JPH10139695A - Production of diphenylmethane - Google Patents

Production of diphenylmethane

Info

Publication number
JPH10139695A
JPH10139695A JP26815897A JP26815897A JPH10139695A JP H10139695 A JPH10139695 A JP H10139695A JP 26815897 A JP26815897 A JP 26815897A JP 26815897 A JP26815897 A JP 26815897A JP H10139695 A JPH10139695 A JP H10139695A
Authority
JP
Japan
Prior art keywords
catalyst
diphenylethane
reaction
hydrogen
water
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
Application number
JP26815897A
Other languages
Japanese (ja)
Inventor
Hideyuki Doi
英幸 土肥
Kazuo Sakamoto
一夫 坂本
Tadashi Tayanagi
正 田柳
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.)
Eneos Corp
Original Assignee
Nippon Petrochemicals Co Ltd
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 Nippon Petrochemicals Co Ltd filed Critical Nippon Petrochemicals Co Ltd
Priority to JP26815897A priority Critical patent/JPH10139695A/en
Publication of JPH10139695A publication Critical patent/JPH10139695A/en
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/08—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule
    • C07C4/12—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by splitting-off an aliphatic or cycloaliphatic part from the molecule from hydrocarbons containing a six-membered aromatic ring, e.g. propyltoluene to vinyltoluene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/46—Ruthenium, rhodium, osmium or iridium

Abstract

PROBLEM TO BE SOLVED: To obtain the subject compound useful as an intermediate for various chemicals in high yield and selectivity by reacting diphenylethane with hydrogen and water in the presence of a metallic catalyst or a metal oxide catalyst. SOLUTION: The objective compound is produced by reacting 1,1 diphenylethane with hydrogen, water or their mixture at 250700 deg.C under atmospheric pressure to 100kg/cm<2> while supplying about 1-30mol of hydrogen and water in total based on 1mol of diphenylethane. The metallic catalyst to be used in the reaction is preferably a noble metal catalyst containing Rh and/or Pd. The metal is supported on a basic or weakly acidic carrier in an amount of 0.001-10wt.% based on the whole catalyst. The metal oxide catalyst is preferably an oxide of an alkali metal or alkaline earth metal such as Na or Ca. A strongly acidic solid acid catalyst such as zeolite is unfavorable because such catalyst is liable to induce a decomposition reaction.

Description

【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION

【０００１】[0001]

【発明の属する技術分野】本発明は各種化学品の中間体
として有用なジフェニルメタンの製造方法に関するもの
である。TECHNICAL FIELD The present invention relates to a method for producing diphenylmethane, which is useful as an intermediate for various chemicals.

【０００２】[0002]

【従来技術】例えば、工業化学雑誌、72〔7〕(1969) p.
1512−1515 には、１,１−ジフェニルエタンを単独で
加熱してジフェニルメタンを得る方法が記載されてい
る。しかしながら、その生成物は、水素化分解による生
成物と考えられるベンゼンやエチルベンゼン、脱水素化
による生成物と考えられる１,１−ジフェニルエチレ
ン、および分解物であるスチレンなどが主成分であり、
ジフェニルメタンの生成はごく僅かである。[Prior Art] For example, Industrial Chemistry Magazine, 72 [7] (1969) p.
1512-1515 describes a method for obtaining diphenylmethane by heating 1,1-diphenylethane alone. However, the main components of the product are benzene and ethylbenzene, which are considered to be products of hydrogenolysis, 1,1-diphenylethylene, which is considered to be a product of dehydrogenation, and styrene, which is a decomposition product.
The production of diphenylmethane is negligible.

【０００３】[0003]

【発明が解決しようとする課題】本発明は、１,１−ジ
フェニルエタンから良好な収率および選択率で、ジフェ
ニルメタンを反応の主生成物として製造する方法を提供
することを目的とする。The object of the present invention is to provide a process for producing diphenylmethane as the main product of the reaction from 1,1-diphenylethane in good yield and selectivity.

【０００４】[0004]

【課題を解決するための手段】本発明者らは、上記の目
的に沿って１,１−ジフェニルエタンを出発原料とする
ジフェニルメタンの合成法を鋭意研究した結果、水素お
よび／または水と反応させることが有用であることを見
出して本発明を完成した。すなわち、本発明の第１は、
１,１−ジフェニルエタンと水素および／または水とを
反応させることを特徴とするジフェニルメタンの製造方
法に関する。また本発明の第２は、上記本発明の第１に
おいて、反応を金属触媒および／または金属酸化物触媒
の存在下に行うことを特徴とするジフェニルメタンの製
造方法に関する。Means for Solving the Problems The inventors of the present invention have made intensive studies on a method for synthesizing diphenylmethane using 1,1-diphenylethane as a starting material in accordance with the above-mentioned objects. The present invention has been completed by finding that is useful. That is, the first of the present invention is:
The present invention relates to a method for producing diphenylmethane, comprising reacting 1,1-diphenylethane with hydrogen and / or water. A second aspect of the present invention relates to the method for producing diphenylmethane according to the first aspect of the present invention, wherein the reaction is carried out in the presence of a metal catalyst and / or a metal oxide catalyst.

