CN103785416B - A kind of hydrogenation of carboxylic acids catalyst, preparation method and application thereof - Google Patents
A kind of hydrogenation of carboxylic acids catalyst, preparation method and application thereof Download PDFInfo
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Abstract
The present invention relates to a kind of hydrogenation of carboxylic acids catalyst, this catalyst contains carrier, cobalt element, alkali earth metal, IB race element, wherein the content of cobalt element accounts for the 15wt% ~ 50wt% of overall catalyst weight, the content of alkali earth metal accounts for the 1wt% ~ 30wt% of overall catalyst weight, the content of IB race element accounts for the 0.1wt% ~ 15.0wt% of overall catalyst weight, described carrier is oxide, and its content accounts for the 10wt% ~ 80wt% of overall catalyst weight.This catalyst activity is higher, and object selectivity of product is high; Manufacturing cost is comparatively cheap; Reaction condition is gentleer.
Description
Technical field
The invention belongs to petrochemical field.More particularly, relating to a kind of can be Catalysts and its preparation method and the application of alcohol by carboxylic acid height yield hydro-conversion.
Background technology
The research that hydrogenation of carboxylic acids prepares alcohol is long-standing, has just applied for using the method that Carboxylic Acid is alcohol by ruthenium catalyst as far back as nineteen fifty Ford etc.But because petroleum resources cost in last century is comparatively cheap and the mankind are lower to sustainable development attention degree, therefore the production of alcohols adopts the technology such as olefin hydration, oxidation-hydration more.After entering 21 century, along with the large-scale development to renewable system and oil replacement resource (coal, natural gas, shale gas, coal bed gas) etc., hydrogenation of carboxylic acids prepares alcohol to be become and has more economy and continuable method.
The main technical difficulty that hydrogenation of carboxylic acids prepares alcohol is to develop has high activity and optionally catalyst, the reaction pressure needed for reduction, and catalyst needs to have the long-time stability used; The cost of catalyst needs in rational scope, to ensure its commercial value in addition.
US4104478 discloses a kind of hydrogenation of carboxylic acids catalyst and application process thereof, the catalyst used is M-rhenium bimetallic catalyst, M is the one in ruthenium, rhodium, platinum and palladium, under the condition of 170 ~ 250 DEG C and 2.0 ~ 14.0MPa, is fatty alcohol by corresponding Carboxylic Acid.But reaction pressure is high all in the extreme in the embodiment disclosed, be all greater than 7.0MPa.
US4517391 discloses the catalyst that a kind of acetic acid gas phase hydrogenation prepares ethanol, and catalyst contains the cobalt being no less than 50wt%, one or more in Yi Jitong, manganese, molybdenum, chromium and phosphoric acid.In unique embodiment, cobalt content is more up to 70%, and the reaction pressure of use is 300bar, and ethanol yield is 97%.This proprietary catalysts cobalt tenor is high, but owing to not using noble metal, cost has certain advantage, but this catalyst activity is lower, ethanol yield is 0.09kg/kgCat/h only, consider catalyst cost still higher, and reactor will be very huge, therefore do not there is commercialization and be worth.The simultaneously content of incoagulability gas phase in the unexposed tail gas of embodiment, and material yield is lower than theoretical value.
CN1008088 discloses the loaded catalyst that a kind of hydrogenation of carboxylic acids prepares alcohol, and the first component of catalyst is tungsten and molybdenum, and second component is the one in palladium, ruthenium and platinum, and carrier is active carbon.This catalyst contains the noble metal of 1 ~ 10wt%, with high costs; And reaction velocity is lower, the LHSV in embodiment is only 0.35h
-1, mean that space-time yield is lower than 0.26kg/m
3cat/h, reaction pressure is in an embodiment about 1.0Mpa.
