JP2723621B2 - Method for producing isopropyl alcohol - Google Patents
Method for producing isopropyl alcoholInfo
- Publication number
- JP2723621B2 JP2723621B2 JP1175502A JP17550289A JP2723621B2 JP 2723621 B2 JP2723621 B2 JP 2723621B2 JP 1175502 A JP1175502 A JP 1175502A JP 17550289 A JP17550289 A JP 17550289A JP 2723621 B2 JP2723621 B2 JP 2723621B2
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- acetone
- isopropyl alcohol
- molar ratio
- producing isopropyl
- 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.)
- Expired - Lifetime
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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明はアセトンと水素又は水素含有ガスを反応させ
てイソプロピルアルコールを製造する方法に関する。Description: TECHNICAL FIELD The present invention relates to a method for producing isopropyl alcohol by reacting acetone with hydrogen or a hydrogen-containing gas.
アセトンを水素により触媒の存在下気相で還元してイ
ソプロピルアルコールを得る従来の方法としてはU.S.P2
456,187に軽石に担持した銅触媒を用いて製造する方法
が記載されている。この方法で示されている水素とアセ
トンのモル比は20で圧力は常圧である。USP2 is a conventional method for obtaining isopropyl alcohol by reducing acetone in the gas phase with hydrogen in the presence of a catalyst.
No. 456,187 describes a method for producing using a copper catalyst supported on pumice. The molar ratio of hydrogen to acetone shown in this method is 20 and the pressure is normal pressure.
然し、イソプロピルアルコール製造の工業化を考える
場合、水素とアセトンのモル比を出来る限り低くし、水
素循環に要する動力を下げることが好ましい。However, when considering the industrialization of isopropyl alcohol production, it is preferable to lower the molar ratio of hydrogen to acetone as much as possible to reduce the power required for hydrogen circulation.
本発明者等は酸化銅・酸化クロム触媒の存在下で触媒
当たりのイソプロピルアルコールの収率を出来る限り高
く、且つ水素の対アセトンモル比を下げること鋭意検討
したが、単に水素の対アセトンモル比を下げると循環量
は低下し循環に要する動力は下がるが、水素モル比の低
下により反応速度も小さくなり、転化率が低下するため
触媒当たりのイソプロピルアルコールの収率が下がるば
かりか、未反応アセトンの回収にもエネルギーを要する
ことになり経済的損失は非常に大きいことが判明した。The present inventors have studied diligently to increase the yield of isopropyl alcohol per catalyst in the presence of a copper oxide / chromium oxide catalyst as much as possible and to reduce the molar ratio of hydrogen to acetone, but simply to reduce the molar ratio of hydrogen to acetone. Although the amount of circulation decreases and the power required for circulation decreases, the reaction rate decreases due to the decrease in the molar ratio of hydrogen, and the conversion rate decreases, so not only the yield of isopropyl alcohol per catalyst decreases, but also the recovery of unreacted acetone Energy was required, and the economic loss was found to be very large.
従って本発明者等は更に研究を進めた結果上記問題点
を解決し本発明に到達した。Therefore, the present inventors have further studied and as a result, solved the above-mentioned problems and arrived at the present invention.
即ち本発明のイソプロピルアルコールの製造方法は、
酸化銅・酸化クロム触媒の存在下アセトンを水素又は水
素とイナートガスより成る水素含有ガスにより気相で水
素化してイソプロピルアルコールを製造する方法におい
て、水素とアセトンのモル比が1.1〜5.0で且つ水素含有
ガスとアセトンのモル比が５以下であり、反応温度が60
〜200℃、反応圧力１〜10Kg/cm2Gであることを特徴とす
るものである。That is, the method for producing isopropyl alcohol of the present invention comprises:
A method for producing isopropyl alcohol by hydrogenating acetone in the gas phase with hydrogen or a hydrogen-containing gas comprising hydrogen and an inert gas in the presence of a copper oxide / chromium oxide catalyst, wherein the molar ratio of hydrogen to acetone is 1.1 to 5.0 and the hydrogen content The molar ratio of gas to acetone is 5 or less, and the reaction temperature is 60
~ 200 ° C, reaction pressure 1 ~ 10Kg / cm 2 G.
ここで水素とアセトンのモル比が1.1以下であるとア
セトンの転化率が低下するばかりか、イソプロピルアル
コールへの選択率も低下し、副生物が多くなる。水素と
アセトンのモル比が５以上では前述の様に水素を回収し
て循環使用する動力が増大する、本発明の方法では純度
の高い水素を使う必要がなく、例えばエチレン製造プラ
ントで発生するメタンを含む水素あるいは窒素を含む水
素の使用も可能である。この場合反応に水素とアセトン
のモル比1.1以上、水素含有ガスとアセトンのモル比5.0
以下であれば好い。反応温度は通常60℃から200℃であ
れば良く、200℃以上では副生物の生成が多くイソプロ
ピルアルコール選択率が低下する、又60℃以下では反応
速度が低下し未反応アセトンが増加する。反応圧力は1K
g/cm2G以上、10Kg/cm2G以下が好ましいが1Kg/cm2G以下
では反応速度が低下する、10Kg/cm2以上では反応器の耐
圧が高くなり反応器が高価になる。Here, if the molar ratio of hydrogen to acetone is 1.1 or less, not only the conversion of acetone decreases, but also the selectivity to isopropyl alcohol decreases, and the amount of by-products increases. When the molar ratio of hydrogen to acetone is 5 or more, the power for recovering and recycling hydrogen is increased as described above. In the method of the present invention, it is not necessary to use high-purity hydrogen. It is also possible to use hydrogen containing nitrogen or hydrogen containing nitrogen. In this case, the molar ratio of hydrogen to acetone is 1.1 or more, and the molar ratio of hydrogen-containing gas to acetone is 5.0 or more.
