CN1386733A - Process for preparing isobutanoic acid - Google Patents
Process for preparing isobutanoic acid Download PDFInfo
- Publication number
- CN1386733A CN1386733A CN 01114954 CN01114954A CN1386733A CN 1386733 A CN1386733 A CN 1386733A CN 01114954 CN01114954 CN 01114954 CN 01114954 A CN01114954 A CN 01114954A CN 1386733 A CN1386733 A CN 1386733A
- Authority
- CN
- China
- Prior art keywords
- manufacture method
- isopropylformic acid
- reaction
- acid manufacture
- isopropylformic
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
A process for industrially preparing isobutanoic acid fron isobutyraldehyde is characterized by that under the action of the catalyst which is the isobutyrate, acetate or butyrate of Mn, Co, Or Cu or their mixture, the reaction takes place at 0-50 deg.C and 0-2.0 MPa in bubbling tower or reactor. Its advantages is high conversion of isobutyraldehyde (more than 99.5%) and high selectivity of isobutyric acid (more than 90%).
Description
The present invention relates to a kind of isobutyric manufacture method, particularly relating to a kind of is that raw material is produced isobutyric processing method with the isobutyric aldehyde.
Isopropylformic acid has widespread use as flavouring agent, medicine and fine chemical material, and its preparation method can be divided into Isobutyraldehyde process and isopropylcarbinol oxidation style, oxygenant available air or oxygen by raw material sources.Alcohol oxidation style product yield is low, and productive rate only is 73%～76%, and the production cost height, by product is more, three wastes treatment capacity is big, and applying of its technology is restricted.Isobutyraldehyde oxidation method product selectivity height, technological process is simple, is the isopropylformic acid manufacture method that generally adopts at present.
It is less to prepare isobutyric method report about the isobutyric aldehyde oxidation step, Japanese Patent JP 4-108758 discloses a kind of manufacture method of carboxylic acid: under the katalysis of nickel compound, contain the aldehyde cpd and the oxygen-containing gas reaction of straight or branched alkyl, aromatic base, generate corresponding carboxylic acid.The catalyzer that is adopted is the polyoxy heterogeneous ring compound of a class complexity, the nickeliferous heterogeneous ring compound complex structure of this class, and synthetic difficulty, and cost an arm and a leg, use as commercial catalysts, will cause production cost to increase.U.S. Pat 5,068,366 have introduced coproduction oxidation iso-butylene and isobutyric synthetic method.This reaction adopts the straight-chain carboxylic acid's salt such as the Cobaltous diacetate of variable valency metals such as cobalt, manganese, iron, copper to make catalyzer, under the dichlorobenzene solvent action, 20～180 ℃ of temperature of reaction, reaction times 4h makes isobutylene oxidation thing and isopropylformic acid by iso-butylene and the common oxidation of isobutyric aldehyde.As the coproduction product, isobutyric yield is very low, and the highest have only 12.5%.
The objective of the invention is, provide a kind of that be suitable for that industrial production is used and catalytic effect is good, adopt isobutyric aldehyde to make isobutyric novel method as the raw material oxidation.Another object of the present invention is a catalyzer cheap and easy to get by adopting, that toxicity is little, can under the reaction conditions of gentleness, react, and the product selectivity height, production cost is low, thereby improves competitiveness of product.
In order to achieve the above object, the present invention proposes following isobutyric manufacture method:
In the plastics bubble tower or reactor of stainless steel, lass lining or organic solvent-resistant, add isobutyric aldehyde and mixture of catalysts, in the presence of oxygen-containing gas and/or solvent, reaction generates isopropylformic acid.Reaction can be carried out in the presence of solvent, also can tap into capable oxidizing reaction.The solvent that is adopted is generally isopropylformic acid, acetic acid, propionic acid, butanic acid etc.These solvents both may be used alone, can also be used in combination.Especially isopropylformic acid helps obtaining high product yield, does not have separation problem simultaneously.The quality compositing range of isobutyric aldehyde is 5%～99.5% in the general reaction raw materials, and the quality compositing range of solvent is 95%～0.5%.
