CN1123556C - Process for preparing ketone by dehydrogenating para-alcohol - Google Patents
Process for preparing ketone by dehydrogenating para-alcohol Download PDFInfo
- Publication number
- CN1123556C CN1123556C CN99113310A CN99113310A CN1123556C CN 1123556 C CN1123556 C CN 1123556C CN 99113310 A CN99113310 A CN 99113310A CN 99113310 A CN99113310 A CN 99113310A CN 1123556 C CN1123556 C CN 1123556C
- Authority
- CN
- China
- Prior art keywords
- alcohol
- ketone
- prepares
- processing method
- catalyzer
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The present invention discloses a process for preparing ketone from alkyl groups and naphthenic groups by dehydrogenation of secondary alcohols, which is characterized in that a composition composed of 10% to 90m% of CuO, 0% to 50m% of oxide of Zn, Mg, Cr, Mn, Fe or Ca, 5% to 40m% of Al2O3 and 0.3% to 3.0m% of alkali metal oxide is used as a catalyst, and the corresponding ketone is prepared by utilizing gas-phase dehydrogenation of alcohols. The process has the advantages that generated products of ketone have high selectivity, the used catalyst has high mechanical strength, the phenomenon of chalking is not easy to occur, the speed of carbon deposition on the surface of the catalyst is slowed down, and the single-pass running life of the catalyst is prolonged.
Description
This patent relates to the processing method that a kind of alcohol dehydrogenase prepares ketone, and especially dehydrogenating para-alcohol prepares the processing method of ketone.
Dehydrogenating para-alcohol is a kind of main method of preparation ketone compounds.Main technological process has: dehydrogenation of isopropanol system acetone; The sec-butyl alcohol dehydrogenizing preparing ethyl methyl ketone; Cyclohexanol dehydrogenation prepares pimelinketone; The Zhong Xin alcohol dehydrogenase prepares octanone etc.Above dehydrogenation reaction was once used the brass alloys catalyzer in early days, because the temperature of reaction height of its requirement is active low, developed the Zinc oxide catalyzer again, though this catalyzer has improved activity, but still need higher temperature of reaction, and selectivity and life of catalyst are not high.The main in the recent period reduction copper catalyst that adopts, this catalyzer is main catalyst component with the copper of going back ortho states, be added with metal oxides such as zinc, magnesium, chromium, calcium to improve the dispersity and the stability of copper crystallite, also can be on carriers such as aluminum oxide, diatomite, float stone with these component appendix.The temperature of reaction that this catalyzer requires is low, and selectivity is better, long service life.
In the patent in the past, for the used copper catalyst of above reaction, the patent introduction is added with the oxide compound of zinc, magnesium, calcium or chromium etc. as helping catalyst component, passes through compression molding.In the catalyzer of this type, in order to reach the catalyst activity of permission, the content of copper is quite high.But because the processability of the oxide compound of cupric oxide and zinc, magnesium, chromium etc. is poor, the catalyzer physical strength that obtains is very poor, some in addition can only provide with pulverulence, physical strength is too poor, except easy fragmentation in transporting and loading, efflorescence induces reaction the transformation efficiency reduction until the catalyzer termination in work-ing life gradually in the running use.
Chinese patent CN1056067 has introduced a kind of cyclohexanol dehydrogenation catalyst, contains CuO, ZnO, MgO, CaO and micro-Na
2O is though add Zn, Mg Ca and micro-Na
2After the O modification, can improve the selectivity of pimelinketone, but because above oxide powder processability is poor, belong to catalyzer exoskeletal, no bonding composition, the physical strength of moulding rear catalyst is low, and easily efflorescence is its shortcoming.
In order to overcome the above problems, can add some carrier or with the caking agent compression molding.If use carrier dipping copper component, in order to soak the catalyst component of enough content, carrier must have big, and the characteristics such as the avidity of metal oxide is big, physical strength height of specific surface area, as activated alumina, diatomite, zeolite etc.; If use caking agent to the metal oxide powder compression molding, then this caking agent must have with the avidity height of metal oxide powder, moulding after physical strength big, under reaction conditions, do not decompose, as aluminium hydrate powder, silicon sol etc.But these carriers or caking agent composition are condensed into higher ketone for dehydration, the ketone of alcohol very strong catalytic activity is arranged, thus simple introducing these become branches to increase the probability of side reactions, reduce main reaction product selectivity and productive rate.
