況を簡易に測定できる方法を見いだし、本発明を完成するにいたった。 The phenol recovery method of the present invention includes, for example, a step of removing the resinous material by sedimentation (tank 1), a step of cooling to 30 ° C. or lower and sedimentation of phenol in the sedimentation tank (tank 2). The process of collecting and storing (tank 3) and the simple measurement of phenol concentration are combined. The lower the temperature of the tank 1 and the tank 2, the higher the concentration of recovered phenol, which is effective in use. Therefore, in the tank 1, it is preferable that the temperature is lowered to some extent by air cooling, and further the temperature is lowered by 2 to 30 ° C. at the stage of transfer to the tank 2. If it is 2 ° C or less, there is a possibility that the effect of cooling is small and the cost of the equipment is wasted. If it is 30 ° C or more, a large amount of cooling water is required, which is very disadvantageous in terms of energy economy. It becomes. More preferably, the cooling is preferably performed so that a temperature difference of 5 to 15 ° C. occurs. Thereby, energy consumption is not so much required, and a stable concentration of phenol can be recovered, which is an industrial advantage. When cooling is sufficient, separation of water and phenol does not occur in tank 2 and tank 3, but separation of water and phenol may occur in tank 2 and tank 3 due to outside air temperature or the like. Therefore, the present inventors have found a method capable of easily measuring the phenol concentration in tank 2 and tank 3 and the separation status of water and phenol, and completed the present invention.
本発明は、図1に示す水−フェノール2成分系の相互溶解度曲線温度に着目したことで、可能となったものであり、2相に分かれた点Aの水が溶媒となった飽和フェノール溶液と、点Bのフェノールが溶媒となった飽和水溶液の、電気伝導率の違いに着目した。タンク1で処理した回収フェノールは、タンク2へ移送中、30℃以下の任意の温度にする。これにより分離された回収フェノールのフェノール濃度は70重量%前後になる。しかし外気温によりタンク2とタンク3の温度が変動すると、タンク3での保管時において再分離を起こし、フェノール濃度が均一にならない。そこで、タンク2とタンク3において、回収フェノールの温度と電気導電率を測定することで、フェノール濃度を把握することができる。また、これらの測定値をコンピュータにフィードバックすることで、自動的に既知濃度の回収フェノールのみ、回収、使用することが可能となった。 The present invention has been made possible by paying attention to the mutual solubility curve temperature of the water-phenol binary system shown in FIG. 1, and a saturated phenol solution in which water of point A divided into two phases is used as a solvent. Attention was paid to the difference in electrical conductivity between saturated aqueous solutions in which the phenol at point B was the solvent. The recovered phenol treated in tank 1 is brought to an arbitrary temperature of 30 ° C. or lower during transfer to tank 2. The phenol concentration of the recovered phenol separated by this becomes around 70% by weight. However, if the temperature of the tank 2 and the tank 3 fluctuates due to the outside air temperature, re-separation occurs during storage in the tank 3, and the phenol concentration is not uniform. Therefore, the phenol concentration can be grasped by measuring the temperature and electric conductivity of the recovered phenol in the tank 2 and the tank 3. In addition, by feeding back these measured values to a computer, it becomes possible to automatically collect and use only a known concentration of recovered phenol.
次に本発明のフェノール回収装置について説明する。該フェノール回収装置はフェノール樹脂製造工程から排出される廃液を処理するタンク1と、熱交換器の後工程に位置するタンク2と、タンク3と、タンク2とタンク3のフェノール回収系に設置される温度計及び電気導電率計を備えるものである。 Next, the phenol recovery apparatus of the present invention will be described. The phenol recovery apparatus is installed in a tank 1 for treating waste liquid discharged from a phenol resin manufacturing process, a tank 2 located in a post-process of a heat exchanger, a tank 3, and a phenol recovery system of the tank 2 and the tank 3. A thermometer and an electric conductivity meter.
原料となる廃液は、フェノール樹脂製造工程の例えば脱水、濃縮工程から排出される廃液であって、フェノールを、5〜30重量%含有する。またこの廃液にはモノマーの他に若干ポリマーを含んでもよい。 The waste liquid used as a raw material is a waste liquid discharged from, for example, the dehydration and concentration process in the phenol resin production process, and contains 5 to 30% by weight of phenol. In addition to the monomer, the waste liquid may contain some polymer.
