CN103755537B - The co-production of a kind of hexone and diisobutyl ketone - Google Patents
The co-production of a kind of hexone and diisobutyl ketone Download PDFInfo
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- CN103755537B CN103755537B CN201410016321.0A CN201410016321A CN103755537B CN 103755537 B CN103755537 B CN 103755537B CN 201410016321 A CN201410016321 A CN 201410016321A CN 103755537 B CN103755537 B CN 103755537B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
- C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
- C07C45/70—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction with functional groups containing oxygen only in singly bound form
- C07C45/71—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction with functional groups containing oxygen only in singly bound form being hydroxy groups
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
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Abstract
The present invention relates to a kind of preparation method of medicine intermediate, specifically refer to a kind of method of hexone and diisobutyl ketone coproduction.The present invention be by acetone and Virahol through mixing and preheating, enter in the reactor that copper-palladium-zirconium-zinc/aluminium oxide catalyst is housed, at temperature of reaction 130 ~ 210 DEG C, reaction pressure 0.1 ~ 4.0MPa, Virahol liquid phase air speed 0.1 ~ 2.5h
-1with under the reaction conditions of keto-alcohol mol ratio 1 ~ 7, acetone generates the reaction mixture based on hexone and diisobutyl ketone through reaction, obtains hexone product and diisobutyl ketone product through separation and purification.Advantage of the present invention is that the use cost of catalyzer also significantly reduces, energy consumption is low, and the heavy constituent that equipment simply produces without particular requirement, method of the present invention is few, and the utilization ratio of acetone is high, and product yield is high.
Description
Technical field
The present invention relates to a kind of preparation method of medicine intermediate, specifically refer to a kind of method of hexone and diisobutyl ketone coproduction.
Background technology
Hexone (MIBK) is a kind of the water white transparency mid-boiling point ketones solvent with aromatic ketone smell and chemical intermediate of excellent performance, solvency power is 10 times of acetic ester, can with alcohol, benzene, ether and most of immiscible organic solvent, can be used as the raw material etc. of coating, nitrocotton, ethyl cellulose, videotape recording, paraffin and multiple natural or synthetic resins solvent, the dewaxing medium of lube oil finishing, rare earth metal extractant, polymer reaction initiator, tensio-active agent, medicine, agricultural chemicals extraction agent and rubber antioxidant.Be the current comparatively well sold and in short supply Speciality Petrochemicals intermediate of China, in many Application Areass, there is irreplaceability, the main dependence on import of current needs.
Hexone industrialized producing technology divides by raw material isopropanol method and acetone method.Isopropanol method is raw material with Virahol, and obtain acetone through dehydrogenation, then acetone obtains MIBK through shortening again, simultaneously cogeneration of propanone and mesityl oxide.Before mid-term in 20th century, most of acetone is obtained by dehydrogenation of isopropanol, and therefore many petro-chemical corporations Virahol produces MIBK.Along with production phenols produces the successful use of acetone novel process, acetone production cost significantly reduces, be that Material synthesis MIBK device still occupies 25% in the industrial production with Virahol at present, along with the competitive edge of acetone as raw material becomes clear day by day, estimate to be that the operational path of raw material is by fewer and feweri from now on Virahol.Acetone method is divided into again three-step approach and single stage method according to reaction process, and because single stage method has, technical process is short, less investment, feed stock conversion advantages of higher, has become the main flow of MIBK synthetic technology.
Acetone three-step approach is produced MIBK production technique and is divided into three-step reaction process, i.e. liquid phase condensations, acid catalyst dehydration and selec-tive hydrogenation.Due to succeeding in developing of multifunctional efficient catalyst technology, acetone through one-step method hydrogenation produces MIBK becomes the most practical operational path of current industrialization, reaction mechanism is dewatered by aldol condensation, generate mesityl oxide, then generate MIBK through shortening, therefore catalyzer is polyfunctional catalyst.
