JPH04208237A - Production of nucleus-substituted chlorinated toluene - Google Patents
Production of nucleus-substituted chlorinated tolueneInfo
- Publication number
- JPH04208237A JPH04208237A JP2334979A JP33497990A JPH04208237A JP H04208237 A JPH04208237 A JP H04208237A JP 2334979 A JP2334979 A JP 2334979A JP 33497990 A JP33497990 A JP 33497990A JP H04208237 A JPH04208237 A JP H04208237A
- Authority
- JP
- Japan
- Prior art keywords
- catalyst
- magnesia
- toluene
- mct
- reaction
- 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
- 150000003613 toluenes Chemical class 0.000 title claims description 14
- 238000004519 manufacturing process Methods 0.000 title claims description 9
- 239000003054 catalyst Substances 0.000 claims abstract description 26
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 20
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 9
- NPDACUSDTOMAMK-UHFFFAOYSA-N 4-Chlorotoluene Chemical compound CC1=CC=C(Cl)C=C1 NPDACUSDTOMAMK-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 abstract description 21
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 14
- 239000000460 chlorine Substances 0.000 abstract description 14
- 229910052801 chlorine Inorganic materials 0.000 abstract description 14
- 239000007795 chemical reaction product Substances 0.000 abstract description 9
- 239000002994 raw material Substances 0.000 abstract description 5
- 150000001875 compounds Chemical class 0.000 abstract description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 2
- 239000003905 agrochemical Substances 0.000 abstract description 2
- 239000003814 drug Substances 0.000 abstract description 2
- 229940079593 drug Drugs 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 239000011777 magnesium Substances 0.000 abstract description 2
- 229910052749 magnesium Inorganic materials 0.000 abstract description 2
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 abstract description 2
- 239000001095 magnesium carbonate Substances 0.000 abstract description 2
- 229910000021 magnesium carbonate Inorganic materials 0.000 abstract description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 abstract description 2
- 239000000347 magnesium hydroxide Substances 0.000 abstract description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 abstract description 2
- 238000001354 calcination Methods 0.000 abstract 1
- 235000014380 magnesium carbonate Nutrition 0.000 abstract 1
- 235000012254 magnesium hydroxide Nutrition 0.000 abstract 1
- 238000005406 washing Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- RYMMNSVHOKXTNN-UHFFFAOYSA-N 1,3-dichloro-5-methyl-benzene Natural products CC1=CC(Cl)=CC(Cl)=C1 RYMMNSVHOKXTNN-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- WYUIWKFIFOJVKW-UHFFFAOYSA-N 1,2-dichloro-4-methylbenzene Chemical compound CC1=CC=C(Cl)C(Cl)=C1 WYUIWKFIFOJVKW-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CAHQGWAXKLQREW-UHFFFAOYSA-N Benzal chloride Chemical compound ClC(Cl)C1=CC=CC=C1 CAHQGWAXKLQREW-UHFFFAOYSA-N 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- XEMRAKSQROQPBR-UHFFFAOYSA-N (trichloromethyl)benzene Chemical compound ClC(Cl)(Cl)C1=CC=CC=C1 XEMRAKSQROQPBR-UHFFFAOYSA-N 0.000 description 1
- DMEDNTFWIHCBRK-UHFFFAOYSA-N 1,3-dichloro-2-methylbenzene Chemical compound CC1=C(Cl)C=CC=C1Cl DMEDNTFWIHCBRK-UHFFFAOYSA-N 0.000 description 1
- KFAKZJUYBOYVKA-UHFFFAOYSA-N 1,4-dichloro-2-methylbenzene Chemical compound CC1=CC(Cl)=CC=C1Cl KFAKZJUYBOYVKA-UHFFFAOYSA-N 0.000 description 1