CN201110104763.7 and CN201110103802.1 discloses a kind of acetic acid hydrogenation catalyst and application process thereof, first active component of catalyst is tungsten and molybdenum, second component is the one in ruthenium, rhodium, platinum and palladium, carrier is active carbon or graphite, in embodiment disclosed in it, reaction pressure is 7.0 ~ 10.0MPa.
At Aqueous-phasehydrogenationoflacticacidtopropyleneglycol, in AppliedCatalysisA:General219 (2001) 89-98, Zhang etc. have studied lactic acid aqueous phase Hydrogenation for propane diols, the ruthenium catalyst of working load and trickle bed reactor, wherein water content is generally the water of 40 ~ 80%.In the method, the energy consumption when water of high level significantly can increase separation undoubtedly; The Ru/C that the catalyst used is 5wt%, high catalyst cost makes it be not suitable for commercial operation.
CN102149662 discloses a kind of Co catalysts for acetic acid hydrogenation, and the load capacity of cobalt lower than 20wt%, and also contains palladium and the platinum of about 1wt% in catalyst.Cobalt content is all lower than 10wt% in the embodiment disclosed.
US7863489 discloses a kind of acetic acid hydrogenation catalyst, and catalyst activity component is platinum, and auxiliary agent is tin.Acetic acid can be converted into ethanol with higher yield by catalyst, but platinum content is higher, and in the embodiment announced, platinum content is more than 1wt%.As everyone knows, the price of platinum is very expensive and reserves are very limited, and the cost of catalyst therefore will be made in commercial applications high.Same problem is also present in another patent US7608744, and Co catalysts content is lower, is about 10wt%, and catalyst needs to use precious metal additive simultaneously, and as platinum and palladium, auxiliary agent content is higher than 1wt%.
In sum, there is some technology and commercialization problem in prior art: catalyst is with high costs and produce that the raw material supplying amount of catalyst is limited, space-time yield is low, selective lower, reaction pressure is higher makes that operating condition is too harsh, energy consumption is too high.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of cobalt metallic catalyst containing alkaline-earth metal and IB race metal promoter and preparation method thereof and its application in monocarboxylic acid hydrogenation, and this catalyst activity is higher, and object selectivity of product is high; Manufacturing cost is comparatively cheap; Reaction condition is gentleer.
An object of the present invention is to provide a kind of hydrogenation of carboxylic acids catalyst, it is characterized in that catalyst contains carrier, cobalt element, alkali earth metal, IB race element, wherein the content of cobalt element accounts for the 15wt% ~ 50wt% of overall catalyst weight, the content of alkali earth metal accounts for the 1wt% ~ 30wt% of overall catalyst weight, the content of IB race element accounts for the 0.1wt% ~ 15.0wt% of overall catalyst weight, described carrier is oxide, and its content accounts for the 10wt% ~ 80wt% of overall catalyst weight.
Detailed description of the present invention:
The main active component of catalyst of the present invention is cobalt, and wherein cobalt tenor accounts for the 15wt% ~ 50wt% of overall catalyst weight, and preferred content is 20 ~ 40wt%, and described cobalt tenor refers to the content of element cobalt.Those skilled in the art often think that the content improving main active component can improve the activity of catalyst, but inventor is surprised to find that: lower compared with the activity of catalyst during low cobalt content, and more the cobalt of high-load not only makes the cost increase of catalyst, and the activity of catalyst can not be improved, decline even to some extent, significantly decrease when high level; Increase in the preparation difficulty of cobalt content higher than catalyst when 50wt%, as forming process etc., this will make the commercialization of catalyst comparatively difficult.The source of cobalt metal can be selected from water miscible nitrate, sulfate, villaumite, acetate, oxalates and bromine salt, specifically, be selected from cobalt nitrate, cobalt chloride, cobalt oxalate, cobaltous sulfate, cobalt acetate one or more, be more preferably in cobalt nitrate, cobalt acetate and cobalt oxalate one or more.