本発明の実施の形態におけるフェノール回収装置を、図2を参照して説明する。本実施の形態におけるフェノール回収装置は、図2に示すように濃縮釜1におけるフェノール樹脂合成後、縮合水を除去するため脱水濃縮工程に入る。本工程で生じる蒸発ベーパーをコンデンサー2で凝縮させ、その凝縮液(廃液)を受液槽4へ送り、フェノール回収を行う。廃液は受液槽4からタンク1(7)へ50〜80℃の廃液が移送されるが、20Hr放置すると廃液中の樹脂状物が底部へ沈降してくる。そこでこれを除去する。 A phenol recovery apparatus according to an embodiment of the present invention will be described with reference to FIG. As shown in FIG. 2, the phenol recovery apparatus in the present embodiment enters a dehydration and concentration step in order to remove condensed water after synthesizing the phenol resin in the concentration kettle 1. The evaporation vapor generated in this step is condensed by the condenser 2, and the condensed liquid (waste liquid) is sent to the liquid receiving tank 4 to recover phenol. As for the waste liquid, the waste liquid at 50 to 80 ° C. is transferred from the liquid receiving tank 4 to the tank 1 (7), but when left for 20 hours, the resinous material in the waste liquid settles to the bottom. Therefore, this is removed.
次いで、廃液は熱交換器9を介して定量ポンプ8にてタンク2(10)へ移送される。タンク2(10)ではフェノールが分離除去された上澄液がオーバーフローし、回収フェノールは底部より抜き出されるが、タンク2(10)底部に設置された公知の電気導電率計11で電気導電率が測定され、コンピュータ13で演算処理して表示器12で電気導電率が表示される。また予めコンピュータ13に設定した電気導電率により、遮断バルブ14を自動で開閉することで一定電気導電率以上の回収フェノールのみ、つまり一定のフェノール濃度の回収フェノールのみ、タンク3(15)へ抜き出される。一方、タンク2(10)の上部からオーバーフローした上澄液は、タンク1(7)へ再度移送される。
Next, the waste liquid is transferred to the tank 2 (10) by the metering pump 8 through the heat exchanger 9. In the tank 2 (10), the supernatant liquid from which phenol has been separated and removed overflows, and the recovered phenol is extracted from the bottom. The electric conductivity is measured by a known electric conductivity meter 11 installed at the bottom of the tank 2 (10). Is measured and processed by the
次いで、タンク3(15)に抜き出された回収フェノールは、プロセスで使用するまで保管されるが、温度条件が変動すると再び分離し、フェノール濃度がばらつくことになる。このため、タンク3(15)の底部に設置された電気導電率計16で電気導電率を測定し、コンピュータ18で演算処理して表示器17で電気導電率が表示され、またフェノール濃度異常警報装置によりプロセスで使用されないよう、送液ポンプ20の自動停止や、ブザー及びランプによる発報を行う。
Next, the recovered phenol extracted into the tank 3 (15) is stored until it is used in the process. However, when the temperature condition fluctuates, it is separated again and the phenol concentration varies. For this reason, the electrical conductivity is measured by the electrical conductivity meter 16 installed at the bottom of the tank 3 (15), and the
以下、本発明を実施例に基づき具体的に説明するが、単に例示であって本発明を制限するものではない。
(実施例1)
前記実施の形態におけるフェノール回収装置6を使用して、次のような実験を行った。すなわち、フェノール樹脂製造工程から排出されるフェノール濃度5〜30重量%の廃液を、タンク1(7)へは50〜80℃の温度で移送されるが、20Hr放置すると廃液中の不溶樹脂状物が底部へ沈降してくる。そこでこれを除去する。次いで、廃液は熱交換器9を介して定量ポンプ8にてタンク2(10)へ移送される。
実施例では、熱交換器9の入口で、36℃出口で22℃であった。タンク2(10)はフェノールを沈降分離させるもので、槽断面積はフェノールの沈降速度により一定以上の値を有するものが必要である。本実施例では供給液300kg/hrに対し2m2の断面積である。
EXAMPLES Hereinafter, although this invention is demonstrated concretely based on an Example, it is only an illustration and does not restrict | limit this invention.
Example 1
The following experiment was performed using the
In the examples, the temperature at the inlet of the heat exchanger 9 was 22 ° C. at the outlet of 36 ° C. The tank 2 (10) is for sedimentation and separation of phenol, and the tank cross-sectional area needs to have a certain value or more depending on the sedimentation speed of phenol. In this embodiment, the cross-sectional area is 2 m 2 with respect to 300 kg / hr of the supply liquid.
