CN103787828B - A kind of method applied cobalt B catalyst and alcohol prepared by carboxylic acid gas phase hydrogenation - Google Patents

A kind of method applied cobalt B catalyst and alcohol prepared by carboxylic acid gas phase hydrogenation Download PDF

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CN103787828B
CN103787828B CN201210429959.8A CN201210429959A CN103787828B CN 103787828 B CN103787828 B CN 103787828B CN 201210429959 A CN201210429959 A CN 201210429959A CN 103787828 B CN103787828 B CN 103787828B
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carboxylic acid
alcohol
gas phase
catalyzer
acid gas
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CN103787828A (en
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黄龙
田保亮
戴伟
王国清
杨溢
彭晖
李宝芹
唐国旗
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
    • C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/894—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8946—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The present invention relates to a kind of method that hydrogenation of carboxylic acids is prepared as alcohol.In method in the present invention, the catalyzer of use is at least containing the cobalt of 10wt% ~ 40wt% and the boron of 0.5wt% ~ 15wt% that account for overall catalyst weight.By this catalyzer, under 220 ~ 300 DEG C and 0.5 ~ 4.0MPa condition, carboxylic acid can with higher than 90% be selectively converted to corresponding alcohol and ester, the catalyst activity used is high, good stability and cost is lower, and the reaction conditions used is not harsh, therefore more easily realizes commercial operation.

Description

A kind of method applied cobalt B catalyst and alcohol prepared by carboxylic acid gas phase hydrogenation
Technical field
The present invention relates to a kind of method that carboxylic acid selec-tive hydrogenation prepares alcohol, specifically, the present invention is a kind of cobalt B catalyst of application is the method for alcohol by carboxylic acid height yield hydrocracking.
Background technology
It is the important chemical reaction of a class that hydrogenation of carboxylic acids prepares alcohol, as acetic acid hydrogenation prepare ethanol, lactic acid Hydrogenation all also exists demand urgently for propylene glycol.This causes due to multiple reason: due to technique progress, cause the manufacturing cost of carboxylic acid to reduce, and if acetic acid is along with the maturation of methanol carbonyl method, manufacturing cost reduces; Or because raw material changes, make the manufacture of carboxylic acid have sustainability, as biomass derivatives such as lactic acid, 3-hydroxy-propionic acids.
The Hydrogenation of carboxylic acid is long-standing for the research of alcohol, as as far back as nineteen fifty, Ford etc. have just applied for using the method that Carboxylic Acid is alcohol by ruthenium catalyst, but because petroleum resources cost in last century is comparatively cheap and the Sustainable development attention degree of the mankind is lower, therefore the production of alcohols adopts the technology such as olefin hydration, oxidation-hydration more.After entering 21 century, people to the large-scale development of renewable system and oil replacement resource (coal, Sweet natural gas, shale gas, coal-seam gas) etc., make hydrogenation of carboxylic acids prepare alcohol become alcohols produce have more economy and continuable method.
In fact hydrogenation of carboxylic acids is prepared alcohol and is had high challenge, main technical difficulty is to develop has high reactivity and optionally catalyzer, reaction pressure needed for reduction, and catalyzer needs to have the long-time stability used, the cost of certain catalyzer needs in rational scope, to ensure its commercial value.
US4104478 discloses a kind of hydrogenation of carboxylic acids catalyzer and application method thereof, the catalyzer 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.Disclosed embodiment pressure all in the extreme high (>7.0MPa).
US4517391 discloses the catalyzer that a kind of acetic acid gas phase hydrogenation prepares ethanol, and catalyzer contains the cobalt being no less than 50wt%, one or more in Yi Jitong, manganese, molybdenum, chromium and phosphoric acid.In unique embodiment, cobalt contents is more up to 70%, and the reaction pressure of use is 300bar, and ethanol yield is 97%.Although this proprietary catalysts cobalt metal content is high, but owing to not using precious metal, cost has certain advantage, but this catalyst activity is lower, ethanol yield is 0.09kg/kg Cat/h only, consider catalyzer cost still higher, and reactor will be very huge, therefore do not there is commercialization and be worth.Simultaneously in the unexposed tail gas of embodiment the content of incoagulability gas phase and material yield lower than theoretical value.