Described catalyst also containing alkaline earth metal component, alkali earth metal be selected from calcium, magnesium and barium one or more, its content accounts for the 1wt% ~ 30wt% of overall catalyst weight, and preferred content accounts for the 5wt% ~ 25wt% of overall catalyst weight.Alkaline-earth metal source can be water miscible nitrate, carbonate, villaumite, phosphate, sulfate, acetate, fluoride, hydroxide etc.Particular compound is as one or more in calcium nitrate, calcium dihydrogen phosphate, magnesium nitrate, magnesium phosphate, barium nitrate.
Described catalyst another must component be IB race metallic element, it accounts for the 0.1wt% ~ 15.0wt% of overall catalyst weight, and preferred content is the 0.5wt% ~ 10wt% accounting for overall catalyst weight.IB race metallic element is preferably at least one in silver and copper.Appropriate IB race metallic element add the activity drastically increasing catalyst, selective and stability.
Containing oxide component in described catalyst, its content accounts for the 10wt% ~ 80wt% of overall catalyst weight.Described oxide component be selected from silica, zirconia, titanium oxide one or more, preferential oxidation silicon.These oxides mainly play the effect of carrier, not only play a supporting role, and can also assist the dispersion of active component or the activation of carboxylic acid.Therefore these carriers affect structural behaviour, the critical index such as product and raw material diffusion wherein, mechanical strength, activity and stability of catalyst.
Described silica support can be selected from waterglass precipitate method, SiO 2 powder, teos hydrolysis, Ludox etc.It is raw material that described waterglass precipitate method refers to waterglass, adds acidic precipitation agent or ion precipitation agent, as sulfuric acid, hydrochloric acid, nitric acid, acetic acid, calcium nitrate, zirconyl nitrate, zirconium oxychloride, magnesium nitrate, cobalt nitrate etc. in waterglass.Precipitating reagent adds rear formation white gum thing, washs the precipitation method using or carry out on this basis other components for several times and adds.After described SiO 2 powder is dry after can passing through chemical deposition, waterglass precipitate, the method such as ball milling acquisition or Ludox spraying dry obtains, and its size is selected from 10nm ~ 500 μm; As the gross porosity microballoon silica that Haiyang Chemical Plant, Qingdao produces, average pore size is 8.0 ~ 12.0nm, and specific area is 300 ~ 600m2/g, and pore volume is 0.8 ~ 1.1ml/g; The and for example precipitated silica of Guangzhou people chemical plant production, dioxide-containing silica %>=95.0, fineness (325 screen residue) %≤1.8, specific area is 400 ~ 600m
2/ g or active carbon white; The and for example aerosil AEROSIL200 of goldschmidt chemical corporation, its specific surface is 200m
2/ g; And for example make the silicon dioxide microsphere that spraying dry obtains by oneself, specific surface is 400 ~ 500m
2/ g, is of a size of 2 ~ 30 μm.SiO 2 powder can add as carrier in precipitation or deposition-precipitation.Ethyl orthosilicate prepares in catalyst of the present invention in sol-gel process to use.Ludox, as liquid-state silicon source, can directly use in the precipitation system entering precipitation, deposition-precipitation.
Described Zirconia carrier is selected from powder zirconia material or is obtained by the precipitation of zirconates.Powder zirconia size is selected from 10nm ~ 500 μm, and specific surface is greater than 20m
2/ g.The sediment of zirconates can realize according to following approach: be first dissolved in water by zirconium oxychloride, add the highly basic such as caustic soda subsequently, finally by gel that sediment washing and filtering obtains; Or use zirconyl nitrate as zirconium source, the gel that after adding caustic soda precipitation, washing and filtering obtains.Above-mentioned gel is joined in other sediments, or the carrier that above-mentioned gel is worn into as deposition-precipitation after powder after super-dry is added.