As English Patent BP1,444,484 have introduced a kind of Cu-MgO-Cr
2O
3/ SiO
2Catalyzer is used for the dehydrogenation of Virahol, sec-butyl alcohol and hexalin and the hydrogenation of butyraldehyde etc.When advancing alcohol dehydrogenase merely, its selectivity to purpose product ketone is lower.As be used for sec-butyl alcohol dehydrogenizing, and when advancing alcohol merely, under 260 ℃, condition of normal pressure, the transformation efficiency of sec-butyl alcohol is more than 90%, and the selectivity of methylethylketone has only 94%.This patent prolongs the one way life-span of catalyzer operation by introduce the carbon distribution that water or nitrogen reduce by-product and catalyzer in charging alcohol.Can increase running cost but introduce the 3rd component, and increase the difficulty of product separation.
English Patent 1,500,884 introduce, and extremely atomizing silicic acid powder adds in the precipitation of hydroxide of Cu, Cr, Mg, after mixing, obtains finished catalyst behind the compression molding.The crushing force of the granules of catalyst that compressing tablet makes is 5～10Kg, and the crushing force after the reduction is 2～5Kg.This catalyzer is used for the dehydrogenation of sec-butyl alcohol, and under 260 ℃, condition of normal pressure, transformation efficiency is 85%, and the methylethylketone selectivity is 95%.The selectivity of this catalyzer dehydrogenation slightly increases, but the physical strength of catalyzer is still very low.
If adopt the inert material to prepare catalyzer, as the α-Al of macropore as carrier
2O
3, because its absorption property is very poor,, can only support very a spot of copper if support the copper metal, the temperature of reaction of requirement is very high.As United States Patent (USP) 4453015, Cu Zn Cr is dipped in the α-Al of macropore
2O
3Go up as mellow wine dehydrogenating, be used for sec-butyl alcohol dehydrogenizing, 380 ℃ of temperature of reaction are at sec-butyl alcohol charging air speed 6h
-1Under the condition, sec-butyl alcohol transformation efficiency 93.4%, the methylethylketone selectivity is 93.6%.But because temperature of reaction is too high, catalyst carbon deposition is too fast.
Also have the patent introduction to adopt precious metals such as more highly active palladium, lawrencium to be stated from α-Al
2O
3Go up as mellow wine dehydrogenating, introduce, adopt Pt/ α-Al of 0.25% as United States Patent (USP) 3981923
2O
3Be catalyzer, be used for sec-butyl alcohol dehydrogenizing, at 358 ℃, charging sec-butyl alcohol air speed 4.0h
-1Under the condition, sec-butyl alcohol transformation efficiency 93.3%, the methylethylketone selectivity is 96%, but its service temperature height, after running 300 hours, it is constant to keep transformation efficiency, and temperature has improved 10 ℃, the charging air speed reduces by one times, illustrate that catalyst carbon deposition is very fast, the life-span short, and the price of catalyzer is also high.
The purpose of this patent provides a kind of processing method of dehydrogenating para-alcohol, improves the transformation efficiency and the selectivity of reaction, and reduces the carbon distribution of catalyzer, the work-ing life of improving catalyzer.
Technical scheme of the present invention is as follows:
The secondary alcohol of the alkyl or cycloalkyl of gas phase contacts with dehydrogenation catalyst in being seated in fixed-bed tube reactor, dehydrogenation reaction takes place generate the ketone identical with the raw alcohol carbonatoms, and the reaction conditions of employing is:
Temperature of reaction: 180～350 ℃, preferably 230～280 ℃;
Reaction pressure: 0.01～0.5MPa, preferably 0.05～0.3MPa;
Volume space velocity: 0.5～10.0h during the liquid of charging alcohol
-1, 1.0～8.0h preferably
-1
The composition of dehydrogenation catalyst: with the weight percent is benchmark, and CuO10%～90% contains Al
2O
35%～40%, contain in the oxide compound of Zn, Mg, Cr, Mn, Fe one or more 0%～50%, alkali metal containing oxide compound 0.1%～5.0%.