- IBSQPLPBRSHTTG-UHFFFAOYSA-N 1-chloro-2-methylbenzene Chemical compound CC1=CC=CC=C1Cl IBSQPLPBRSHTTG-UHFFFAOYSA-N 0.000 description 1
- OSOUNOBYRMOXQQ-UHFFFAOYSA-N 1-chloro-3-methylbenzene Chemical compound CC1=CC=CC(Cl)=C1 OSOUNOBYRMOXQQ-UHFFFAOYSA-N 0.000 description 1
- FUNUTBJJKQIVSY-UHFFFAOYSA-N 2,4-Dichlorotoluene Chemical compound CC1=CC=C(Cl)C=C1Cl FUNUTBJJKQIVSY-UHFFFAOYSA-N 0.000 description 1
- 238000005727 Friedel-Crafts reaction Methods 0.000 description 1
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 description 1
- 229940073608 benzyl chloride Drugs 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001640 fractional crystallisation Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 229940031958 magnesium carbonate hydroxide Drugs 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- -1 trichlorotoluene Chemical class 0.000 description 1
- 239000002699 waste material Substances 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
Description
【発明の詳細な説明】
イ）発明の目的
〔産業上の利用分野〕
本発明は、トルエン（以下、Ｔ、ＯＬと省略）および／
またはモノクロロトルエン（以下、ＭＣＴと省略）を塩
素化し、核置換塩素化トルエンを製造する方法に関する
ものである。Detailed Description of the Invention A) Purpose of the Invention [Industrial Application Field] The present invention provides toluene (hereinafter abbreviated as T and OL) and/or
Alternatively, the present invention relates to a method for producing nuclear-substituted chlorinated toluene by chlorinating monochlorotoluene (hereinafter abbreviated as MCT).
核置換塩素化トルエンは工業的に重要な化合物であり、
医薬、農薬の原料として用いられている。Nuclear-substituted chlorinated toluene is an industrially important compound;
It is used as a raw material for medicines and agricultural chemicals.
特にＭＣ，Ｔあるいはジクロロトルエン（以下、ＤＣ，
Ｔと省略）は有用であり、ＭＣＴには、オルソクロロト
ルエン、メタクロロトルエン、パラクロロトルエンの３
種の異性体か、ＤＣＴには、２゜３−ジクロロトルエン
、２，４−ジクロロトルエン、２，５−ジクロロ・トル
エン、２，６−ジクロロトルエン、３，４−ジクロロト
ルエン、３，５−ジクロロトルエンの６種の異性体が存
在する。In particular, MC, T or dichlorotoluene (hereinafter referred to as DC,
(abbreviated as T) is useful, and MCTs include orthochlorotoluene, metachlorotoluene, and parachlorotoluene.
Species isomers, DCT include 2゜3-dichlorotoluene, 2,4-dichlorotoluene, 2,5-dichlorotoluene, 2,6-dichlorotoluene, 3,4-dichlorotoluene, 3,5-dichlorotoluene, There are six isomers of dichlorotoluene.
従来、核置換塩素化トルエンは、塩化第二鉄等のフリー
デルクラフト型触媒を用い、ＴＯＬを塩素化して製造し
ている。・
一般に、塩化第二鉄を触媒、とする反応では、トリクロ
ロトルエン等の高次核置換塩素化トルエンの副生が多く
、工業的に有用であるＭＣＴ、ＤＣＴの収率の低下の原
因となっている。また、この触媒は反応生成物に均一に
溶解するため、反応生成物から触媒を除去するための水
洗工程、水洗後の反応生成物の脱水工程か必要であり、
更に水洗工程において触媒か水和物となるため、触媒の
再利用か不可能となる等の問題かあり、操作か複雑で１
．経済的に不利であった。Conventionally, nuclear-substituted chlorinated toluene has been produced by chlorinating TOL using a Friedel-Crafts type catalyst such as ferric chloride. - In general, reactions using ferric chloride as a catalyst produce many by-products of highly substituted chlorinated toluenes such as trichlorotoluene, which causes a decrease in the yield of MCT and DCT, which are industrially useful. ing. In addition, since this catalyst is uniformly dissolved in the reaction product, a water washing step is required to remove the catalyst from the reaction product, and a dehydration step for the reaction product after water washing is necessary.
Furthermore, since the catalyst becomes a hydrate in the water washing process, there are problems such as the reuse of the catalyst becomes impossible, and the operation is complicated.
．． It was economically disadvantageous.