Veba-Chemie company of Germany took the lead in building One-step production device in nineteen sixty-eight, and its acetone per pass conversion is 34.4%, MIBK selectivity is 96.5%.Veba and Taxaco two company of Germany selects storng-acid cation exchange resin and makees catalyzer to the Pd of olefinic double bonds hydrogenating function, prepares more difficult; U.S. Mobil company develops Pd-NSM-5 modified zeolite catalyst in recent years, only needs dipping, roasting just can be prepared.China's part scientific research institutions also carry out a large amount of research and development to polyfunctional catalyst in recent years, catalyzer as Fushun Petrochemical Research Institute's development is made up of form ion exchange resin and a year Pd active al2o3, also develop molecular sieve catalyst, non-amine method synthesis ZSM-5 molecular sieve is adopted to be carrier, take metal Pd as active ingredient, take Ni metal as promotor, synthesis MIBK.Nanjing petrochemical industry research institute develops the bimetal resin type catalyst of one-step synthesis method MIBK, take Zeo-karb as carrier, with metal Pd and a kind of transition metal, Pd and a kind of lanthanide element, Pd and a kind of alkali earth metal for active ingredient forms, this catalyst activity is high, selectivity is good, and uses stable.
Make a general survey of prior art, the catalyzer that focus is compared in present industrialized catalyzer and research is precious metals palladium catalyst.Because palladium catalyst is easily poisoning, to reaction raw materials and conditional request high, and require that hydrogen purity is high, particularly the content of oxygen isoreactivity material is low as far as possible, definitely can not sulfur-bearing element, otherwise easily make precious metals pd poisoning fast, rare gas element such as nitrogen removes as far as possible in addition, because the total pressure in reactor can be improved, and reduces the dividing potential drop of hydrogen; Require that raw material acetone is not moisture, to prevent water, acidic cation-exchange resin catalytic activity is reduced.Palladium Content in Catalyst is higher, generally about 0.2%, causes catalyzer cost higher.
Diisobutyl ketone (DIBK), also known as valerone, is excellent middle high boiling solvent, as resin solvent, has solvability good, do not corrode the advantages such as ground, have good performance in plastic paint.Diisobutyl ketone is mainly used in the industries such as vacuum plating coating, plastic paint and leather finish, can dissolve rhodia, soluble cotton, polystyrene, ethenoid resin, wax, varnish, natural resin and rubber etc.Because boiling point is high, velocity of evaporation is slow, also can be used as Nitrocellulose, nitro sprays paint, the solvent of acrylic resin, ethenoid resin paint and other synthetic resin coatings (has and do not sting the end, solvency power is strong, improve film levelling, gloss, recoatability and the wettability to plastic bottom material, increase the effects such as sorptive force); Also can be used as the fine solvent of manufacture organic dispersing agent, food spices (is mainly used in preparation Fructus Artocarpi Heterophylli, banana, orange juice, Purple Granadilla, tropical fruit, Rum and health and makes gram wine essence used.These product are mainly used as organic solvent), the extraction agent of rare metal (separation as zirconium hafnium etc.) and some drugs, sterilant intermediate.As a kind of fine solvent, DIBK also can be used as the solvent of mobile telephone, high-end computer surface of shell coating.Make the housing of solvent with DIBK, bright in luster, colour-fast, not aging, surface hardness is high, and the long-time surface that uses is still bright as new, deeply likes by consumers in general.
Diisobutyl ketone (DIBK) is industrially the product preparing hexone process by-product, but the selectivity that this process generates diisobutyl ketone is very low, only account for 0.2 ~ 0.3% of base first isobutyl ketone amount, cannot meet the requirement that existing market demand increases day by day; Separately have report to generate Fu Er ketone by acetone through acid catalyzed condensation, repeated hydrogenation is reduced into diisobutyl ketone and preparation method, but does not have the report of suitability for industrialized production.Therefore to develop a kind of technological process of producing diisobutyl ketone be market in the urgent need to.
To sum up state, need at present exploitation a kind of with acetone and Virahol for raw material, use non-pure noble metal catalyst to prepare hexone for suitability for industrialized production, and the production method of coproduction diisobutyl ketone.