CN1008088 discloses the loaded catalyst that a kind of hydrogenation of carboxylic acids prepares alcohol, and the first component of catalyzer is tungsten and molybdenum, and second component is the one in palladium, ruthenium and platinum, and carrier is gac.This catalyzer contains the precious metal of 1 ~ 10wt%, with high costs; And reaction velocity is lower, and (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 method thereof, first active ingredient of catalyzer is tungsten and molybdenum, second component is the one in ruthenium, rhodium, platinum and palladium, carrier is gac or graphite, in embodiment disclosed in it, reaction pressure is 7.0 ~ 10.0MPa.
Zhang etc. have studied lactic acid aqueous phase Hydrogenation for propylene glycol, the ruthenium catalyst of working load and trickle-bed reactor, wherein water-content is generally the water (Aqueous-phase hydrogenation of lactic acidto propylene glycol, Applied Catalysis A:General 219 (2001) 89-98) of 40 ~ 80%.In the method, this energy consumption when significantly can increase separation undoubtedly of water of high level; The Ru/C that the catalyzer used is 5wt%, high catalyzer cost makes it be not suitable for commercial operation.
CN102149662 discloses a kind of cobalt catalyst for acetic acid hydrogenation, and the charge capacity of cobalt lower than 20wt%, and also contains palladium and the platinum of about 1wt% in catalyzer.Cobalt contents 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 catalyzer, but platinum content is higher, 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 catalyzer therefore will be made in commercial applications high.Same problem is also present in another patent US7608744, cobalt catalyst content lower (~ 10wt%), and catalyzer needs to use precious metal additive simultaneously, and as platinum and palladium, auxiliary agent content is higher than 1wt%.
CN102149662 discloses a kind of acetic acid hydrogenation catalyst containing cobalt, preparation method is pickling process, the charge capacity of cobalt is 0.1wt% ~ 20wt%, in embodiment disclosed in it, cobalt loading is at 5wt% ~ 10wt%, and the auxiliary agent used uses precious metal additive, as platinum and palladium, auxiliary agent content is higher than 1wt%, and this will make the cost of catalyzer extremely high, or for having the chromium auxiliary agent compared with high pollution; And the transformation efficiency of acetic acid is lower, although inventor's its space-time yield unexposed, the embodiment data provided by it, can calculate its space-time yield lower, cobalt-chrome catalysts disclosed in it, and the space-time yield of ethanol is only at 82g/L/h ~ 258g/L/h.
In sum, in existing carboxylic acid technical scheme, there is some technology and commercialization problem: catalyzer is with high costs and produce that the raw material supplying amount of catalyzer is limited, space-time yield is low, selectivity is lower, reaction pressure is higher makes that operational condition is too harsh, energy consumption is too high.
Method of the present invention, under relatively mild reaction conditions, with higher yield, acetic acid can be converted into ethanol, and catalyzer has higher space-time yield and cheap manufacturing cost.
Summary of the invention
The present invention relates to and a kind ofly use the method containing the cobalt catalytic hydrogenation of boron additive, monocarboxylic acid being hydrogenated to alcohol, described catalyzer not only have active high, selectivity is high and the feature of good stability, and cost is comparatively cheap, and forms comparatively environmental protection.
A kind of carboxylic acid gas phase hydrogenation of the present invention prepares the method for alcohol, in fixed-bed reactor, carboxylic acid steam mixes with hydrogen-containing gas and is converted into alcohol and water after hydrogenation catalyst contact reacts, the mol ratio of hydrogen and carboxylic acid is 4:1 ~ 40:1, temperature of reaction is 180 ~ 350 DEG C, reaction pressure is 0.3 ~ 8.0MPa, and the volume space velocity of carboxylic acid is 0.1 ~ 5.0h -1;
Described hydrogenation catalyst comprises following component:
(1) containing cobalt and boron, wherein cobalt metal content accounts for the 10wt% ~ 50wt% of overall catalyst weight, and boron accounts for the 0.1wt% ~ 20wt% of overall catalyst weight;
(2) oxide compound; Described oxide compound be selected from silicon oxide, diatomite, Calucium Silicate powder, zirconium white, titanium oxide one or more, its content accounts for the 10wt% ~ 80wt% of overall catalyst weight;
Described hydrogenation catalyst combines preparation by one or more in co-precipitation, deposition-precipitation, ammonia still process precipitation, sol-gel and ball milling method; The described carboxylic acid for hydrogenation is monocarboxylic acid.