【０００５】以下、本発明をさらに詳しく説明する。本
発明における出発原料は１,１−ジフェニルエタンであ
るが、１,１−ジフェニルエタンを５０重量％以上含む
炭化水素原料も本発明の出発原料とすることができる。
上記１,１−ジフェニルエタンは、各種化学プロセスに
おいて副生することが知られており、例えばベンゼンと
エチレンとの反応によりエチルベンゼンを製造するプロ
セスから副生する重質物には、１,１−ジフェニルエタ
ンが５０重量％以上含まれている。このような副生油
は、本発明の反応原料として好ましいものである。本発
明においては、１,１−ジフェニルエタンに、水素、水
またはこれらの混合物を反応させる。１,１−ジフェニ
ルエタン単独では、たとえ触媒を使用しても、前記文献
に記載されているようにジフェニルメタンの生成はごく
僅かである。反応生成物のガス分析から、本発明の方法
において、１,１−ジフェニルエタンと水素との反応は
下記化１のように進行すると考えられる。Hereinafter, the present invention will be described in more detail. The starting material in the present invention is 1,1-diphenylethane, but a hydrocarbon raw material containing 50% by weight or more of 1,1-diphenylethane can also be used as the starting material in the present invention.
It is known that 1,1-diphenylethane is a by-product in various chemical processes. For example, 1,1-diphenylethane is a by-product of the reaction between benzene and ethylene to produce ethylbenzene. Ethane is contained in an amount of 50% by weight or more. Such a by-product oil is preferable as the reaction raw material of the present invention. In the present invention, 1,1-diphenylethane is reacted with hydrogen, water or a mixture thereof. With 1,1-diphenylethane alone, even with the use of a catalyst, the production of diphenylmethane is negligible, as described in the literature. From the gas analysis of the reaction product, it is considered that the reaction between 1,1-diphenylethane and hydrogen in the method of the present invention proceeds as shown in the following chemical formula 1.

【０００６】[0006]

【化１】 Embedded image

【０００７】また、１,１−ジフェニルエタンと水との
反応は下記化２のように進行すると考えられる。また、
生成する水素により上記化１の反応も併発する。The reaction between 1,1-diphenylethane and water is considered to proceed as shown in the following chemical formula 2. Also,
The reaction of the above chemical formula 1 occurs simultaneously with the generated hydrogen.

【０００８】[0008]

【化２】 Embedded image

【０００９】１,１−ジフェニルエタンと水素、水また
はそれらの混合物との供給組成比は、モル換算で１,１
−ジフェニルエタン１に対し、水素と水との合計として
通常１〜３０程度が選ばれる。上記モル比が１未満で
は、転化率が低かったり、副反応が多く発生するなどの
傾向が見られる。モル比が３０を超えると、水素や水を
増量する割には反応率の向上が見られないため不経済で
ある。反応温度は２５０〜７００℃の範囲とすることが
好ましい。２５０℃未満では極端に反応速度が遅くな
り、７００℃を超えると分解反応などの副反応が多くな
り、いずれも好ましくない。反応圧力は常圧から高圧、
例えば１００kg/cm2まで任意に選択することができる。
好ましくは系内が気相を保つような温度と圧力に設定す
る。The supply composition ratio of 1,1-diphenylethane to hydrogen, water or a mixture thereof is 1.1, in terms of mole.
Usually, about 1 to about 30 is selected as the sum of hydrogen and water with respect to 1-diphenylethane. When the molar ratio is less than 1, there is a tendency that the conversion rate is low and that many side reactions occur. When the molar ratio exceeds 30, it is uneconomical because no improvement in the reaction rate is seen for increasing the amount of hydrogen or water. The reaction temperature is preferably in the range of 250 to 700 ° C. If the temperature is lower than 250 ° C., the reaction rate becomes extremely slow. If the temperature exceeds 700 ° C., side reactions such as a decomposition reaction increase, and both are not preferable. Reaction pressure is from normal pressure to high pressure,
For example, it can be arbitrarily selected up to 100 kg / cm 2 .
Preferably, the temperature and pressure are set so that the inside of the system keeps the gas phase.