Summary of the invention
The present invention in order to overcome the defect of prior art, and considers industrial easy realization, propose a kind of with acetone and Virahol for raw material, use non-pure noble metal catalyst, simultaneously the production method of coproduction diisobutyl ketone and diisobutyl ketone.Concrete technical scheme is as follows:
The method of coproducing methyl isobutyl ketone of the present invention and diisobutyl ketone, through mixing and preheating by acetone and Virahol, enter in the reactor that copper-palladium-zirconium-zinc/aluminium oxide catalyst is housed, at temperature of reaction 130 ~ 210 DEG C, reaction pressure 0.1 ~ 4.0MPa, Virahol liquid phase air speed 0.1 ~ 2.5h
-1with under the reaction conditions of keto-alcohol mol ratio 1 ~ 7, acetone generates the reaction mixture based on hexone and diisobutyl ketone through reaction, obtains hexone product and diisobutyl ketone product through separation and purification.
In order to better play the catalytic performance of catalyzer, preferably, in described copper-palladium-zirconium-zinc/aluminium oxide catalyst, alumina supporter is the aluminum oxide of alkaline earth metal oxide modification, more preferably, described copper-palladium-zirconium-zinc/aluminium oxide catalyst is the trade mark XH-A-69 catalyzer that ZheJiang XinHua Chemical Engineering Co., Ltd has by oneself.Copper-palladium-zirconium-zinc/aluminium oxide catalyst is non-pure noble metal catalyst, relative to pure palladium/strong acidic ion resin catalyzer, palladium content significantly reduces, therefore catalyzer cost is greatly reduced, and selectivity of catalyst and good stability, while generation hexone, also generate diisobutyl ketone, this just in time meets the market requirement at present to diisobutyl ketone, a process coproduction two kinds of products, output is all larger.At present domestic and international full scale plant is not seen the application of non-pure noble metal catalyst.The preparation method of catalyzer of the present invention can use conventional method for preparing catalyst, such as coprecipitation method, dipping method, spraying method etc.With overall catalyst weight gauge, copper content is 0.5 ~ 15%, palladium content is 0.05 ~ 0.1%, zirconium content is 0.1 ~ 1.5%, Zn content is 0.3 ~ 5%, aluminum oxide can be gama-alumina etc., the aluminum oxide of preferred bases soil metal oxide modification, such as magnesium oxide modified aluminum oxide, in alumina supporter, content of magnesia is preferably 0.2 ~ 7%, more preferably 0.4 ~ 3.5%, most preferably ZheJiang XinHua Chemical Engineering Co., Ltd has the alumina supporter that trade mark XH-A-69 catalyzer mates by oneself, although can not its action principle detailed, but the alumina supporter of this coupling is used for producing this catalyzer has the incomparable advantage of other carrier, there is acetone conversion high, the selectivity generating hexone and diisobutyl ketone is high, the advantages such as heavy constituent is few.Composition and the mass content of this trade mark catalyzer current are: copper content is 0.5 ~ 15%, and palladium content is 0.05 ~ 0.1%, and zirconium content is 0.1 ~ 1.5%, and Zn content is 0.3 ~ 5%, and aluminum oxide is gama-alumina; Aluminum oxide in wherein said copper-palladium-zirconium-zinc/aluminium oxide catalyst is preferably the aluminum oxide of alkaline earth metal oxide modification, and in alumina supporter, the mass content of alkaline earth metal oxide is 0.2 ~ 7%.As: the aluminum oxide of alkaline earth metal oxide modification is magnesium oxide modified aluminum oxide, and in alumina supporter, content of magnesia is preferably 0.2 ~ 7%.
The method of coproducing methyl isobutyl ketone of the present invention and diisobutyl ketone, the sepn process of each component comprises the following steps:
(1) synthesis of hexone and diisobutyl ketone:
Raw material acetone and Virahol are through mixing and preheating, enter in the reactor that copper-palladium-zirconium-zinc/aluminium oxide catalyst is housed, under the reaction conditions of temperature of reaction 130 ~ 210 DEG C, reaction pressure 0.1 ~ 4.0MPa, Virahol liquid phase air speed 0.1 ~ 2.5h-1 and keto-alcohol mol ratio 1 ~ 7, Virahol and acetone generate the reaction product based on hexone and diisobutyl ketone through reaction, through cooling and gas-liquid separation, obtain reaction mixture;
(2) from mixed solution, unreacted acetone is separated:
The reaction mixture of (1) step gained enters lightness-removing column, through rectifying separation, from the unreacted acetone of overhead extraction, is mixed by return line with raw material acetone, obtains the still liquid removing acetone from tower reactor;
(3) from Separation of Water the still liquid removing acetone:
The still liquid removing acetone step (2) obtained sends into dehydration tower, and through rectifying separation, from dehydration overhead extraction isopropyl alcohol and water, tower reactor obtains dehydrating kettle liquid, and the logistics of overhead extraction obtains Virahol through Separation of Water;
(4) hexone is separated:
Dehydrating kettle liquid step (3) obtained sends into hexone tower, and through rectifying separation, from the overhead extraction hexone product of hexone tower, tower reactor obtains the still liquid based on diisobutyl ketone;
(5)) diisobutyl ketone is separated:
The still liquid based on diisobutyl ketone step (4) obtained sends into diisobutyl ketone tower, and through rectifying separation, from overhead extraction diisobutyl ketone product, tower reactor obtains heavy constituent.