The catalyzer that reaction is used can be the straight or branched carboxylate salt of manganese metal, cobalt, copper etc., as isobutyrate, acetate or butanic acid salt, good catalytic activity be the isobutyrate of this metalloid, preferred isopropylformic acid manganese.Also two kinds of materials wherein can be made composite catalyzer, the representative isopropylformic acid enumerated manganese and isopropylformic acid copper, isopropylformic acid manganese and neutralized verdigris, manganese acetate and Cobaltous diacetate, isopropylformic acid manganese and butanic acid cobalt etc. with any than the mixture of forming.These catalyzer can be obtained with any method, do not have special restriction, and are also passable with what sell on the market.
In the present invention, suitable catalyzer add-on is 0.005%～5.0% (wt) of material total amount, improves catalyst consumption, helps the carrying out of oxidizing reaction.But catalyst levels is too many, and production cost improves first, second easily causes deep oxidation and causes product selectivity to descend.Be preferably 0.05%～3.0% (wt), preferred 0.05%～1.0% (wt).
In bubble tower or tank reactor, temperature of reaction is controlled in 0～50 ℃ of scope, and temperature of reaction is 20～40 ℃ preferably; React (20～30 ℃) under the room temperature, speed of response is fast at this moment, reaction yield is high, reaches reaction effect preferably.
The system pressure of reaction is 0～2.0MPa (absolute pressure), and reaction pressure improves, and dissolved oxygen speeds up, and the isobutyric aldehyde transformation efficiency raises.Pressure does not have influence substantially to the selectivity of reaction.
Being used for oxygen-containing gas of the present invention can be oxygen, air or oxygen and the mixture that reaction is inert gasses.In 30～600 minutes, feed the oxygen oxygen-containing gas of equivalent oxygen (or contain) of 0.5～2.0 times of theoretical amount, can keep speed of response and reaction yield preferably.
In the present invention, oxygen or oxygen-containing gas are fed by bubble tower or reactor bottom, are divided into bubble in small, broken bits through gas distributor, can increase the gas-to-liquid contact area like this, improve gas effciency.Reaction mass, is injected by bubble tower or reactor top after the outer water cooler cooling of process by bubble tower or the extraction of reactor bottom through pump again in reaction process, thereby forms the outer circulation of reaction mass.Outer circulation rises stirs and condensation, the selectivity of control reaction temperature and product effectively.The total overall reaction material at 1～10 minute internal recycle once.
Reaction of the present invention both can be carried out in liquid phase continuously, also can carry out in the gap.Adopt isobutyric manufacture method disclosed in this invention, the transformation efficiency of isobutyric aldehyde is greater than 99.5%, and isobutyric selectivity reaches more than 90%.
The isobutyric synthesis technique that the present invention proposes adopts isobutyrate catalyzer cheap and easy to get, catalytic efficiency height not only, thus improved isobutyric selectivity; And do not introduce other impurity, easily separate with product.On the other hand, reaction is at room temperature carried out, and reaction heat can shift out by outer circulation and water coolant, needn't adopt low temperature control system, and facility investment is less, and energy consumption reduces.Whole process flow is simple, and the product yield height is easy to industry and promotes.
In order more specifically to describe technical scheme of the present invention, be described further below in conjunction with embodiment, but the present invention is not limited to these embodiment.
Embodiment 1
At internal diameter is to add 150 gram isobutyric aldehydes, 0.2 gram isopropylformic acid manganese in the stainless steel bubbling tower of 20mm, high 750mm.To 0.3MPa, in 180 minutes, at the uniform velocity feed 99.8 gram oxygen with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process, and keeping temperature of reaction is 20～30 ℃, and reaction heat can shift out by outer circulation and water coolant, and afterreaction finished in 180 minutes.Through gas chromatographic analysis, the isobutyric aldehyde transformation efficiency is 99.5%, and the isopropylformic acid selectivity is 91.9%.
Embodiment 2
Employing is with the same bubbling column reactor of embodiment 1.Add 100 gram isobutyric aldehydes, 0.2 gram manganese acetate.To 0.2MPa, in 200 minutes, at the uniform velocity feed 24.7 gram oxygen and 123.5 gram air with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process, and the maintenance temperature of reaction is 20～30 ℃.Afterreaction finished in 200 minutes.Analyze through vapor-phase chromatography, drawing the isobutyric aldehyde transformation efficiency is 99.4%, and the isopropylformic acid selectivity is 90.1%.