本発明者らは、高次核置換塩素化トルエンの生成を抑制
し、Ｍ（：Ｔ、ｎ）ＣＴの収率を実質的に高め、更に触
媒が反応生成物に溶解せず、目的物の取得が効率的で経
済的な核置換塩素化トルエンの製造方法について鋭意研
究した結果、本発明を完成した。The present inventors suppressed the production of highly substituted chlorinated toluene, substantially increased the yield of M(:T,n)CT, and furthermore, the catalyst was not dissolved in the reaction product and the target product was obtained. The present invention was completed as a result of intensive research into a method for producing nuclear-substituted chlorinated toluene that is efficient and economical to obtain.
口）発明の構成
〔課題を解決するための手段〕
本発明はＴＯＬおよび／またはＭＣＴを塩素化して核置
換塩素化トルエンを製造するに際し、触媒としてマグネ
シアを用い、液相て塩素化することを特徴とする核置換
塩素化トルエンの製造方法である。(1) Structure of the invention [Means for solving the problem] The present invention involves using magnesia as a catalyst and chlorinating in the liquid phase when producing nuclear-substituted chlorinated toluene by chlorinating TOL and/or MCT. This is a characteristic method for producing nuclear-substituted chlorinated toluene.
本発明において、触媒として使用するマグネシアは、軽
焼マグネシアか好適であり、炭酸マグネシウム、水酸化
マグネシウムを力焼己て製造したもの、金属マグネシウ
ムを空気中で加熱し製造したもの等を用いればよい。In the present invention, the magnesia used as a catalyst is preferably lightly calcined magnesia, and those produced by force-burning magnesium carbonate or magnesium hydroxide, those produced by heating metallic magnesium in air, etc. may be used. .
触媒の形状は反応の方式によって任意に選択することか
でき、粉末状、顆粒状、球状、筒状、環状等の形状の触
媒が使用可能である。マグネシアの形状及び大きさは反
応結果に本質的な影響を余り与えない。The shape of the catalyst can be arbitrarily selected depending on the reaction method, and catalysts in powder, granule, spherical, cylindrical, annular, etc. shapes can be used. The shape and size of magnesia have little essential influence on the reaction results.
本発明の反応は液相反応であり、回分式および連続式の
いずれの方法でも行うことか中米る。回分式では、例え
ば、触媒をＴＯＬまたはＭＣＴに懸濁させ、塩素ガスを
供給することにより実施できる。連続式反応は、例えば
、触媒を充填した反応塔にＴＯＬまたはＭＣＴおよび塩
素を流通させることにより実施できる。塩素は窒素等の
不活性ガスで希釈して用いてもよい。The reaction of the present invention is a liquid phase reaction and can be carried out either batchwise or continuously. The batch method can be carried out, for example, by suspending the catalyst in TOL or MCT and supplying chlorine gas. The continuous reaction can be carried out, for example, by flowing TOL or MCT and chlorine through a reaction tower packed with a catalyst. Chlorine may be used after being diluted with an inert gas such as nitrogen.
塩素の反応系への供給割合は、反応温度、ＴＯ′Ｌまた
はＭＣＴと触媒の比率なとによって最適範囲か決定され
るか、０． ００１〜’Ｉｍｏｌ ’／ｇ−ｃａｔ’ｈ
ｒか好ましく、更に好ましい割合は、００１〜０． １
ｍｏｌ ７ｇ−ｃａｔ−ｈｒである。０００１ ｍｏｌ
／ ｇ−ｃａｔ −ｈｒ未満ては、塩素転化率は１
００％となるか、工業的見地からすると非能率的であり
、所要の生産量を得ようとすれば、装置が大型となるの
で好ましいとはいえない。又、１ｍｏｌ ７ｇ−ｃａｔ
−ｈｒを超えると、未反応塩素が増加し、廃液処理
費用も嵩み、経済的とはいえない。The rate of supply of chlorine to the reaction system is determined by the reaction temperature, TO'L, or the ratio of MCT to catalyst, or is within an optimal range. 001~'Imol'/g-cat'h
r is preferable, and the more preferable ratio is 001 to 0. 1
mol 7g-cat-hr. 0001 mol
/ g-cat -hr, the chlorine conversion rate is 1
00%, which is inefficient from an industrial standpoint and requires a large-sized device to obtain the required production volume, which is not desirable. Also, 1mol 7g-cat
If it exceeds -hr, unreacted chlorine increases and waste liquid treatment costs also increase, making it uneconomical.