The reactor used in the method for the invention can be upper feeding mode, and also can be lower feeding manner, the reaction pressure preferably 0.5 ~ 2.5MPa of synthesis system, Virahol liquid phase air speed be preferably 0.5 ~ 2.0h-1.Acetone and Virahol are through catalyzed reaction, and be converted into hexone through condensation, dehydration, wherein a part of hexone generates diisobutyl ketone with Virahol condensation further, also has and is inevitably converted into heavier condensation product on a small quantity.First take off light process by unreacted acetone separation out through rectifying, return it to reactor cycles and use.Have no particular limits the number of theoretical plate of described lightness-removing column and operational condition, the technician in rectifying field can freely design according to rectifying object and operate.
After reclaiming acetone, by the rectifying separation of dehydration tower, separated by the isopropyl alcohol and water lower than methyl iso-butyl ketone (MIBK) volatility from tower top, the isopropyl alcohol and water separated obtains Virahol product through Separation of Water unit.Have no particular limits the number of theoretical plate of described dehydration tower and operational condition, as long as can reach, to be separated object just passable.The technology of Virahol Separation of Water can be taked to add three components as azeotropic entrainment agent, and azeotropic entrainment agent is such as benzene or hexanaphthene etc., also can adopt membrane separation technique etc., repeat no more here.
The liquid separated by water is sent into hexone tower again and is carried out rectifying separation, tower top obtains hexone product, tower reactor obtains the still liquid based on diisobutyl ketone, the same number of theoretical plate to hexone rectifying tower and operational condition do not have particular requirement, the technician in rectifying separation field can according to object design and Choice Theory plate number and operational condition, such as number of theoretical plate is 30 ~ 50 pieces, and reflux ratio is 4, normal pressure or decompression operation.
The still liquid based on diisobutyl ketone obtained from hexone tower tower reactor is delivered to diisobutyl ketone tower and carries out rectifying separation, tower top obtains diisobutyl ketone product, and tower reactor obtains heavier component, such as acetone become with Virahol four consor 2, the heavy constituents such as 6,8-trimethylammonium-4-nonanone.The liquid collecting of tower reactor extraction gets up, and sells or falls as fuel consumption.
The method of coproducing methyl isobutyl ketone of the present invention and diisobutyl ketone has following advantage compared to existing technology:
1. method of the present invention uses non-pure noble metal catalyst, and catalyzer cost is very low compared with pure palladium series catalyst, and industrial application shows that the stability of the catalyzer that the present invention uses obviously is better than pure palladium series catalyst, and the use cost of catalyzer also significantly reduces.
2. method of the present invention can produce hexone and diisobutyl ketone simultaneously.Hexone and diisobutyl ketone are that existing market exists two kinds of considerable Chemicals of insufficiency of supply-demand, economic benefit.Simultaneously by adjustment adjustable product hexone and the diisobutyl ketone of raw material acetone and isopropanol ratios, increase the market ability to ward off risks.
3. the technical process connection and reasonable arrangement of method of the present invention, be different from the production technique of existing hexone, energy consumption is low, and equipment is simple without particular requirement.Diisobutyl ketone is not byproduct in the method for the invention, but a main coproduction product.
4. the heavy constituent of method generation of the present invention is few, and the utilization ratio of acetone is high, and product yield is high.
5, the synthesis for MIBK/DIBK of bibliographical information and XH-A-69 catalyzer shares activity component is had, but it is with acetone or Virahol is single a kind ofly carries out building-up reactions for raw material, the present invention is with acetone and Virahol by a certain percentage for raw material carries out building-up reactions, and both have any different.