The detailed description of the invention is as follows:
The main active ingredient of catalyzer of the present invention is cobalt, and wherein cobalt metal content accounts for the 10wt% ~ 50wt% of overall catalyst weight, and preferred content accounts for the 15wt% ~ 45wt% of overall catalyst weight, preferably accounts for the 10wt% ~ 40wt% of overall catalyst weight further; Described cobalt metal content refers to the content of element cobalt.The content of cobalt catalyst is through that contriver carefully filters out: lower compared with the activity of catalyzer during low cobalt content when being in, this can make the ethanol space-time yield of catalyzer remain at low levels, because carboxylic acid has stronger corrodibility, therefore the reactor that its direct hydrogenation prepares alcohol generally needs the stainless material used costly, therefore makes the cost of reactor high when space-time yield is lower; And more the cobalt of high-content not only makes the cost increase of catalyzer, and the activity of catalyzer can not be improved, even make activity decline to some extent, decline obviously when cobalt contents is higher.This result is unexpected: because often it is believed that improving metal content can improve the activity of catalyzer.Further, contriver finds to increase in the preparation difficulty of cobalt contents higher than catalyzer when 50wt%, and as moulding process etc., this will make the commercialization of catalyzer comparatively difficult.
The source of cobalt metal can be selected from water miscible metal-salt as nitrate, vitriol, villaumite, acetate, oxalate and bromine salt, or is selected from cobalt metal, as cobalt metal sheet etc.Water-soluble metal salt is selected from one or more in Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, cobalt chloride, cobalt oxalate, rose vitriol, Cobaltous diacetate more specifically, is more preferably one or more in Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES, Cobaltous diacetate and cobalt oxalate.
Boron is another important composition in catalyzer of the present invention, and adding of appropriate boron additive drastically increases selectivity of catalyst and stability, and more embodies the superiority of the present invention program by the catalyzer that specific preparation method obtains.
After boron additive adds, the index that catalyst stability etc. represent catalyst reaction performance significantly improves, and reason wherein may be many-sided: boron improves the electronics form of cobalt or inhibits the generation etc. of carbon distribution.More unexpected, the present inventor finds, at the cobalt catalyst prepared by methods such as co-precipitation, deposition-precipitation and ball millings, the effect that boron additive improves catalyst reaction performance is more obvious.
Boron metal accounts for the 0.1wt% ~ 20wt% of overall catalyst weight, and preferred content accounts for the 0.5wt% ~ 15wt% of overall catalyst weight further, and the content more optimized is 1wt% ~ 10wt%.
Not limiting the source of boron, can be known all boron-containing compounds.There are pure boron, boric acid, metaboric acid, sodium tetraborate, Sodium peroxoborate, sodium metaborate, fluoroboric acid, Sodium tetrafluoroborate, phenylo boric acid, sodium borohydride, POTASSIUM BOROHYDRIDE, triethyl borate, trimethyl borate etc. in the source of the boron of further optimization.
Method for preparing catalyst of the present invention can be obtained by existing catalyst preparation technology, as the method such as pickling process, ion exchange method, blending method, kneading method, co-precipitation, deposition-precipitation, steaming ammonium precipitation, melting-suction filtration, ball milling and sol-gel.Preferred method comprises one or more the combination in co-precipitation, deposition-precipitation and ball milling, these Kaolinite Preparation of Catalyst methods are well known to those skilled in the art as existing mature technology mostly, detailed introduction is all had in the books of this area, as Huang Zhongtao the < commercial catalysts design and development > that shows, the <Preparation of Solid Catalysts> that Gerhard professor Ertl etc. shows.Wherein steaming ammonium intermediate processing of the present invention, concise and to the point step is as follows: salt solubility in water, also may be contained other metals or non-metal salt by (one); (2) ammoniacal liquor is progressively added in above-mentioned salts solution, form cobalt ammonium complex compound with ammonia; (3) other components are added; (4) heat up and progressively evaporated by ammonia, cobalt precipitates; (5) wash, filter; (6) dry, roasting.The step essence of the melting-suction method in the present invention refers to the preparation process of Raney catalyzer: (one) is by will having the fusion of the cobalt metal of catalytic activity, bismuth and aluminium (or silicon) in a furnace, the melt obtained carries out quench cooled, then be crushed into uniform fine particle, dissolve in step the auxiliary agent that also may add other; (2) catalyst fines is shaping, forming technique can adopt existing known technology, as beaten sheet, mediating extrusion, spin etc.; (3) by above-mentioned preformed catalyst suction filtration in alkali lye of gained, namely catalyzer is obtained.
Catalyzer of the present invention also containing one or more elements be selected from IB race, palladium, platinum, ruthenium, rhenium as auxiliary agent, one or more elements in preferred silver, copper, palladium, ruthenium, rhenium, one or more elements further preferably in silver, copper and rhenium, with silver and/or copper for the best.