In the above-mentioned catalyzer, the content preferable range of cupric oxide is 30%～60%; The preferable range of alumina content is 10%～30%; Alkalimetal oxide can be one or more in lithium, sodium, potassium, rubidium, the caesium oxide compound, and the preferable range of its content is between 0.3%～3.0%.In the described catalyzer, can contain in the oxide compound of zinc, chromium, magnesium, manganese, iron, calcium one or more as the case may be, also can not have, preferably contain these components, its content is preferably between 10%～45%.
The present invention is applicable to the dehydrogenation of carbonatoms at 3～15 alkyl secondary alcohol, can contain aromatic ring, ehter bond in the carbochain; Be applicable to that also carbonatoms is the dehydrogenation of the cycloalkyl alcohol between 5～10.The alcohol that is used for dehydrogenation system ketone has mainly contained Virahol, sec-butyl alcohol, hexalin, secondary octanol, phenylethyl alcohol, methyl-2-hydroxyl isopropyl ether etc.
Preparation of catalysts of the present invention, the coprecipitation method and the pickling process that can adopt those skilled in the art to know.Co-precipitation promptly is after metal ion solutions such as copper, zinc, chromium, magnesium, iron, manganese, calcium are added alkali solution precipitate, and after adding aluminium hydroxide caking agent compressing tablet or the extrusion molding, the alkalimetal oxide preparation is flooded in roasting again after the drying precipitate; Also can select an alumina carrier with certain specific surface area and definite shape, dipping is gone up cupric ion, zinc, magnesium, chromium, iron, manganese, calcium plasma and alkalimetal ion respectively, and roasting makes.
This catalyzer at first should reduce before use, and reduction is generally after catalyzer is packed reactor into, between 150～230 ℃, reduce with nitrogen and hydrogen mixture, hydrogen concentration raises gradually during reduction, it is constant to import and export hydrogen concentration to reactor, when reactor does not have water generates till.When being used for alcohol dehydrogenase, also can when 150～230 ℃ of left and right sides, directly advancing pure steam catalyzer is reduced.
For the dehydrogenation of low-carbon alcohol, because its molecule is little, the ketone of corresponding generation is easier to condensation, so as low-carbon alcohol such as Virahol and sec-butyl alcohols, the selectivity that reaches during dehydrogenation will be hanged down; It is corresponding few that the condensation of the ketone after higher alcohols and the cycloalkanol dehydrogenation is wanted, and the selectivity of dehydrogenation is higher, but the carrying out of carbon distribution reaction is more more than low-carbon alcohol, and the one way of catalyzer shortens with the carbonatoms increase of dehydrogenation feed work-ing life.
When dehydrogenation reaction is carried out to a certain degree, because the carbon distribution of catalyst surface, activity of such catalysts can reduce, be reduced to a certain degree, temperature can increase the transformation efficiency of reaction by improving temperature of reaction, but had better not surpass 300 ℃, when can not continue to raise for the use temperature of reduction copper catalyst, just must stop work, catalyzer is regenerated.The one way life-span that is called catalyzer during this period of time.Generally between 700～5000 hours, the one way life-span of catalyzer reduces with carbonatoms and increases.