Embodiment
Explain further by way of example below and coproducing methyl isobutyl ketone of the present invention and diisobutyl ketone method are described, but method of the present invention is not limited to cited embodiment.
Embodiment 1
The trade mark XH-A-69 catalyzer that ZheJiang XinHua Chemical Engineering Co., Ltd is own is housed in the reactor, its composition and mass content are: copper content is 0.5 ~ 15%, and palladium content is 0.05 ~ 0.1%, and zirconium content is 0.1 ~ 1.5%, Zn content is 0.3 ~ 5%, and aluminum oxide is gama-alumina.
Temperature of reaction is 145 DEG C, and reaction pressure is 0.5MPa, and Virahol liquid hourly space velocity is 0.5L Virahol/(L catalyzer hour), acetone: the mol ratio of Virahol is 1:1.Reaction result: iso-propanol conversion rate 53%, hexone selectivity 65%, diisobutyl ketone selectivity about 33%.Wherein reacted mixed solution sepn process is specific as follows:
(1) from reaction mixture, unreacted acetone is separated:
Reaction mixture is entered lightness-removing column, through rectifying separation, from the unreacted acetone of overhead extraction, is mixed with raw material acetone by return line, obtain the still liquid removing acetone from tower reactor;
(2) from Separation of Water the still liquid removing acetone:
The still liquid removing acetone step (1) obtained sends into dehydration tower, and through rectifying separation, from dehydration overhead extraction isopropyl alcohol and water, tower reactor obtains dehydrating kettle liquid, and the logistics of overhead extraction obtains Virahol through Separation of Water;
(3) hexone is separated:
Dehydrating kettle liquid step (2) obtained sends into hexone tower, and through rectifying separation, from the overhead extraction hexone product of hexone tower, tower reactor obtains the still liquid based on diisobutyl ketone;
(4) diisobutyl ketone is separated:
The still liquid based on diisobutyl ketone step (3) obtained sends into diisobutyl ketone tower, and through rectifying separation, from overhead extraction diisobutyl ketone product, tower reactor obtains heavy constituent.
Embodiment 2
Use catalyzer with embodiment 1 in reactor.
Temperature of reaction is 170 DEG C, and reaction pressure is 1.8MPa, and Virahol liquid hourly space velocity is 1.2L Virahol/(L catalyzer hour), acetone: the mol ratio of Virahol is 2:1.Reaction result: iso-propanol conversion rate 70%, hexone selectivity 70%, diisobutyl ketone selectivity about 26%.Reacted mixed solution sepn process is concrete identical with embodiment 1.
Embodiment 3
The composition of catalyzer and mass content is used to be in reactor: copper content is 3%, and palladium content is 0.05%, and zirconium content is 1.0%, and Zn content is 2.3%, and aluminum oxide is gama-alumina, is magnesium oxide modified aluminum oxide, and content of magnesia is 5% in alumina supporter.
Temperature of reaction is 150 DEG C, and reaction pressure is 1.5MPa, and Virahol liquid hourly space velocity is 1.0L Virahol/(L catalyzer hour), acetone: the mol ratio of Virahol is 4:1.Reaction result: iso-propanol conversion rate 82%, hexone selectivity 78%, diisobutyl ketone selectivity about 19%.Reacted mixed solution sepn process is concrete identical with embodiment 1.
Embodiment 4
The composition of catalyzer and mass content is used to be in reactor: copper content is 5%, and palladium content is 0.09%, and zirconium content is 1.2%, and Zn content is 1.5%, and aluminum oxide is gama-alumina, is magnesium oxide modified aluminum oxide, and content of magnesia is 3% in alumina supporter.
Temperature of reaction is 200 DEG C, and reaction pressure is 2.5MPa, and Virahol liquid hourly space velocity is 1.8L Virahol/(L catalyzer hour), acetone: the mol ratio of Virahol is 5:1.Reaction result: iso-propanol conversion rate 96%, hexone selectivity 78%, diisobutyl ketone selectivity about 12%.Reacted mixed solution sepn process is concrete identical with embodiment 1.