Silver and copper metal content account for the 0wt% ~ 10wt% of overall catalyst weight, preferably 0 ~ 5wt%.The source of silver metal is Silver Nitrate, and the source of copper can be one or more in metallic copper, cupric nitrate, cupric chloride, neutralized verdigris, cupric oxalate.Silver can be various with the addition manner of copper: add after dissolving together with cobalt salt in precipitation, deposition-precipitation, the steaming ammonium precipitator 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 precipitator method or sol-gel or xerogel, or in material after Roasting Decomposition; Or add beating the formative stage such as sheet or extrusion; Or add when flooding with cobalt liquor, or with cobalt salt step impregnation; Add together with cobalt metal in melting process.
Catalyzer in the present invention is also optionally containing basic metal or alkaline-earth metal, and it is selected from one or more in potassium, sodium, calcium, magnesium, barium, and content accounts for the 0wt ~ 30wt% of catalyzer total amount, preferred 0wt ~ 15wt%, and preferred scope is 0wt% ~ 10wt% further.Alkali and alkaline earth metal ions source can be water miscible nitrate, carbonate, villaumite, phosphoric acid salt, vitriol, acetate, fluorochemical, oxyhydroxide etc.More specifically, be selected from potassium hydroxide, saltpetre, salt of wormwood, Potassium ethanoate, Potassium monofluoride, potassiumphosphate, sodium hydroxide, SODIUMNITRATE, sodium carbonate, sodium bicarbonate, sodium-chlor, sodium sulfate, sodium-acetate, nitrocalcite, monocalcium phosphate, magnesium nitrate, trimagnesium phosphate, nitrate of baryta one or more.
The feed postition of alkali and alkaline earth metal ions element can be selected from any one under type: add after dissolving together with cobalt salt in dipping, kneading, precipitation, deposition-precipitation or sol-gel process; Add together with cobalt salt in the method such as blended, ball milling, melting or add step by step; Add respectively or step by step with cobalt salt in dipping, precipitation, deposition-precipitation or sol-gel process; Add in catalyst precursor, as in filter cake after the drying that obtains in precipitation, deposition-precipitation or sol-gel or xerogel, or in material after Roasting Decomposition; Or add beating the formative stage such as sheet or extrusion.
Catalyzer is also containing some oxide components, contriver thinks that these oxide compounds mainly play the effect of carrier, described oxide component be selected from silicon oxide, aluminum oxide, diatomite, Calucium Silicate powder, zirconium white, titanium oxide one or more, its content accounts for the 10wt% ~ 80wt% of overall catalyst weight.In fact, these carriers are not only play a supporting role, can also assist the dispersion of active ingredient or the activation of carboxylic acid, therefore these carriers affect structure properties, the critical index such as product and raw material diffusion wherein, physical strength, activity and stability of catalyzer.
Support Silica can be selected from waterglass precipitate method, SiO 2 powder, teos hydrolysis, silicon sol etc. and obtain.Described SiO 2 powder can be obtained by methods such as rear ball milling acquisition dry after chemical deposition, waterglass precipitate or silicon sol spraying dry, and its size is selected from 10nm ~ 500 μm; As the gross porosity microballoon silicon-dioxide (mean pore size is 8.0-12.0nm, and specific surface area is 300 ~ 600m2/g, and pore volume is 0.8 ~ 1.1ml/g) that Haiyang Chemical Plant, Qingdao produces, the precipitated silica (silicon-dioxide (SiO of and for example Guangzhou people chemical plant production 2) content %>=95.0, fineness (325 screen residue) %≤1.8, specific surface area is 400 ~ 600m 2/ g) or active carbon white, and for example the 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.It is raw material that described water glass direct precipitation method refers to water glass, adds acidic precipitation agent or ion precipitation agent, as sulfuric acid, hydrochloric acid, nitric acid, acetic acid, nitrocalcite, Zircosol ZN, zirconium oxychloride, magnesium nitrate, Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKES etc. in water glass.Precipitation agent adds rear formation white gum thing, washs the precipitator method using or carry out on this basis other components for several times and adds.Tetraethoxy prepares in catalyzer of the present invention in sol-gel method to use.Silicon sol, as liquid-state silicon source, can directly use in the precipitation system entering precipitation, deposition-precipitation.
Support Silica or aluminum oxide also may be add as binding agent in the catalyzer prepared as melting-suction method, make the catalyst fines of gained can be shaped to shape required for the present invention.