The regeneration of catalyzer is to adopt nitrogen oxygen atmosphere that catalyzer is burnt carbon, during regeneration, temperature of reactor promotes gradually, the oxygen level of resurgent gases also is promoted to air concentration gradually, the speed and the concentration of oxygen of regenerative process control temperature raising, the temperature that makes the temperature rise of beds be unlikely to surpass catalyzer to allow (generally can not above 400 ℃).Reach the highest (generally being not more than 300 ℃) in regeneration temperature, air burns under the carbon situation, and beds does not have temperature rise, and the oxygen concn that reactor is imported and exported is constant, exports no CO and CO
2
Compared with prior art, the present invention has following beneficial effect:
Since selected be main active component with copper, being the catalyzer of cocatalyst component among a kind of or several in zinc, magnesium, zirconium, iron, the manganese, adopt aluminum oxide to make binding agent or carrier, has very high physical strength, and add an amount of alkali metal in the catalyzer again, a large amount of side reactions and the carbon deposit on the catalyzer have been reduced, life of catalyst obtains prolonging, and has also improved the selectivity and the transformation efficiency of reaction simultaneously.
Embodiment
Embodiment 1
A kind of catalyzer that makes by the method in the above explanation contains CuO 45m%, ZnO30m%, Al
2O
324m%, K
2O1.0m%.With this catalyzer 100ml, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 4.0h during with liquid
-1Enter sec-butyl alcohol, under 260 ℃ of temperature of reaction, normal pressure, sec-butyl alcohol dehydrogenizing prepares methylethylketone, sec-butyl alcohol transformation efficiency 87.5%, and the selectivity that generates methylethylketone is 98.40%, and by product is mainly 5-methyl-2-heptanone.Keep above reaction conditions and index, the catalyzer continous-stable turns round more than 2000 hours.
Embodiment 2
The catalyzer 100ml that embodiment 1 is identical presses certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 6.0h during with liquid
-1Enter Virahol, under 230 ℃ of temperature of reaction, normal pressure, dehydrogenation of isopropanol prepares acetone, Virahol transformation efficiency 90.5%, and the selectivity that generates acetone is 95.40%, and main by product is a methyl iso-butyl ketone (MIBK).Keep above reaction conditions and index, the catalyzer continous-stable turns round more than 3000 hours.
Embodiment 3
A kind of catalyzer that makes by the method in the above explanation contains CuO 35%, Cr
2O
335%, MgO15%, Al
2O
328%, Cs
2O2.0%.With this catalyzer 100ml, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 4.0h during with liquid
-1Enter sec-butyl alcohol, under 270 ℃ of temperature of reaction, 0.3MPa pressure, sec-butyl alcohol dehydrogenizing prepares methylethylketone, sec-butyl alcohol transformation efficiency 78.5%, and the selectivity that generates methylethylketone is 93.3%.
Embodiment 4
A kind of catalyzer that makes by the method in the above explanation contains CuO55%, Fe
2O
37%, MnO12%, Al
2O
324%, Na
2O2%.With this catalyzer 100ml, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 4.0h during with liquid
-1Enter sec-butyl alcohol, under 260 ℃ of temperature of reaction, normal pressure, sec-butyl alcohol dehydrogenizing prepares methylethylketone, sec-butyl alcohol transformation efficiency 85.6%, and the selectivity that generates methylethylketone is 97.3%.
Embodiment 5
A kind of catalyzer that makes by the method in the above explanation contains CuO60%, Al
2O
337%, K
2O3.0%.With this catalyzer 100ml, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 4.0h during with liquid
-1Enter sec-butyl alcohol, under 260 ℃ of temperature of reaction, normal pressure, sec-butyl alcohol dehydrogenizing prepares methylethylketone, sec-butyl alcohol transformation efficiency 88.6%, and the selectivity that generates methylethylketone is 94.8%.
Comparative example 1
The effect of alkalimetal oxide in the catalyzer is described.
A kind of catalyzer that makes by the method in the above explanation contains CuO45%, ZnO30%, Al
2O
325%, alkali metal containing oxide compound not.With this catalyzer 100ml, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 4.0h during with liquid
-1Enter sec-butyl alcohol, under 260 ℃ of temperature of reaction, normal pressure, sec-butyl alcohol dehydrogenizing prepares methylethylketone, sec-butyl alcohol transformation efficiency 88.5%, and the selectivity that generates methylethylketone is 85.40%, and the selectivity that generates 5-methyl-2-heptanone is 14%, and other are dehydration reaction..