タンク2(10)ではフェノールが分離除去された上澄液がオーバーフローし、回収フェノールは底部より抜き出され、プロセスで使用するまでタンク3(15)に保管する。タンク3(15)ではフェノール濃度が70重量%前後になるが、保管時においても温度条件が変動し、冬場では約10℃まで低下する。そのため回収フェノールと水が再分離するが、タンク3(15)に設置した温度計と電気導電率計で測定すると、回収フェノールの温度が15℃となり、電気導電率は16.4μΩ/cmとなる。上部に分離した水の温度は15℃と同じあるが、電気導電率は1470μΩ/cmになり、水と回収フェノールの分離層が測定できる。 In the tank 2 (10), the supernatant liquid from which phenol has been separated and removed overflows, and the recovered phenol is extracted from the bottom and stored in the tank 3 (15) until it is used in the process. In the tank 3 (15), the phenol concentration is around 70% by weight, but the temperature condition fluctuates even during storage and falls to about 10 ° C. in winter. Therefore, the recovered phenol and water are separated again, but when measured with a thermometer and an electric conductivity meter installed in the tank 3 (15), the temperature of the recovered phenol is 15 ° C., and the electric conductivity is 16.4 μΩ / cm. . Although the temperature of the water separated at the top is the same as 15 ° C., the electric conductivity is 1470 μΩ / cm, and a separated layer of water and recovered phenol can be measured.
図1は水−フェノール2成分系の相互溶解度曲線温度を示す図で、本発明で温度によりフェノール濃度を簡易に解るようにし、また電気導電率で飽和フェノール溶液と飽和水溶液の分離状態を解るようにしたものである。 FIG. 1 is a graph showing the mutual solubility curve temperature of a water-phenol binary system. In the present invention, the phenol concentration is easily understood by the temperature, and the separation state of the saturated phenol solution and the saturated aqueous solution is understood by electric conductivity. It is a thing.
1 濃縮釜
2 コンデンサー
3 切替バルブ
4 受液槽
5 送液ポンプ
6 フェノール回収装置
7 第1沈降分離槽(タンク1)
8 定量ポンプ
9 熱交換器
10 第2沈降分離槽(タンク2)
11 電気導電率計
12 表示器
13 コンピュータ
14 遮断バルブ
15 回収フェノールタンク(タンク3)
16 電気導電率計
17 表示器
18 コンピュータ
19 フェノール濃度異常警報装置
20 送液ポンプ
DESCRIPTION OF SYMBOLS 1 Concentration pot 2 Condenser 3 Switching valve 4 Receiving tank 5
8 Metering pump 9
11
16
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JPS58104685A (en) * | 1981-12-15 | 1983-06-22 | Matsushita Electric Works Ltd | Method for separating and recovering waste liquid used for preparation of phenol resin |
JPS606628A (en) * | 1983-06-27 | 1985-01-14 | Hitachi Chem Co Ltd | Recovery of phenol from condensed water of phenolic resin synthesis process |
JPS63305116A (en) * | 1987-06-05 | 1988-12-13 | Aisin Chem Co Ltd | Reuse of concentrated solution formed in phenolic resin production |
JPH04334348A (en) * | 1991-05-09 | 1992-11-20 | Nippon Shokubai Co Ltd | Process for producing organic acid ester |
JPH10314764A (en) * | 1997-05-15 | 1998-12-02 | Teijin Ltd | Method for control of catalyst wet type oxidation treating device |
JPH11147093A (en) * | 1997-11-18 | 1999-06-02 | Teijin Ltd | Control method of catalytic wet oxidizing treatment apparatus |
JP2006122728A (en) * | 2004-10-26 | 2006-05-18 | Nippon Rensui Co Ltd | Apparatus, system and method for recovering waste water from rinser of aseptic filling equipment |
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JPS58104685A (en) * | 1981-12-15 | 1983-06-22 | Matsushita Electric Works Ltd | Method for separating and recovering waste liquid used for preparation of phenol resin |
JPS606628A (en) * | 1983-06-27 | 1985-01-14 | Hitachi Chem Co Ltd | Recovery of phenol from condensed water of phenolic resin synthesis process |
JPS63305116A (en) * | 1987-06-05 | 1988-12-13 | Aisin Chem Co Ltd | Reuse of concentrated solution formed in phenolic resin production |
JPH04334348A (en) * | 1991-05-09 | 1992-11-20 | Nippon Shokubai Co Ltd | Process for producing organic acid ester |
JPH10314764A (en) * | 1997-05-15 | 1998-12-02 | Teijin Ltd | Method for control of catalyst wet type oxidation treating device |
JPH11147093A (en) * | 1997-11-18 | 1999-06-02 | Teijin Ltd | Control method of catalytic wet oxidizing treatment apparatus |
JP2006122728A (en) * | 2004-10-26 | 2006-05-18 | Nippon Rensui Co Ltd | Apparatus, system and method for recovering waste water from rinser of aseptic filling equipment |
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