Titanium dioxide carrier in the present invention can be commercially available titanium dioxide, as the P25 of goldschmidt chemical corporation, also the method for liquid-phase precipitation can be adopted to prepare, as adopted titanium tetrachloride or titanium sulfate as titanium source, add urea, ammoniacal liquor, sodium carbonate or caustic soda etc. as precipitating reagent, organic metatitanic acid also can be adopted as butyl titanate hydrolysis preparation.
Described catalyst can also contain thulium, and its oxide content accounts for the 0.1wt% ~ 8wt% of catalyst total amount; Described thulium selects the one in lanthanum or cerium, and its oxide content preferably accounts for the 0.5wt% ~ 5wt% of catalyst total amount.The rare earth element adding trace can reduce incoagulable gas content and make the selective raising obtained to a certain extent of Co catalysts.
Described catalyst can also contain one or more inorganic non-metallic elements, and content accounts for the 0.1wt% ~ 5wt% of catalyst total amount.Specifically, described inorganic non-metallic element is selected from the one in phosphorus, boron, fluorine, and content accounts for the 0.3wt% ~ 2wt% of catalyst total amount.Adding of these inorganic non-metallic elements, what have enters catalyst system along with adding of other auxiliary agents, as potassium fluoride.Have plenty of and added by extra mode, add the mode that can adopt and be added by boric acid aqueous solution in filter cake as boron.
The preparation method of described catalyst is selected from least one in coprecipitation, deposition-precipitation, the steaming ammonium precipitation method and sol-gel process.Coprecipitation, deposition-precipitation and sol-gel process Kaolinite Preparation of Catalyst are well known to those skilled in the art as existing mature technology, detailed introduction is all had in the books of this area, as Huang Zhongtao " the industrial catalyst design and development " shown, " PreparationofSolidCatalysts " that professor GerhardErtl etc. show.
The concise and to the point step of steaming the ammonium precipitation method is as follows: cobalt salt and IB race dissolving metal salts are dissolved in the water by (1) in water, also may contain other metals or non-metal salt; (2) ammoniacal liquor is progressively added in above-mentioned salting liquid, form complex compound with ammonia, as cuprammonium complex, cobalt ammonium complex compound, silver-colored ammonium complex compound etc.; (3) other components are added, such as carrier and alkaline earth metal component; (4) heat up and progressively evaporated by ammonia, cobalt and other components precipitate get off; (5) wash, filter; (6) dry, roasting.Above-mentioned steps just lists some steps necessarys wherein, and order does not have strict requirement, and professional and technical personnel can add some steps as required or change the essence that number of times does not change invention.
The feed postition of alkali earth metal can be selected from any one under type: add after dissolving together with cobalt salt in precipitation, deposition-precipitation or sol-gel process; Add respectively with cobalt salt in precipitation, deposition-precipitation, the steaming ammonium precipitation method or sol-gel process; Add in catalyst precursor, as in filter cake after the drying that obtains in precipitation, deposition-precipitation, the steaming ammonium precipitation method or sol-gel or xerogel, or in material after Roasting Decomposition; Or add beating the formative stage such as sheet or extrusion.
Another object of the present invention is to provide a kind of method above-mentioned catalyst application being prepared alcohol in hydrogenation of carboxylic acids.Specifically, be monocarboxylic acid is gasified and mixes with hydrogen, or enter in hydrogenation reactor after monocarboxylic acid is gasified in hydrogen, and be converted into fatty alcohol and water with catalyst exposure of the present invention.
The reactor of Catalyst packing is fixed bed reactors, preferred shell and tube reactor.Specifically, be by Catalyst packing in pipe, and filling heat-conducting medium between pipe, as conduction oil or water etc., be more conducive to shifting out of reaction heat like this.Those skilled in the art all knows this technical key point, as every root pipe loadings need be consistent.
Catalyst of the present invention is when being applied in hydrogenation of carboxylic acids, need by its fully reduction activation make most cobalt all be reduced to zero valence state before carrying out hydrogenation reaction, the mode of activation can be under Elevated Temperature Conditions, pass into hydrogen, use reducing agent as Boratex etc. or the method adopting ionizing radiation.These methods are all known by those skilled in the art.