The shape of catalyzer of the present invention can be diversified, as spherical, strip, column, ring-type etc., size is between 0.3 ~ 15mm, more preferably between 1 ~ 10mm, the requirement of this size mainly designs according to fixed-bed reactor of the present invention, with convenient installation, reduces the requirements such as bed layer pressure.These knowledge are known by professional and technical personnel.
Described zirconia material source is powder zirconia material or the precipitation by zirconates.Powder zirconium white size is selected from 10nm ~ 500 μm, and specific surface is greater than 20m 2/ g.The precipitation 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 throw out washing and filtering obtains; Or use Zircosol ZN as zirconium source, the gel that after adding caustic soda precipitation, washing and filtering obtains.Above-mentioned gel is joined in other throw outs, or the carrier that above-mentioned gel is worn into as deposition-precipitation after powder after super-dry is added.
Titanium oxide in the present invention can be some satisfactory 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 precipitation agent, organic metatitanic acid also can be adopted as butyl (tetra) titanate hydrolysis preparation.
Catalyzer is also optionally containing thulium, and its oxide content accounts for the 0wt ~ 8wt% of catalyzer total amount; Described rare earth element selects the one in lanthanum or cerium, and its oxide content accounts for the 0wt ~ 5wt% of catalyzer total amount.The rare earth element adding trace can make the selectivity of cobalt catalyst obtain raising to a certain extent by reducing non-condensable gases content.
Catalyzer is also optionally containing one or more inorganic non-metallic elements, and its content accounts for the 0wt ~ 5wt% of catalyzer total amount.More specifically, described inorganic non-metallic element is selected from the one in phosphorus, fluorine, and content preferably accounts for the 0wt ~ 2wt% of catalyzer total amount.Adding of these inorganic non-metallic elements, what have enters catalyst system along with adding of other auxiliary agents, as Potassium monofluoride.
Described in the present invention is the method for fatty alcohol by organic carboxyl acid hydrocracking, its concrete principle is by monocarboxylic acid gasification and mixes with hydrogen, or enter in hydrogenator 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 loading is fixed-bed reactor, is more preferably shell and tube reactor, more specifically, is by catalyst loading in pipe, and filling heat-conducting medium between pipe, as thermal 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.
Catalyzer of the present invention is when being applied to 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 reductive agent as Sodium Tetraborate 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, temperature of reaction is 180 ~ 350 DEG C, is more preferably 220 ~ 300 DEG C, less in the selectivity change of this scope inner catalyst, maintains higher level.When temperature of reaction is lower, Carboxylic Acid leads lower, and this makes circulating consumption increase; And during temperature of reaction continuation rising, the by product especially amount of non-condensable gases product as ethane significantly increases.
For monocarboxylic acid Hydrogenation for alcohol, the mol ratio of hydrogen gas consumption and carboxylic acid is 2 in theory, but for maintaining subsequent reactions pressure and catalyst life, the molar ratio of hydrogen and carboxylic acid controls at 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.
The catalyst selectivity used in the present invention is higher, therefore in by product the selectivity of non-condensable gases lower than 15%, lower than 10% when more excellent, lower than 5% in further optimization situation.
The hydrogenation of carboxylic acid is typical compressive reaction, and the reaction pressure that the present invention uses 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 conditions gentleer, and reduces cost.
In the method, the volume space velocity of carboxylic acid 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 transformation efficiency is lower, but the productive rate of ethanol and vinyl acetic monomer and increasing on the contrary, particularly vinyl acetic monomer selectivity can improve; When air speed is lower, acetic acid transformation efficiency is high, but the productive rate of ethanol may reduce, therefore for having separating power and wishing the factory of voluminous vinyl acetic monomer, high-speed operator scheme can be adopted, and for the less factory of later separation ability, low-speed can be adopted to operate.Catalyzer of the present invention, at 0.3 ~ 1.0h -1in can ensure that the transformation efficiency of acetic acid is higher than 50%, preferred higher than 75%, preferred higher than 90% further.
The present invention can be widely used in monocarboxylic Hydrogenation for alcohol, and specifically, described monocarboxylic acid is selected from one in acetic acid, propionic acid, butyric acid, lactic acid, 3-hydroxy-propionic acid, methylene-succinic acid or mixture.These carboxylic acids derive from reproducible biomass resource, as mix acid liquors etc. such as lactic acid, 3-hydroxy-propionic acid, phenylformic acid, acetic acid/propionic acid, also can derive from other oil replacement resources, as acetic acid.Preferred, described carboxylic acid is one in acetic acid and propionic acid or mixture.Preferred carboxylic acid is acetic acid further.