【００１０】反応は、金属、金属酸化物またはこれらの
混合物を含む触媒の存在下で行うことが好ましい。金属
酸化物は、塩基性ないし弱酸性を呈することが好まし
い。触媒としては、種々の金属または金属酸化物を利用
することができる。例えば、金属触媒としては、Ｃo、
Ｒh、Ｉr、Ｎi、Ｐd、Ｐt、Ｒe、Ｒu 等の金属またはこ
れらの混合物が例示される。好ましくは貴金属触媒であ
る。さらに好ましくは Ｒh、Ｐd またはその両方を含
む触媒である。金属触媒を用いる場合は、常法により塩
基性ないし弱酸性を呈する担体、例えば、ＳiＯ2、Ｔi
Ｏ2、Ａl2Ｏ3などに担持させることができる。担持量
は、金属の重量換算で触媒全体に対して０.００１〜１
０重量％の範囲が好ましい。また、金属酸化物触媒とし
ては、例えば、ＣoＯ、ＢeＯ、ＮiＯ、ＣaＯ、Ｎa2Ｏ、
Ｋ2Ｏ、ＵＯ3、Ｃr2Ｏ3、Ｆe2Ｏ3、ＳiＯ2、ＴiＯ2、Ａ
l2Ｏ3等の金属酸化物またはその混合物が例示される。
好ましくはアルカリ金属もしくはアルカリ土類金属の酸
化物またはこれらの混合物である。さらに好ましくはＮ
a もしくはＣa の酸化物またはこれらの混合物を含む触
媒である。なお、本発明の方法において触媒を用いる場
合に、シリカ・アルミナやゼオライトなどの強い酸性を
有する固体酸触媒は、水素、水またはこれらの混合物を
共存させた場合でも分解反応が多く生起するので好まし
くない。The reaction is preferably carried out in the presence of a catalyst containing a metal, a metal oxide or a mixture thereof. The metal oxide preferably exhibits basic or weak acidity. Various metals or metal oxides can be used as the catalyst. For example, as a metal catalyst, Co,
Examples thereof include metals such as Rh, Ir, Ni, Pd, Pt, Re, and Ru, and mixtures thereof. Preferably, it is a noble metal catalyst. More preferred is a catalyst containing Rh, Pd or both. When a metal catalyst is used, a basic or weakly acidic carrier such as SiO 2 , Ti
It can be carried on O 2 , Al 2 O 3 or the like. The supported amount is 0.001 to 1 with respect to the entire catalyst in terms of metal weight.
A range of 0% by weight is preferred. Examples of the metal oxide catalyst include CoO, BeO, NiO, CaO, Na 2 O,
K 2 O, UO 3 , Cr 2 O 3 , Fe 2 O 3 , SiO 2 , TiO 2 , A
Examples thereof include metal oxides such as l 2 O 3 and mixtures thereof.
Preferable is an oxide of an alkali metal or an alkaline earth metal or a mixture thereof. More preferably N
A catalyst containing an oxide of a or Ca or a mixture thereof. In the case where a catalyst is used in the method of the present invention, a solid acid catalyst having strong acidity such as silica-alumina or zeolite is preferably used because a large amount of decomposition reaction occurs even when hydrogen, water or a mixture thereof is used. Absent.

【００１１】反応様式としては、回分式および連続式の
いずれも用いることができる。連続式においては、固定
床および流動床のいずれの場合でも、所定の温度および
圧力に保った反応器に、１,１−ジフェニルエタンと
水、水素またはこれらの混合物とを供給することにより
反応を行う。１,１−ジフェニルエタンの液空間速度
は、 ０.１〜５０hr-1の範囲から選択することができ
る。また連続式の場合は、通常反応器出口をコールドト
ラップに接続し、反応生成物を凝縮させて回収すること
が望ましい。As a reaction mode, any of a batch system and a continuous system can be used. In the continuous method, the reaction is carried out by supplying 1,1-diphenylethane and water, hydrogen or a mixture thereof to a reactor maintained at a predetermined temperature and pressure in both a fixed bed and a fluidized bed. Do. The liquid hourly space velocity of 1,1-diphenylethane can be selected from the range of 0.1 to 50 hr -1 . In the case of a continuous system, it is usually desirable to connect the outlet of the reactor to a cold trap to condense and collect the reaction product.

【００１２】[0012]

【発明の実施の形態】次に、実施例により本発明をさら
に詳しく説明する。Next, the present invention will be described in more detail by way of examples.