Method of hydrotreating of the present invention, reaction temperature is 180 ~ 350 DEG C, is more preferably 220 ~ 300 DEG C, less in the selective change of this scope inner catalyst, maintains higher level.When reaction temperature is lower, Carboxylic Acid leads lower, and this makes circulating consumption increase; And during reaction temperature continuation rising, the accessory substance especially amount of incoagulable gas product as ethane significantly increases.
Monocarboxylic acid hydrogenation is prepared as to the reaction of alcohol, hydrogen gas consumption and monocarboxylic mol ratio are 2 in theory, but for maintaining subsequent reactions pressure and catalyst life, hydrogen and monocarboxylic molar ratio are 4:1 ~ 40:1, more ratio of greater inequality is 6:1 ~ 25:1, and further Optimal Ratio is 8:1 ~ 20:1.From reactor thick product out after gas-liquid separator, excessive hydrogen can recycle.
Catalyst choice of the present invention is higher, therefore incoagulable gas selective lower than 15% in accessory substance, lower than 10% when more excellent, lower than 5% in further optimization situation.
The reaction pressure of method of hydrotreating of the present invention is 0.3 ~ 8.0MPa, and preferred reaction pressure is 0.5 ~ 4.0MPa, and the reaction pressure optimized further is 1.0 ~ 2.5MPa.The reaction pressure that the present invention uses, relative to reaction pressure disclosed in many hydrogen addition technologies is much lower before, this makes reaction condition gentleer, and reduces cost.
In method of the present invention, monocarboxylic volume space velocity is 0.1 ~ 5.0h
-1; Preferred volume space velocity is 0.2 ~ 2.0h
-1.Air speed is actual is wish that extraction product composition is relevant with later separation ability according to factory, the present invention is not restricted in force, this be due to: when air speed is higher, although acetic acid conversion ratio is lower, but the productive rate of ethanol and ethyl acetate and increasing on the contrary, particularly ethyl acetate is selective can improve; When air speed is lower, acetic acid conversion ratio is high, but the productive rate of ethanol may reduce, therefore for having separating power and wishing the factory of voluminous ethyl acetate, high-speed operator scheme can be adopted, and for the less factory of later separation ability, low-speed can be adopted to operate.Catalyst of the present invention, at 0.3 ~ 1.0h
-1in can ensure that the conversion ratio of acetic acid is higher than 50%, preferred higher than 75%, preferred higher than 90% further.
Catalyst of the present invention can be widely used in monocarboxylic acid hydrogenation and be prepared as alcohol, and specifically, described monocarboxylic acid is selected from one in acetic acid, propionic acid, butyric acid, lactic acid, 3-hydracrylic acid, itaconic acid or mixture.These carboxylic acids derive from reproducible biomass resource, as mix acid liquors etc. such as lactic acid, 3-hydracrylic acid, benzoic acid, acetic acid/propionic acid, also can derive from other oil replacement resources, as acetic acid.Preferred, described monocarboxylic acid is one in acetic acid and propionic acid or mixture.Preferred monocarboxylic acid is acetic acid further.
Method of the present invention, when after monocarboxylic acid and hydrogen and catalyst exposure, product, except alcohol, also has other accessory substances of trace, is mainly derived from (1) decarboxylation/decarbonylation product and comprises carbon monoxide, carbon dioxide, alkane; (2) ketonization product; (3) alkyd/aldehyde condensation products; (4) dehydration product etc.For example, for acetic acid preparation of ethanol through hydrogenation, product, except primarily of except ethanol and ethyl acetate, also has acetaldehyde, ether, butanols, acetone, isopropyl alcohol, dimethoxym ethane, methane, ethane, propane, carbon monoxide, carbon dioxide etc.The catalyst that the present invention describes and application thereof can ensure that Carboxylic Acid is that total selection rate of alcohol and corresponding ester is greater than 70%, and situation of more optimizing is greater than 85%, and situation about optimizing further is greater than 90%.