The following is good. The reaction temperature may be usually from 60 ° C. to 200 ° C. If it is higher than 200 ° C., by-products are generated and the selectivity of isopropyl alcohol is reduced. Reaction pressure is 1K
g / cm 2 G or more and 10 kg / cm 2 G or less are preferable, but if it is 1 kg / cm 2 G or less, the reaction rate decreases. If it is 10 kg / cm 2 or more, the pressure resistance of the reactor increases and the reactor becomes expensive.
以下実施例により更に詳細に説明する。 Hereinafter, the present invention will be described in more detail with reference to examples.
実施例１ 内径27.2mm、管長4000mmの反応器に酸化銅・酸化クロ
ム触媒を1.5充填し触媒を水素で還元後、アセトンを
毎時26.0mol、水素を毎時52.0mol、メタンを毎時2.0mo
l、温度120℃で圧力2.0Kg/cm2Gで供給した。この時の反
応ガスのモル比は水素：メタン：アセトン＝2:2:1であ
る、又この時の空搭速度は1941/Hrである。Example 1 A reactor having an inner diameter of 27.2 mm and a tube length of 4,000 mm was filled with 1.5 catalysts of copper oxide and chromium oxide, and after reducing the catalyst with hydrogen, 26.0 mol / h of acetone, 52.0 mol / h of hydrogen, and 2.0 mol / h of methane were used.
l, supplied at a temperature of 120 ° C. and a pressure of 2.0 kg / cm 2 G. At this time, the molar ratio of the reaction gas is hydrogen: methane: acetone = 2: 2: 1, and the airborne speed at this time is 1941 / Hr.
この結果、アセトンの転化率は94％であり、イソプロ
ピルアルコールへの選択率は98％であった。As a result, the conversion of acetone was 94%, and the selectivity to isopropyl alcohol was 98%.
実施例２ 実施例１と同じ反応器を使用し、種々な条件で実験し
た結果を第１表に示す。Example 2 Table 1 shows the results of experiments conducted under various conditions using the same reactor as in Example 1.
〔発明の効果〕 本発明の方法によれば、アセトンからイソプロピルア
ルコールを高収率で経済的に得られ、アセトンを原料と
するイソプロピルアルコール製造プロセスが工業的に確
立出来る。 [Effects of the Invention] According to the method of the present invention, isopropyl alcohol can be economically obtained from acetone at a high yield, and a process for producing isopropyl alcohol using acetone as a raw material can be industrially established.
Claims (1)
を水素又は水素とイナートガスより成る水素含有ガスに
より気相で水素化してイソプロピルアルコールを製造す
る方法において、水素とアセトンのモル比が1.1〜5.0で
且つ水素含有ガスとアセトンのモル比が５以下であり、
反応温度が60〜200℃、反応圧力１〜10Kg/cm2Gであるこ
とを特徴とするイソプロピルアルコールの製造方法1. A method for producing isopropyl alcohol by hydrogenating acetone in the gas phase with hydrogen or a hydrogen-containing gas comprising hydrogen and an inert gas in the presence of a copper oxide / chromium oxide catalyst, wherein the molar ratio of hydrogen to acetone is 1.1 to 1. 5.0 and the molar ratio between the hydrogen-containing gas and acetone is 5 or less;
A method for producing isopropyl alcohol, wherein the reaction temperature is 60 to 200 ° C. and the reaction pressure is 1 to 10 kg / cm 2 G.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1175502A JP2723621B2 (en) | 1989-07-10 | 1989-07-10 | Method for producing isopropyl alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1175502A JP2723621B2 (en) | 1989-07-10 | 1989-07-10 | Method for producing isopropyl alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0341038A JPH0341038A (en) | 1991-02-21 |
| JP2723621B2 true JP2723621B2 (en) | 1998-03-09 |
Family
ID=15997165
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1175502A Expired - Lifetime JP2723621B2 (en) | 1989-07-10 | 1989-07-10 | Method for producing isopropyl alcohol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2723621B2 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4754058B2 (en) * | 2000-10-16 | 2011-08-24 | 三井化学株式会社 | Method for producing isopropyl alcohol |
| ITMI20012707A1 (en) | 2001-12-20 | 2003-06-20 | Enichem Spa | PROCESS FOR THE ALKYLATION OF AROMATIC COMPOUNDS |
| JP4506463B2 (en) | 2004-12-28 | 2010-07-21 | トヨタ自動車株式会社 | Vehicle height adjustment device |
| JP4678841B2 (en) | 2005-08-24 | 2011-04-27 | 本田技研工業株式会社 | Engine drive generator output voltage regulator |
| US7569942B2 (en) | 2006-07-03 | 2009-08-04 | Honda Motor Co., Ltd. | Output voltage controller of engine-driven generator |
| JP5300392B2 (en) * | 2008-09-25 | 2013-09-25 | 三井化学株式会社 | Method for producing isopropanol |
| WO2010064500A1 (en) * | 2008-12-01 | 2010-06-10 | 三井化学株式会社 | Method for producing olefin |
| JP5497411B2 (en) * | 2008-12-01 | 2014-05-21 | 三井化学株式会社 | Olefin production method |
| WO2010106966A1 (en) | 2009-03-16 | 2010-09-23 | 三井化学株式会社 | Process for production of olefins |
-
1989
- 1989-07-10 JP JP1175502A patent/JP2723621B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0341038A (en) | 1991-02-21 |
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