原料であるＴＯＬまたはＭＣＴの反応系への供給量は、
回分式の場合はマグネシア１．Ｏｇｒ当り、０．０５〜
ｌ Ｏｍｏｌ’、が好ましく、更に好ましい上限値は１
ｍｏｌである。ｏ、ｏｓｍｏｔ未満では、使用触媒量に
比較して原料供給量が少ないため非能率的であり、１０
ｍｏｌを超えると、触媒の負荷か大きくなり、十分な塩
素転化率が得られない。連続式による場合のＴＣ）Ｌま
たはＭＣ’Ｔの供給量は、好ましくは０． ０”ＯＬ〜
１ｍｏｌ ７ｇ −ｃａｔ −ｈｒ、更に好ましくは０
． ０１〜０．１ｍｏｌ ７ｇ −ｃａｔ・ｈｒである
。０． ００１’ｍｏｌ ／ ｇ −ｃａｔ ’ｈｒ
未満では、回分式同様、非能率的であり、Ｉｍｏｌ／ｇ
−ｃａｔ −ｈｒを超えると、触媒の負荷が大きくな
り、十分な塩素転化率が得られない。The amount of raw material TOL or MCT supplied to the reaction system is
For batch type, magnesia 1. Per Ogr, 0.05 ~
l Omol', is preferable, and the more preferable upper limit is 1
It is mol. If it is less than 10 osmot, it is inefficient because the amount of raw material supplied is small compared to the amount of catalyst used.
If it exceeds mol, the load on the catalyst becomes large and a sufficient chlorine conversion rate cannot be obtained. In the continuous system, the supply amount of TC)L or MC'T is preferably 0. 0"OL~
1mol 7g-cat-hr, more preferably 0
．． 01-0.1 mol 7g-cat·hr. 0. 001'mol/g-cat'hr
If it is less than Imol/g, it is inefficient like the batch method, and
If -cat -hr is exceeded, the load on the catalyst becomes large and a sufficient chlorine conversion rate cannot be obtained.
本発明における塩素の、ＴＯＬまたはＭ’ＣＴに対する
供給割合は、対象目的物によって適宜選択すればよいが
、例えばＴＯＬを出発原料としてＭＣＴまたはＤＣＴを
製造する場合は、ＴＯＬ １ｍｏｌに対し化学量論量の
６０〜８０ｍｏ１％程度とすればよく、Ｍ’ＣＴを出発
原料としてＤＣＴを製造する場合は、ＭＣＴｌｍｏｌに
対し化学量論量の４０〜７０ｍｏ１％程度とすればよい
。In the present invention, the supply ratio of chlorine to TOL or M'CT may be appropriately selected depending on the target object, but for example, when producing MCT or DCT using TOL as a starting material, The amount may be about 60 to 80 mo1% of the stoichiometric amount, and when producing DCT using M'CT as a starting material, the amount may be about 40 to 70 mo1% of the stoichiometric amount with respect to 1 mol of MCT.
反応温度は、ＴＯＬまたはＭＣＴ反応液の融点から沸点
までであるが、２０°Ｃ〜８０℃が好ましい。２０°Ｃ
未満で塩素化を続けると反応液が凝固する恐れかあり、
十分な塩素転化率が得られず、８０°Ｃを超えると塩化
ベンジル等の側鎖塩化物が副生じ易くなり、核置換塩素
化トルエンの選択率の低下につながり、好ましくない。The reaction temperature is from the melting point to the boiling point of the TOL or MCT reaction solution, preferably 20°C to 80°C. 20°C
If chlorination is continued at a temperature lower than that, the reaction solution may solidify.
If a sufficient chlorine conversion rate is not obtained and the temperature exceeds 80°C, side chain chlorides such as benzyl chloride are likely to be produced as by-products, leading to a decrease in the selectivity of nuclear-substituted chlorinated toluene, which is not preferable.