Relative to prior art, hydrogenation of carboxylic acids catalyst of the present invention and application thereof have the following advantages:
(1) catalyst activity is higher, and object selectivity of product is high;
(2) catalyst manufacturing cost is comparatively cheap, and investment and operating cost are reduced;
(3) reaction condition is gentleer, can run under wider operation condition, broadening action pane.
Detailed description of the invention
With embodiment, the present invention is described below, but and unrestricted invention scope.
Embodiment 1
Get the cobalt nitrate aqueous solution 0.8 liter of 1.5mol/L, add silver nitrate 2.0 grams and copper nitrate 5.8 grams wherein, after fully dissolving, add concentrated ammonia liquor when high degree of agitation (containing NH
3mass percent is about 28%) 0.6L, form transparent complex solution.Be warming up to 70 DEG C, constant temperature is after 2 hours, join lentamente in the sodium silicate solution of 500g dilution (dioxide-containing silica is about 10wt%), drip calcium nitrate solution 100ml(calcium nitrate concentration 1.0mol/L again at above-mentioned slurry species), and continue to stir constant temperature 12 hours.By above-mentioned slurry thing filtration washing, and dried overnight obtains dry cake.Shaping by beating sheet after filter cake Roasting Decomposition, obtain catalyst CHZ-41.
Embodiment 2
Get the cobalt nitrate aqueous solution 1 liter of 0.4mol/L, add four water-calcium nitrate 23.6 grams and lanthanum nitrate 4.33g wherein, precipitated silica 40g(dioxide-containing silica %>=95.0 that people chemical plant, Guangzhou produces are added after stirring, fineness (325 screen residue) %≤1.8, specific area is 400 ~ 600m
2/ g).After being warming up to 40 DEG C, add the soda lye of 10wt%, Real-Time Monitoring solution pH value, when solution pH value stops about 7.5 time entering soda lye, and stir after adding the diatomite of 10g, be warming up to 70 DEG C of washings after aging three hours subsequently to without sodium ion.By slurry by filtration, and filtration cakes torrefaction is spent the night.Decompose under 450 DEG C of conditions after 5 hours and obtain catalyst precursor.Get above-mentioned presoma 80g, add the silver nitrate aqueous solution (argentiferous is 50mg/ml) of about 10ml wherein, beat sheet shaping acquisition catalyst CHZ-42 subsequently.
Comparative example 1
Get 30 grams of silica supports (Haiyang Chemical Plant, Qingdao, water absorption rate is about 0.9g/g), by 60 grams of cobalt nitrates and 1g silver nitrate soluble in water, prepare presoma by the method combining repeatedly dipping-total immersion stain-incipient impregnation, and by this presoma 400 DEG C of roastings acquisition catalyst CHZ-43.
Comparative example 2
According to method disclosed in CN200980134837.2, prepared the silicon dioxide carried cobalt-platinum catalyst of a calcium modification, cobalt loading is 10wt% and platinum load capacity 0.85wt%.This catalyst is CHZ-44.
Embodiment 3
Evaluated in fixed bed reactors by above-mentioned catalyst, for acetic acid preparation of ethanol through hydrogenation, loadings is 10ml, adopt the quartz sand dilution of 1:1, before use adopt pure hydrogen reduction, reduction maximum temperature be 450 ~ 500 DEG C, concrete reaction condition and reaction result as shown in table 1.
In the present embodiment, acetic acid conversion ratio and ethanol selectivity calculate according to the carbon molar content of each component and obtain.
Other products have: acetaldehyde, ethane, methane, carbon monoxide, carbon dioxide, acetic acid aldehyde, acetone, propyl alcohol etc.;
Table 1 reaction condition and result
As can be seen from Table 1, catalyst activity of the present invention is high, selective height.