Embodiment 5
The composition of catalyzer and mass content is used to be in reactor: copper content is 12%, and palladium content is 0.1%, and zirconium content is 0.7%, and Zn content is 4.3%, and aluminum oxide is gama-alumina, is magnesium oxide modified aluminum oxide, and content of magnesia is 7% in alumina supporter.
Temperature of reaction is 170 DEG C, and reaction pressure is 1.5MPa, and Virahol liquid hourly space velocity is 1.0L Virahol/(L catalyzer hour), acetone: the mol ratio of Virahol is 4:1.Reaction result: iso-propanol conversion rate 93%, hexone selectivity 71%, diisobutyl ketone selectivity about 25.0%.Reacted mixed solution sepn process is concrete identical with embodiment 1.
Claims (4)
1. the co-production of a hexone and diisobutyl ketone, it is characterized in that, raw material acetone and Virahol are through mixing and preheating, enter in the reactor that copper-palladium-zirconium-zinc/aluminium oxide catalyst is housed, at temperature of reaction 130 ~ 210 DEG C, reaction pressure 0.1 ~ 4.0MPa, Virahol liquid phase air speed 0.1 ~ 2.5h
-1and under the reaction conditions of keto-alcohol mol ratio 1 ~ 7, acetone and Virahol generate the reaction mixture based on hexone and diisobutyl ketone through reaction, obtain hexone product and diisobutyl ketone product through separation and purification;
In described copper-palladium-zirconium-zinc/aluminium oxide catalyst, alumina supporter is the aluminum oxide of alkaline earth metal oxide modification, wherein with overall catalyst weight gauge, copper content is 0.5 ~ 15%, palladium content is 0.05 ~ 0.1%, zirconium content is 0.1 ~ 1.5%, Zn content is 0.3 ~ 5%, and aluminum oxide is gama-alumina;
The sepn process of each component is:
(1) from reaction mixture, unreacted acetone is separated:
Reaction mixture is entered lightness-removing column, through rectifying separation, from the unreacted acetone of overhead extraction, is mixed with raw material acetone by return line, obtain the still liquid removing acetone from tower reactor;
(2) from Separation of Water the still liquid removing acetone:
The still liquid removing acetone step (1) obtained sends into dehydration tower, and through rectifying separation, from dehydration overhead extraction isopropyl alcohol and water, tower reactor obtains dehydrating kettle liquid, and the logistics of overhead extraction obtains Virahol through Separation of Water;
(3) hexone is separated:
Dehydrating kettle liquid step (2) obtained sends into hexone tower, and through rectifying separation, from the overhead extraction hexone product of hexone tower, tower reactor obtains the still liquid based on diisobutyl ketone;
(4) diisobutyl ketone is separated:
The still liquid based on diisobutyl ketone step (3) obtained sends into diisobutyl ketone tower, and through rectifying separation, from overhead extraction diisobutyl ketone product, tower reactor obtains heavy constituent.
2. co-production according to claim 1, is characterized in that, reaction pressure is 0.5 ~ 2.5MPa, Virahol liquid phase air speed is 0.5 ~ 2.0h
-1.
3. co-production according to claim 1, is characterized in that, aluminum oxide is magnesium oxide modified aluminum oxide, and in alumina supporter, content of magnesia is 0.2 ~ 7%.
4. co-production according to claim 3, is characterized in that, in alumina supporter, content of magnesia is 0.4 ~ 3.5%.
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| CN110903179B (en) * | 2018-09-17 | 2022-05-24 | 中国石油化工股份有限公司 | Method for synthesizing acetone condensation compound by acetone and hydrogen |
| CN111375393A (en) * | 2018-12-29 | 2020-07-07 | 中国石油化工股份有限公司 | Alumina carrier and preparation method and application thereof |
| CN110054555A (en) * | 2019-03-14 | 2019-07-26 | 镇江李长荣高性能材料有限公司 | A kind of purification isobutyrone Product Process and its equipment |
| CN116253631A (en) * | 2023-02-15 | 2023-06-13 | 宁波宁咨绿色发展有限公司 | Rectification process for synthesizing methyl isobutyl ketone by energy-saving acetone one-step method |
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| CN101376623A (en) * | 2007-08-31 | 2009-03-04 | 中国石油天然气股份有限公司 | Separation method of methyl isobutyl ketone synthetic liquid |
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