Embodiment 6
The catalyzer 100ml that embodiment 1 is identical presses certain particle size, is loaded in the tubular reactor of internal diameter 15mm, advance nitrogen and be warming up to 150 ℃ to reactor, the back enters sec-butyl alcohol steam by 200ml per hour, is warming up to 230 ℃ of constant temperature more gradually 12 hours, with raw alcohol catalyzer is reduced.Be warming up under 260 ℃, normal pressure volume space velocity 4.0h during with liquid after the reduction
-1Enter sec-butyl alcohol, dehydrogenation prepares methylethylketone, sec-butyl alcohol transformation efficiency 88.5%, and the selectivity that generates methylethylketone is 98.6%, and is basic consistent with the nitrogen hydrogen reduction method.
Embodiment 7
Will the catalyzer 100ml identical with embodiment 1, be loaded in the tubular reactor of internal diameter 15mm, 150-200 ℃ with after the nitrogen oxygen atmosphere reduction, reactor is warming up to 260 ℃, enter the steam of the hexalin that is preheated to temperature of reaction, volume space velocity is 2.0h during the liquid of charging hexalin
-1, after the dehydrogenation reaction, the transformation efficiency of hexalin is more than 84%, and the selectivity that generates pimelinketone is greater than 99%.
Embodiment 8
Will the catalyzer 100ml identical with embodiment 1, press certain particle size, be loaded in the tubular reactor of internal diameter 15mm, in the time of 150-200 ℃ with after the nitrogen and hydrogen mixture reduction, volume space velocity 2.0h during with liquid
-1Enter 2-hydroxypropyl methyl ether (CH3OCH2CHOHCH3), at 240 ℃ of temperature of reaction volume space velocity 4.0h during with liquid
-1Enter 2-hydroxypropyl methyl ether, under the normal pressure, dehydrogenation prepares 2-carbonyl propyl group methyl ether (CH3OCH2COCH3), 2-hydroxypropyl methyl ether transformation efficiency 92.0%, and the selectivity that generates 2-carbonyl propyl group methyl ether is 94.6%.
Embodiment 9
Will the catalyzer 100ml identical with embodiment 1, be loaded in the tubular reactor of internal diameter 15mm, 150-200 ℃ with after the nitrogen oxygen atmosphere reduction, reactor is warming up to 260 ℃, enter the steam of the sec-n-octyl alcohol that is preheated to temperature of reaction, volume space velocity 2.0h during charging octanol liquid
-1, after the dehydrogenation reaction, the transformation efficiency of sec-n-octyl alcohol can reach 92%, and the selectivity that generates methyln-hexyl ketone is more than 99%.
Embodiment 10
Will the catalyzer 100ml identical with embodiment 1, be loaded in the tubular reactor of internal diameter 15mm, 150-200 ℃ with after the nitrogen oxygen atmosphere reduction, reactor is warming up to 240 ℃, enter the steam of the phenylethyl alcohol that is preheated to temperature of reaction, volume space velocity is 1.0h during benzene feed alcoholic acid liquid
-1, after the dehydrogenation reaction, the transformation efficiency of phenylethyl alcohol is 82%, the selectivity that generates methyl phenyl ketone is more than 99%.
Claims (11)
1. a dehydrogenating para-alcohol prepares the processing method of ketone, the secondary alcohol of the alkyl or cycloalkyl of gas phase contacts with dehydrogenation catalyst in being seated in fixed-bed tube reactor, dehydrogenation reaction taking place generates the ketone identical with the raw alcohol carbonatoms, it is characterized in that described reaction conditions is:
Temperature of reaction: 180～350 ℃;
Reaction pressure: 0.01～0.5MPa;
Volume space velocity: 0.5～10.0h during the liquid of charging alcohol
-1
The composition of dehydrogenation catalyst: with the weight percent is benchmark, and CuO10%～90% contains Al
2O
35%～40%, contain oxide compound or its oxide mixture 0%～50% of Zn, Mg, Cr, alkali metal containing oxide compound 0.1%～5.0%.
2. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, it is characterized in that described catalyzer consists of: with the weight percent benchmark, and CuO30%～60%; Al
2O
310%～30%; Alkalimetal oxide 0.3%～3.0%; In the oxide compound of Zn, Mg, Cr, Mn, Fe, Ca one or more 10%～45%.
3. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, it is characterized in that described catalyzer is used for reducing earlier before the dehydrogenation reaction.
4. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, and the secondary alcohol that it is characterized in that described alkyl is that carbonatoms is 3～15 secondary alcohol, can contain ehter bond or aromatic ring in the carbochain.
5. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, it is characterized in that described cycloalkyl alcohol is that carbonatoms is 5～10 cycloalkyl alcohols.
6. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, it is characterized in that described temperature of reaction is between 230～280 ℃.
7. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, and the pressure that it is characterized in that described reaction is between 0.05～0.3MPa.
8. dehydrogenating para-alcohol according to claim 1 prepares the processing method of ketone, and volume space velocity is at 1.0～8.0h when it is characterized in that the liquid of described charging alcohol
-1Between.
9. dehydrogenating para-alcohol according to claim 1 and 2 prepares the processing method of ketone, it is characterized in that described alkalimetal oxide is one or more in lithium, sodium, potassium, rubidium, the caesium oxide compound.
10. dehydrogenating para-alcohol according to claim 3 prepares the processing method of ketone, it is characterized in that described catalyst reduction is at 150～230 ℃, contacts with catalyzer with nitrogen and hydrogen mixture and finishes.
11. dehydrogenating para-alcohol according to claim 3 prepares the processing method of ketone, it is characterized in that described catalyst reduction is at 150～230 ℃, contacts with catalyzer with the raw alcohol steam and finishes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99113310A CN1123556C (en) | 1999-09-29 | 1999-09-29 | Process for preparing ketone by dehydrogenating para-alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99113310A CN1123556C (en) | 1999-09-29 | 1999-09-29 | Process for preparing ketone by dehydrogenating para-alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1289753A CN1289753A (en) | 2001-04-04 |
| CN1123556C true CN1123556C (en) | 2003-10-08 |
Family
ID=5276516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99113310A Expired - Lifetime CN1123556C (en) | 1999-09-29 | 1999-09-29 | Process for preparing ketone by dehydrogenating para-alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1123556C (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1314648C (en) * | 2002-12-19 | 2007-05-09 | 华东理工大学 | Method for preparing butanedione |
| DE102004011543A1 (en) * | 2004-03-08 | 2005-10-06 | Basf Ag | Process for the preparation of optically active carbonyl compounds |
| CN102249873A (en) * | 2011-07-26 | 2011-11-23 | 烟台大学 | Method for improving alcohol dehydrogenation conversion rate |
| CN102992984A (en) * | 2011-09-13 | 2013-03-27 | 湖南长岭石化科技开发有限公司 | Methyl ethyl ketone preparation method |
| CN103880787B (en) * | 2014-03-12 | 2016-08-24 | 江苏大学 | A kind of coupled reaction prepares the method for gamma-butyrolacton and acetone |
| CN104399474A (en) * | 2014-11-20 | 2015-03-11 | 西安近代化学研究所 | Catalyst for synthesizing methoxy acetone through alcohol dehydrogenization, preparation method and application of catalyst |
| CN105709752B (en) * | 2014-12-04 | 2018-06-19 | 中国石油化工股份有限公司 | A kind of Catalysts of Dehydrogenation Secondary Butand and its preparation method and application |
| CN106478325B (en) * | 2015-08-28 | 2019-06-25 | 南京理工大学 | A method of synthesis alpha-alkyl ketone |
| CN105195210B (en) * | 2015-09-18 | 2018-02-13 | 宁波海越新材料有限公司 | A kind of sec-butyl alcohol dehydrogenizing preparing ethyl methyl ketone catalyst and preparation method thereof |