Embodiment 3
Employing is with the same bubbling column reactor of embodiment 1.Add 150 gram isobutyric aldehydes, 0.4 gram neutralized verdigris.To 0.2MPa, in 180 minutes, at the uniform velocity feed 99.8 gram oxygen and 86.6 gram nitrogen with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process, 30～40 ℃.Afterreaction finished in 180 minutes.Analyze through vapor-phase chromatography, drawing the isobutyric aldehyde transformation efficiency is 99.4%, and the isopropylformic acid selectivity is 90.3%.
Embodiment 4
Employing is with the same bubbling column reactor of embodiment 1.Add 150 gram isobutyric aldehydes, 0.1 gram isopropylformic acid manganese.Normal pressure at the uniform velocity fed 267 gram air in 400 minutes.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process.Temperature of reaction is 20～40 ℃, 400 minutes reaction times.Through sampling analysis, drawing the isobutyric aldehyde transformation efficiency is 98.6%, and the isopropylformic acid selectivity is 92.3%.
Embodiment 5
Employing is with the same bubbling column reactor of embodiment 1.Add 150 gram isobutyric aldehydes, 1.5 gram isopropylformic acid manganese.To 0.3MPa, in 180 minutes, at the uniform velocity feed 80 gram oxygen with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process, and temperature of reaction is 20～40 ℃, 180 minutes reaction times.Through sampling analysis, drawing the isobutyric aldehyde transformation efficiency is 99.1%, and the isopropylformic acid selectivity is 91.7%.
Embodiment 6
Employing is with the same bubbling column reactor of embodiment 1.Add 150 gram isobutyric aldehydes, 0.08 gram manganese acetate and 0.08 gram neutralized verdigris.To 0.3MPa, in 240 minutes, at the uniform velocity feed 88 gram oxygen with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 170ml/min in reaction process, and temperature of reaction is 20～30 ℃, 240 minutes reaction times.Through sampling analysis, drawing the isobutyric aldehyde transformation efficiency is 99.5%, and the isopropylformic acid selectivity is 93.3%.
Embodiment 7
Employing is with the same bubbling column reactor of embodiment 1.Add 100 gram isobutyric aldehydes, 0.013 gram isopropylformic acid manganese and 0.013 gram isopropylformic acid copper.With nitrogen punching press 0.3MPa, in 180 minutes, at the uniform velocity feed 44.6 gram oxygen.Reaction mass carries out outer circulation with the speed of 82ml/min in reaction process, and temperature of reaction is 20～30 ℃, 180 minutes reaction times.Through sampling analysis, drawing the isobutyric aldehyde transformation efficiency is 99.6%, and the isopropylformic acid selectivity is 94.5%.
The comparative example 8
Employing is with the same bubbling column reactor of embodiment 1.Add 150 gram isobutyric aldehydes, 0.15 gram isopropylformic acid manganese.To 0.3MPa, in 180 minutes, at the uniform velocity feed 68 gram oxygen with the nitrogen punching press.Reaction mass carries out outer circulation with the speed of 170ml/min in reaction process, and temperature of reaction is 60～70 ℃, 180 minutes reaction times.Through sampling analysis, drawing the isobutyric aldehyde transformation efficiency is 99.8%, and the isopropylformic acid selectivity is 78.3%.
Claims (13)
1, a kind ofly makes isobutyric processing method by isobutyric aldehyde, it comprise with the straight or branched metal carboxylate of manganese metal, cobalt, copper etc. or this several materials with any than the mixture of forming as catalyzer, have or solvent-free in the presence of, isobutyric aldehyde and oxygen-containing gas liquid phase contact reacts generate isopropylformic acid.
2, isopropylformic acid manufacture method according to claim 1 is characterized in that used catalyzer is the isobutyrate of manganese metal, cobalt, copper etc.
3, isopropylformic acid manufacture method according to claim 1 is characterized in that used catalyzer is the acetate or the butanic acid salt of manganese metal, cobalt, copper etc.
4, isopropylformic acid manufacture method according to claim 1, it is characterized in that used catalyzer be several materials in isobutyrate, acetate and the butanic acid salt of manganese metal, cobalt, copper etc. with any than the mixture of forming.