【実施例】いずれも、加熱装置を有する内径２５ｍｍの
ステンレス鋼製反応管に触媒３０ｍｌを充填し、所定量
の反応原料を連続的に送入する方法により反応を行なっ
た。反応生成物の同定はマススペクトロメトリーにより
行い、定量分析は長さ５０ｍのキャピラリーカラム（Ｏ
Ｖ−１）を取り付けたガスクロマトグラフィーにより行
なった。なお、以下の実施例において、１,１−ジフェ
ニルエタンおよび水の供給流量（ml/hr）は常温の液体
として、また水素の供給流量（ml/min）は標準状態に換
算して表示した。EXAMPLES In all cases, a reaction was carried out by a method in which 30 ml of a catalyst was filled in a stainless steel reaction tube having an inner diameter of 25 mm having a heating device, and a predetermined amount of a reaction material was continuously fed. The reaction product was identified by mass spectrometry, and the quantitative analysis was performed by a 50 m long capillary column (O
This was performed by gas chromatography equipped with V-1). In the following examples, the supply flow rate (ml / hr) of 1,1-diphenylethane and water was shown as a liquid at room temperature, and the supply flow rate of hydrogen (ml / min) was converted to a standard state.

【００１３】＜実施例１＞市販の０.５wt％Ｒh／アルミ
ナペレット（エヌ・イー ケムキャット(株)製）を破砕
し、粒径を０.３５〜１ｍｍに揃えて反応管に充填し、
温度４５１℃、圧力１atm において、１,１−ジフェニ
ルエタン（ＤＰＥ）を３０ml/hr、水素を３７０ml/min
の流量でそれぞれ供給した。コールドトラップに回収さ
れた反応液の分析を行なった。反応条件およびジフェニ
ルメタンの収率を表１に示す。<Example 1> A commercially available 0.5 wt% Rh / alumina pellet (manufactured by NE Chemcat Co., Ltd.) was crushed, the particle size was adjusted to 0.35 to 1 mm, and the reaction tube was filled.
At a temperature of 451 ° C. and a pressure of 1 atm, 1,1-diphenylethane (DPE) is 30 ml / hr and hydrogen is 370 ml / min.
Were supplied at the respective flow rates. The reaction solution collected in the cold trap was analyzed. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１４】＜実施例２＞市販の０.５wt％Ｒh／アルミ
ナペレット（エヌ・イー ケムキャット(株)製）を実施
例１と同様に破砕して反応管に充填し、温度５０４℃、
圧力１２atm において、１,１−ジフェニルエタンを２
９.２ml/hr、水を２４.０ml/hr の流量でそれぞれ供給
した。コールドトラップに回収された水以外の反応液の
分析を行なった。反応条件およびジフェニルメタンの収
率を表１に示す。<Example 2> A commercially available 0.5 wt% Rh / alumina pellet (manufactured by NE Chemcat Co., Ltd.) was crushed in the same manner as in Example 1 and charged into a reaction tube.
At a pressure of 12 atm, 1,1-diphenylethane is
9.2 ml / hr and water were supplied at a flow rate of 24.0 ml / hr, respectively. The reaction solution other than water collected in the cold trap was analyzed. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１５】＜実施例３＞市販の１０wt％Ｎa2Ｏ／アル
ミナペレット（商品名：Ｇ−９２、日産ガードラー触媒
(株)製）を実施例１と同様に破砕して反応管に充填し、
温度６４８℃、圧力１atm において、１,１−ジフェニ
ルエタンを３０ml/hr、水を１７.５ml/hrの流量でそれ
ぞれ供給した。反応管出口を冷水で凝縮し分析を行なっ
た。反応条件およびジフェニルメタンの収率を表１に示
す。Example 3 Commercially available 10 wt% Na 2 O / alumina pellets (trade name: G-92, Nissan Gardler Catalyst)
Was crushed in the same manner as in Example 1 and filled in a reaction tube.
At a temperature of 648 ° C. and a pressure of 1 atm, 1,1-diphenylethane was supplied at a flow rate of 30 ml / hr and water was supplied at a flow rate of 17.5 ml / hr. The reaction tube outlet was condensed with cold water and analyzed. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１６】＜実施例４＞市販のシリカ・カルシア（Ｓ
iＯ2/ＣaＯ重量％比＝６４/２４；商品名：Ｎ−６６１
Ｂ、日揮化学(株)製）を破砕し、粒径を０.３５〜１.５
ｍｍに揃えて反応管に充填し、温度５９８℃、圧力１at
m において、１,１−ジフェニルエタンを３０ml/hr、水
素を３７０ml/min の流量でそれぞれ供給した。コール
ドトラップに回収された反応液の分析を行なった。反応
条件およびジフェニルメタンの収率を表１に示す。Example 4 Commercially available silica calcia (S
iO 2 / CaO wt% ratio = 64/24; trade name: N-661
B, manufactured by JGC Chemicals Co., Ltd.) and the particle size is 0.35 to 1.5.
mm, filled in a reaction tube, temperature 598 ° C, pressure 1at
At m 2, 1,1-diphenylethane and hydrogen were supplied at a flow rate of 30 ml / hr and 370 ml / min, respectively. The reaction solution collected in the cold trap was analyzed. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１７】＜実施例５＞実施例４で用いたシリカ・カ
ルシアに、常法によりＰd を０.５重量％担持させて触
媒とした。この触媒を破砕し、粒径を０.３５〜１.５ｍ
ｍに揃えて反応管に充填し、温度６００℃、圧力１１at
m において、１,１−ジフェニルエタンを３０.５ml/h、
水素を１４０ml/min の流量でそれぞれ供給した。反応
条件およびジフェニルメタンの収率を表１に示す。Example 5 A catalyst was prepared by loading Pd on the silica / calcia used in Example 4 in a conventional manner at 0.5% by weight. This catalyst is crushed to have a particle size of 0.35 to 1.5 m.
m, filled in a reaction tube, temperature 600 ° C, pressure 11at
m, 30.5 ml / h of 1,1-diphenylethane,
Hydrogen was supplied at a flow rate of 140 ml / min. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１８】＜比較例１〜３＞実施例１の装置を用い、
比較例１では無触媒で、比較例２および３では市販のシ
リカ・アルミナ触媒を用い、水や水素を使用せず、その
他は実施例１と同様にして１,１−ジフェニルエタンを
供給し反応を行った。反応条件およびジフェニルメタン
の収率を表１に示す。<Comparative Examples 1 to 3> Using the apparatus of Example 1,
Comparative Example 1 used no catalyst, Comparative Examples 2 and 3 used a commercially available silica-alumina catalyst, did not use water or hydrogen, and supplied 1,1-diphenylethane in the same manner as in Example 1 for the reaction. Was done. Table 1 shows the reaction conditions and the yield of diphenylmethane.