| CN105597840B (en) * | 2015-12-16 | 2018-05-04 | 福州大学 | A kind of in-situ regeneration method for inactivating Cu-series catalyst |
| BR112020013655B1 (en) * | 2018-01-04 | 2023-05-09 | Gevo, Inc | CATALYTIC PROCESSES FOR CONVERTING CRUDE AND/OR REFINED FUSEL OIL REFINED BLENDS INTO HIGHER VALUE RENEWABLE CHEMICALS BY MIXED METAL OXIDE OR ZEOLITE CATALYST |
| CN108892607B (en) * | 2018-08-14 | 2021-12-03 | 山东新和成药业有限公司 | Preparation method of hydroxycitronellal |
| CN111320530B (en) * | 2018-12-13 | 2023-07-28 | 中国石油化工股份有限公司 | Preparation method of 1-hydroxy-2-alkanone |
| CN115677460A (en) * | 2021-07-29 | 2023-02-03 | 安徽圣诺贝化学科技有限公司 | Method for preparing citronellal by dehydrogenating citronellol |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2608596A1 (en) * | 1986-12-19 | 1988-06-24 | Charbonnages Ste Chimique | Catalytic process for the dehydrogenation of higher alcohols |
-
1999
- 1999-09-29 CN CN99113310A patent/CN1123556C/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2608596A1 (en) * | 1986-12-19 | 1988-06-24 | Charbonnages Ste Chimique | Catalytic process for the dehydrogenation of higher alcohols |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1289753A (en) | 2001-04-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1123556C (en) | Process for preparing ketone by dehydrogenating para-alcohol | |
| CN1021636C (en) | Improved aldehyde hydrogenation catalyst and process | |
| US11167280B2 (en) | Catalyst for preparing α-phenylethanol by hydrogenation of acetophenone, preparation method thereof and application thereof | |
| CN108929189B (en) | Method for preparing isopropylbenzene by hydrogenolysis of alpha, alpha-dimethyl benzyl alcohol | |
| US4751248A (en) | Preparation of alcohols from synthesis gas | |
| US5157179A (en) | Method for producing a cycloolefin | |
| CN104230640A (en) | Alpha, alpha-dimethylbenzyl alcohol hydrogenolysis method for preparing isopropyl benzene | |
| CN1597096A (en) | Catalyst used for synthesizing dimethyl carbonate from ured and methanol and its preparation method and application | |
| CN1171841C (en) | Aldol condensation | |
| US20140206527A1 (en) | Catalyst For Preparing Acrolein And Acrylic Acid By Dehydration Of Glycerin, And Its Production Process | |
| CN1230458A (en) | Catalyst for preparation of ethanol by hydrogenating acetaldehyde, ethyl acetate, acetic acid or their mixture | |
| CN1044415A (en) | The sorbent material and the method for making thereof of polyolefine purification usefulness | |
| CN1315226A (en) | Reduction treated copper-base catalyst and process for preparing alpha-phenylethyl alcohol therefrom | |
| EP0412862A1 (en) | Nickel-based adsorbens for arsenic and phosphor removal from liquid hydrocarbon fractions, its preparation and its use | |
| CN1123555C (en) | Process for preparing aldehyde and ketone by dehydrogenating alcohol | |
| CN101811042A (en) | Selective hydrogenation catalyst and preparation method and application thereof | |
| CN1446627A (en) | Catalyst in oxychlorination reaction as well as its preparation method and application | |
| CN112387268B (en) | Solid base catalyst for preparing 3-hydroxybutyraldehyde and preparation method thereof | |
| CN108947757B (en) | Method for preparing isopropylbenzene by catalytic hydrogenolysis of alpha, alpha-dimethyl benzyl alcohol | |
| CN1273567C (en) | Method of eliminating arsenic in acetylene containing hydrocarbon and dearsenic agent | |
| CN1150990C (en) | Catalyst for liquid-phase dehydogenation of cyclohexanol | |
| CN1150060C (en) | Adsorbing agent for removing carbonyl metal compound from gas and its preparation method | |
| CN1646514A (en) | Method for producing gamma-butyrolactone | |
| CN1191221C (en) | Method of preparing alpha-phenyl ethyl alcohol | |
| CN115025779B (en) | Olefin deoxidizer and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20031008 |
|
| CX01 | Expiry of patent term |