Embodiment 4
Above-mentioned catalyst is evaluated in fixed bed reactors, for lactic acid (the 20wt% aqueous solution) Hydrogenation for 1,2-propane diols, loadings is 10ml, adopt the quartz sand dilution of 1:1, before use adopt pure hydrogen reduction, reduction maximum temperature be 450 ~ 500 DEG C, concrete reaction condition and reaction result as shown in table 2.
In the present embodiment, rotational rate of lactic acid and the selective carbon molar content according to each component of 1,2-PD calculate and obtain.Other accessory substances comprise: normal propyl alcohol, isopropyl alcohol, 2-hydroxy-propionaldehyde, propane, ethane, carbon monoxide, carbon dioxide, ethanol, pentanedione etc.
Table 2 reaction condition and result
As can be seen from Table 2, catalyst activity of the present invention is high, selective height.
Claims (20)
1. a hydrogenation of carboxylic acids catalyst, it is characterized in that catalyst contains carrier, cobalt element, alkali earth metal, IB race element, wherein the content of cobalt element accounts for the 15wt% ~ 50wt% of overall catalyst weight, the content of alkali earth metal accounts for the 1wt% ~ 30wt% of overall catalyst weight, the content of IB race element accounts for the 0.1wt% ~ 15.0wt% of overall catalyst weight, described carrier is selected from least one in silica, zirconia, titanium oxide, and its content accounts for the 10wt% ~ 80wt% of overall catalyst weight.
2. hydrogenation of carboxylic acids catalyst according to claim 1, it is characterized in that described alkali earth metal is at least one in calcium, magnesium and barium, its content accounts for the 5wt% ~ 25wt% of overall catalyst weight.
3. hydrogenation of carboxylic acids catalyst according to claim 2, is characterized in that described alkali earth metal derives from water miscible nitrate, carbonate, villaumite, phosphate, sulfate, acetate, fluoride, hydroxide.
4. hydrogenation of carboxylic acids catalyst according to claim 3, it is characterized in that described alkali earth metal derives from water miscible calcium nitrate, calcium dihydrogen phosphate, magnesium nitrate, magnesium phosphate, barium nitrate one or more.
5. hydrogenation of carboxylic acids catalyst according to claim 1, it is characterized in that described IB race element be silver and copper at least one, its content accounts for the 0.1wt% ~ 15.0wt% of overall catalyst weight.
6. hydrogenation of carboxylic acids catalyst according to claim 1, it is characterized in that the source of described cobalt element is selected from water miscible nitrate, sulfate, villaumite, acetate, oxalates and bromine salt, its content accounts for the 20wt% ~ 40wt% of overall catalyst weight.
7. hydrogenation of carboxylic acids catalyst according to claim 6, is characterized in that the source of described cobalt element is selected from least one in water miscible cobalt nitrate, cobalt chloride, cobalt oxalate, cobaltous sulfate, cobalt acetate.
8. hydrogenation of carboxylic acids catalyst according to claim 7, is characterized in that the source of described cobalt element is selected from least one in water miscible cobalt nitrate, cobalt oxalate, cobalt acetate.
9. hydrogenation of carboxylic acids catalyst according to claim 1, is characterized in that described carrier is selected from silica.
10., according to the hydrogenation of carboxylic acids catalyst one of claim 1,2,5,6 Suo Shu, it is characterized in that described catalyst also containing thulium, its oxide content accounts for the 0.1wt% ~ 8wt% of catalyst total amount.
11. hydrogenation of carboxylic acids catalyst according to claim 10, it is characterized in that described thulium is lanthanum or cerium, its oxide content accounts for the 0.5wt% ~ 5wt% of catalyst total amount.
12. according to the hydrogenation of carboxylic acids catalyst one of claim 1,2,5,6 Suo Shu, and it is characterized in that described catalyst also containing at least one inorganic non-metallic element, its content accounts for the 0.1wt% ~ 5wt% of catalyst total amount.