【００１９】[0019]

【表１】 [Table 1]

【００２０】[0020]

【発明の効果】本発明の方法によれば、１,１−ジフェ
ニルエタンに水素または水を反応させることにより、ベ
ンゼンやエチルベンゼンなどを生成させる水素化分解反
応、１,１−ジフェニルエチレンなどを生成させる脱水
素反応、スチレンなどを生成させる分解反応などを減少
させ、ジフェニルメタンを反応の主生成物として得るこ
とが可能である。According to the method of the present invention, 1,1-diphenylethane is reacted with hydrogen or water to produce a hydrogenolysis reaction for producing benzene, ethylbenzene or the like, thereby producing 1,1-diphenylethylene or the like. Thus, diphenylmethane can be obtained as a main product of the reaction by reducing the dehydrogenation reaction to occur and the decomposition reaction to produce styrene and the like.

───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ // Ｃ０７Ｂ 61/00 ３００ Ｃ０７Ｂ 61/00 ３００ ──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 6 Identification symbol FI // C07B 61/00 300 C07B 61/00 300

Claims (2)

【特許請求の範囲】[Claims] 【請求項１】 １,１−ジフェニルエタンと水素および
／または水とを反応させることを特徴とするジフェニル
メタンの製造方法。1. A method for producing diphenylmethane, comprising reacting 1,1-diphenylethane with hydrogen and / or water. 【請求項２】 前記反応を金属触媒および／または金属
酸化物触媒の存在下に行うことを特徴とする請求項１に
記載のジフェニルメタンの製造方法。2. The method for producing diphenylmethane according to claim 1, wherein the reaction is performed in the presence of a metal catalyst and / or a metal oxide catalyst.
JP26815897A 1996-09-12 1997-09-12 Production of diphenylmethane Pending JPH10139695A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP26815897A JPH10139695A (en) 1996-09-12 1997-09-12 Production of diphenylmethane

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP26552096 1996-09-12
JP8-265520 1996-09-12
JP26815897A JPH10139695A (en) 1996-09-12 1997-09-12 Production of diphenylmethane

Publications (1)

Publication Number Publication Date
JPH10139695A true JPH10139695A (en) 1998-05-26

Family

ID=26547011

Family Applications (1)

Application Number Title Priority Date Filing Date
JP26815897A Pending JPH10139695A (en) 1996-09-12 1997-09-12 Production of diphenylmethane

Country Status (1)

Country Link
JP (1) JPH10139695A (en)

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