本発明反応においては、触媒が反応液に溶解しない不均
一系で進行するため、通常の固液分離手段で触媒を分離
することができ、また反応生成物は溶解塩素、塩化水素
を含有するのみであり、ストリップ等の操作により反応
生成物から塩素、塩化水素の除去を行えば良く、従来、
実施されていた触媒分離のための水洗等の手段を特に必
要とせず、分離精製手段としては分留及び晶析あるい□
は吸着分離等を用いればよい。Since the reaction of the present invention proceeds in a heterogeneous system in which the catalyst does not dissolve in the reaction liquid, the catalyst can be separated by ordinary solid-liquid separation means, and the reaction product only contains dissolved chlorine and hydrogen chloride. Therefore, chlorine and hydrogen chloride can be removed from the reaction product by stripping or other operations.
There is no special need for water washing or other means for catalyst separation, which was previously used, and fractional distillation, crystallization, or □
For this purpose, adsorption separation or the like may be used.
以下、実施例および比較例にもとついて本発明を具体的
に説明する。Hereinafter, the present invention will be specifically explained based on Examples and Comparative Examples.
実施例１〜２、比較例１
冷却管、温度計、撹拌器、ガス吹き込み管を備えたフラ
スコに第−表記載の原料（２，０ｍｏｌ ）および触媒
（１０，０ｇ）を仕込み、５０°Ｃに昇温した。続いて
塩素ガスを０ 、 ５ ｍｏｌ／ｈｒの速度て６時間ま
たは２時間導入し、未反応塩素量を分析した。反応後、
得られた反応混合物をガスクロマトグラフにて分析した
。その結果を第−表に示す。Examples 1 to 2, Comparative Example 1 A flask equipped with a cooling tube, a thermometer, a stirrer, and a gas blowing tube was charged with the raw materials (2.0 mol) and catalyst (10.0 g) listed in Table 1, and heated at 50°C. The temperature rose to . Subsequently, chlorine gas was introduced at a rate of 0.5 mol/hr for 6 or 2 hours, and the amount of unreacted chlorine was analyzed. After the reaction,
The resulting reaction mixture was analyzed using a gas chromatograph. The results are shown in Table 1.
塩素転化率は次式で定義される値である。The chlorine conversion rate is a value defined by the following formula.
□以下余白□
ハ）発明の効果
本発明によれば、高次核置換塩素化物の生成か極めて少
ないので、有用な核置換塩素化トルエンであるＭＣＴお
よびＤＣＴの収率か実質的に高く、更に触媒が反応生成
物に溶解せず、反応生成物の後処理操作が極めて簡単で
あり、本発明は工業的に非常に有利な核置換塩素化トル
エンの製造方法である。□ Space below □ C) Effects of the invention According to the present invention, since the production of higher-order nuclear-substituted chlorides is extremely small, the yields of MCT and DCT, which are useful nuclear-substituted chlorinated toluenes, are substantially high; The catalyst does not dissolve in the reaction product, and the post-treatment of the reaction product is extremely simple, so the present invention is an industrially very advantageous method for producing nuclear-substituted chlorinated toluene.
Claims (1)
化し、核置換塩素化トルエンを製造するに際し、触媒と
してマグネシアを用い、液相で塩素化することを特徴と
する核置換塩素化トルエンの製造方法。1. A method for producing nuclear-substituted chlorinated toluene, which comprises using magnesia as a catalyst to chlorinate toluene and/or monochlorotoluene to produce nuclear-substituted chlorinated toluene in a liquid phase.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2334979A JPH04208237A (en) | 1990-11-30 | 1990-11-30 | Production of nucleus-substituted chlorinated toluene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2334979A JPH04208237A (en) | 1990-11-30 | 1990-11-30 | Production of nucleus-substituted chlorinated toluene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04208237A true JPH04208237A (en) | 1992-07-29 |
Family
ID=18283368
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2334979A Pending JPH04208237A (en) | 1990-11-30 | 1990-11-30 | Production of nucleus-substituted chlorinated toluene |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04208237A (en) |
-
1990
- 1990-11-30 JP JP2334979A patent/JPH04208237A/en active Pending
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