13. hydrogenation of carboxylic acids catalyst according to claim 12, it is characterized in that described inorganic non-metallic element is selected from the one in phosphorus, boron, fluorine, its content accounts for the 0.3wt% ~ 2wt% of catalyst total amount.
The preparation method of the hydrogenation of carboxylic acids catalyst that one of 14. claim 1-13 are described, adopts at least one in coprecipitation, deposition-precipitation, the steaming ammonium precipitation method and sol-gel process.
15. the preparation method of hydrogenation of carboxylic acids catalyst according to claim 14, it is characterized in that the described steaming ammonium precipitation method comprise the following steps: (1) by cobalt salt and IB race dissolving metal salts in water; (2) ammoniacal liquor is progressively added in above-mentioned salting liquid, form complex compound with ammonia; (3) carrier and alkaline earth metal component is added; (4) heat up, progressively ammonia is evaporated, precipitation; (5) wash, filter; (6) dry, roasting.
The described hydrogenation of carboxylic acids catalyst of one of 16. claim 1-13 at monocarboxylic acid Hydrogenation for the application in the reaction of alcohol.
The application in the reaction of alcohol prepared by 17. hydrogenation of carboxylic acids catalyst according to claim 16 at acetic acid hydrogenation.
The application of 18. hydrogenation of carboxylic acids catalyst according to claim 16 or 17, it is characterized in that monocarboxylic acid, hydrogen-containing gas become after mist with hydrogenation of carboxylic acids catalyst exposure, be converted into alcohol and water, hydrogen and monocarboxylic molar ratio are 4:1 ~ 40:1, reaction temperature is 180 ~ 350 DEG C, reaction pressure is 0.3 ~ 8.0MPa, and monocarboxylic volume space velocity is 0.1 ~ 5.0h
-1.
The application of 19. hydrogenation of carboxylic acids catalyst according to claim 18, it is characterized in that hydrogen and monocarboxylic molar ratio are 6:1 ~ 25:1, reaction temperature is 220 ~ 300 DEG C, and reaction pressure is 0.5 ~ 4.0MPa, and monocarboxylic volume space velocity is 0.2 ~ 2.0h
-1.
The application of 20. hydrogenation of carboxylic acids catalyst according to claim 19, it is characterized in that hydrogen and monocarboxylic molar ratio are 8:1 ~ 20:1, reaction pressure is 1.0 ~ 2.5MPa, and monocarboxylic volume space velocity is 0.3 ~ 1.0h
-1.
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| US9353035B2 (en) | 2014-04-28 | 2016-05-31 | Celanese International Corporation | Process for producing ethanol with zonal catalysts |
| US9024088B1 (en) | 2014-04-28 | 2015-05-05 | Celanese International Corporation | Hydrogenation catalysts comprising a mixed oxide comprising nickel |
| US9382177B2 (en) | 2014-04-28 | 2016-07-05 | Celanese International Corporation | Hydrogenation catalysts comprising a mixed oxide comprising a promoter metal |
| US9073815B1 (en) | 2014-04-28 | 2015-07-07 | Celanese International Corporation | Hydrogenation catalysts comprising a mixed oxide and processes for producing ethanol |
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| US4104478A (en) * | 1977-11-23 | 1978-08-01 | Ashland Oil, Inc. | Catalytic hydrogenation of fatty acids |
| CN86102420A (en) * | 1985-04-13 | 1986-10-08 | Bp化学有限公司 | The method of carboxylic acid alcohols production by hydrogenation |
| CN86102452A (en) * | 1985-04-13 | 1986-12-03 | Bp化学有限公司 | By hydrogenation of carboxylic acids preparation alcohol |
| CN102149662A (en) * | 2008-07-31 | 2011-08-10 | 国际人造丝公司 | Ethanol production from acetic acid utillizing a cobalt catalyst |
| CN102451687A (en) * | 2010-10-21 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrogenation catalyst and preparation method thereof and synthesis method of ethylene glycol |
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