5, isopropylformic acid manufacture method according to claim 1 is characterized in that described catalyzer or catalyst mixture consumption are 0.005%～5.0% of reaction mixture total amount.
6, isopropylformic acid manufacture method according to claim 1 is characterized in that described catalyzer or catalyst mixture consumption are 0.05%～3.0% of reaction mixture total amount.
7, isopropylformic acid manufacture method according to claim 1 is characterized in that oxidizing reaction temperature is 0～50 ℃.
8, isopropylformic acid manufacture method according to claim 1 is characterized in that oxidizing reaction temperature is 20～40 ℃.
9, isopropylformic acid manufacture method according to claim 1 is characterized in that the oxidation reactor internal pressure is 0～2.0MPa.
10, isopropylformic acid manufacture method according to claim 1 is characterized in that oxygen-containing gas can be oxygen, air or oxygen and the mixture that reaction is inert gasses.
11, isopropylformic acid manufacture method according to claim 1 is characterized in that reaction raw materials by isobutyric aldehyde and/or solvent composition, and the quality of solvent composition accounts for 95%～0.5% of reaction mass total amount.
12, isopropylformic acid manufacture method according to claim 1 is characterized in that solvent for use can be isopropylformic acid, acetic acid, interior acid or butanic acid.
13, isopropylformic acid manufacture method according to claim 1 is characterized in that temperature of reaction passes through material outer circulation mode and control.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01114954 CN1221512C (en) | 2001-05-18 | 2001-05-18 | Process for preparing isobutanoic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 01114954 CN1221512C (en) | 2001-05-18 | 2001-05-18 | Process for preparing isobutanoic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1386733A true CN1386733A (en) | 2002-12-25 |
| CN1221512C CN1221512C (en) | 2005-10-05 |
Family
ID=4661554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 01114954 Expired - Lifetime CN1221512C (en) | 2001-05-18 | 2001-05-18 | Process for preparing isobutanoic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1221512C (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1296132C (en) * | 2004-12-24 | 2007-01-24 | 宜兴市中港精细化工厂 | Zirconium-base catalyst for synthesis of isobutyric acid and preparation method thereof |
| CN102010321A (en) * | 2010-12-04 | 2011-04-13 | 宜兴市恒兴精细化工有限公司 | Process for continuously producing isobutyric acid |
| CN103086866A (en) * | 2013-02-19 | 2013-05-08 | 中国科学院化学研究所 | Method for synthesizing acid by oxidizing aldehyde in photocatalytic selective mode |
| CN109180461A (en) * | 2018-08-21 | 2019-01-11 | 贵州微化科技有限公司 | A kind of method that micro-reacting tcchnology prepares butyric acid |
| CN110526814A (en) * | 2019-07-27 | 2019-12-03 | 宁夏沃凯珑新材料有限公司 | The method that serialization prepares butyric acid |
| CN111116348A (en) * | 2019-12-27 | 2020-05-08 | 浙江工业大学 | Preparation method for synthesizing carboxylic acid by oxidizing aldehyde with bimetallic catalyst |
| CN112076715A (en) * | 2019-06-12 | 2020-12-15 | 中国石油化工股份有限公司 | Reaction device for preparing isobutyric acid |
| CN113185395A (en) * | 2021-04-09 | 2021-07-30 | 润泰新材料股份有限公司 | Process for the production of isobutyric acid |
| CN114591163A (en) * | 2022-03-21 | 2022-06-07 | 中国成达工程有限公司 | Method for synthesizing succinic acid by oxidizing succinic dialdehyde |
-
2001
- 2001-05-18 CN CN 01114954 patent/CN1221512C/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1296132C (en) * | 2004-12-24 | 2007-01-24 | 宜兴市中港精细化工厂 | Zirconium-base catalyst for synthesis of isobutyric acid and preparation method thereof |
| CN102010321A (en) * | 2010-12-04 | 2011-04-13 | 宜兴市恒兴精细化工有限公司 | Process for continuously producing isobutyric acid |
| CN103086866A (en) * | 2013-02-19 | 2013-05-08 | 中国科学院化学研究所 | Method for synthesizing acid by oxidizing aldehyde in photocatalytic selective mode |
| CN109180461A (en) * | 2018-08-21 | 2019-01-11 | 贵州微化科技有限公司 | A kind of method that micro-reacting tcchnology prepares butyric acid |
| CN112076715A (en) * | 2019-06-12 | 2020-12-15 | 中国石油化工股份有限公司 | Reaction device for preparing isobutyric acid |
| CN110526814A (en) * | 2019-07-27 | 2019-12-03 | 宁夏沃凯珑新材料有限公司 | The method that serialization prepares butyric acid |
| CN111116348A (en) * | 2019-12-27 | 2020-05-08 | 浙江工业大学 | Preparation method for synthesizing carboxylic acid by oxidizing aldehyde with bimetallic catalyst |
| CN111116348B (en) * | 2019-12-27 | 2023-02-03 | 浙江工业大学 | Preparation method for synthesizing carboxylic acid by oxidizing aldehyde with bimetallic catalyst |
| CN113185395A (en) * | 2021-04-09 | 2021-07-30 | 润泰新材料股份有限公司 | Process for the production of isobutyric acid |
| CN114591163A (en) * | 2022-03-21 | 2022-06-07 | 中国成达工程有限公司 | Method for synthesizing succinic acid by oxidizing succinic dialdehyde |
| CN114591163B (en) * | 2022-03-21 | 2023-09-15 | 中国成达工程有限公司 | Method for synthesizing succinic acid by oxidizing butanedial |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1221512C (en) | 2005-10-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| TWI234559B (en) | A process for preparing aliphatic carboxylic acids from aldehydes | |
| KR19980064557A (en) | Process for production of higher oxo alcohols | |
| CN107445830B (en) | Method for producing glyoxylic ester by oxidative dehydrogenation of glycolate | |
| WO1994007834A1 (en) | A recycling process for the production of adipic acid and other aliphatic dibasic acids | |
| CN108250069B (en) | Preparation method of isooctanoic acid | |
| CN1221512C (en) | Process for preparing isobutanoic acid | |
| JP2000239211A (en) | Production of cycloalkanone | |
| CN113956151A (en) | Method for oxidizing aldehyde into acid | |
| CA1157039A (en) | Method for producing aliphatic carboxylic acids saturated with alkyl esters | |
| CN102452894B (en) | Method for catalytic oxidation of cyclic ketone by nanometer Beta molecule sieve | |
| CA1162566A (en) | Processes for producing 7-octen-1-al and derivatives thereof | |
| EP3408251B1 (en) | Efficient synthesis of methacrolein from methanol and propionaldehyde | |
| CN1277801C (en) | Method for preparation of propionic acid | |
| CA2157544C (en) | Process for the preparation of mono- or dicarboxylic acids from aldehydes, from their full acetals or hemiacetals or from mixtures therefor | |
| US6696582B2 (en) | Method for producing aliphatic carboxylic acids from aldehydes | |
| RU2294920C2 (en) | Two-stage method for hydrogenation of maleic acid to 1,4-butanediol | |
| JP2002003440A (en) | Method for manufacturing aromatic polycarboxylic acid | |
| CN109575036B (en) | Metal hematoporphyrin diether diester compound, catalyst and preparation method thereof, and cyclohexane catalytic oxidation method | |
| CN103172505A (en) | Method for selectively oxidizing toluene to synthesize benzaldehyde | |
| CN1226272C (en) | Method for preparing methyl-carbonate | |
| CN112521266B (en) | Process for producing adipic acid | |
| EP0118258B1 (en) | Catalytic process for the preparation of ethylene glycol | |
| CN1422840A (en) | 2-ethyl hexanoic acid production method | |
| JP7168565B2 (en) | Method for producing bisacyloxylated exomethylene compound | |
| CN117326938A (en) | Process for oxidation of cyclohexane and products thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROLEUM & CHEMICAL CORPORATION Free format text: FORMER OWNER: QILU PETROCHEMICAL GROUP CO., CHINA PETROCHEMICAL CORP. Effective date: 20071228 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20071228 Address after: Linzi Zibo District, Shandong province Sinopec Qilu Branch of science and technology Patentee after: Sinopec Corp. Address before: 124 mailbox, Zibo City, Shandong Province Patentee before: Qilu Petrochemical Co., China Petrochemical Group Corp. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20051005 |
|
| CX01 | Expiry of patent term |