Method of the present invention, when after carboxylic acid and hydrogen and catalyst exposure, reaction product, except alcohol, also has other by products of trace, is mainly derived from (1) decarboxylation/decarbonylation product and comprises carbon monoxide, carbonic acid gas, alkane; (2) ketonization product; (3) alkyd/aldehyde condensation products; (4) dewatered product etc.For example, for acetic acid preparation of ethanol through hydrogenation, product, except primarily of except ethanol and vinyl acetic monomer, also has acetaldehyde, ether, butanols, acetone, Virahol, methylal, methane, ethane, propane, carbon monoxide, carbonic acid gas etc.The catalyzer that the present invention describes and method thereof can ensure that Carboxylic Acid is that total selection 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 catalyzer of the present invention and method thereof have the following advantages:
(1) catalyst activity is higher, and object selectivity of product is high;
(2) catalyzer manufacturing cost is comparatively cheap, and investment and running cost are reduced;
(3) reaction conditions is gentleer, can run under wider operation condition, broadening action pane.
Embodiment
Following examples describe the present invention's citing specifically, but the present invention is not limited to these embodiments.
Embodiment 1
Get the cobalt nitrate aqueous solution 1 liter of 1mol/L, add the precipitated silica 40g(silicon-dioxide (SiO that people chemical plant, Guangzhou produces wherein 2) content %>=95.0, fineness (325 screen residue) %≤1.8, specific surface area is 400 ~ 600m 2/ g), be warming up to 60 degree, aqueous sodium carbonate to the pH value adding 20wt% when high degree of agitation is 9.0.Progressively be warming up to 85 DEG C, after constant temperature keeps 2 hours, add lanthanum nitrate 3.0g, continue constant temperature and be cooled to room temperature after 2 hours, slowly add boric acid 6.0g.Washing and filtering, and dried overnight obtains dry cake, sprays into granulation after the silver nitrate solution 10ml containing 0.1wt% in this filter cake.Shaping by beating sheet after particle Roasting Decomposition, obtain catalyzer CHZ-81.
Embodiment 2
Get the cobalt nitrate aqueous solution 1 liter of 1.2mol/L, add Silver Nitrate 1.0 grams and cupric nitrate 10.2 grams wherein, after fully dissolving, add strong aqua 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, to join in the sodium silicate solution of 500g dilution in (dioxide-containing silica is about 10wt%) lentamente, in above-mentioned slurry thing, drip ca nitrate soln 100ml(nitrocalcite concentration 1.0mol/L again), and continue to stir constant temperature 12 hours, progressively slurry material is cooled to room temperature after adding boric acid 8g.By above-mentioned slurry thing filtration washing, and dried overnight obtains dry cake.Shaping by beating sheet after filter cake Roasting Decomposition, obtain catalyzer CHZ-82.
Comparative example 1
Get 30 grams of silica supports (Haiyang Chemical Plant, Qingdao, water-intake rate is about 0.9g/g), by 60 grams of Jing Ti/Bao Pian COBALT NITRATE CRYSTALS/FLAKESs 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 catalyzer CHZ-83.
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 charge capacity 0.85wt%.This catalyzer is CHZ-84.
Embodiment 3
Evaluated in fixed-bed reactor by above-mentioned catalyzer, 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 top temperature be 450 ~ 500 DEG C, concrete reaction conditions and reaction result as shown in table 1.
In the present embodiment, acetic acid transformation efficiency and ethanol selectivity calculate according to the carbon molar content of each component and obtain.
Other products have: acetaldehyde, ethane, methane, carbon monoxide, carbonic acid gas, acetic acid aldehyde, acetone, propyl alcohol etc.
Embodiment 4
Above-mentioned catalyzer is evaluated in fixed-bed reactor, for lactic acid (the 20wt% aqueous solution) Hydrogenation for 1,2-propylene glycol, loadings is 10ml, adopt the quartz sand dilution of 1:1, before use adopt pure hydrogen reduction, reduction top temperature be 450 ~ 500 DEG C, concrete reaction conditions and reaction result as shown in table 2.
In the present embodiment, rotational rate of lactic acid and 1,2-PD selectivity calculate according to the carbon molar content of each component and obtain.Other by products comprise: n-propyl alcohol, Virahol, 2-hydroxy-propionaldehyde, propane, ethane, carbon monoxide, carbonic acid gas, ethanol, diacetylmethane etc.
Table 1
Table 2

Claims (16)

1. a carboxylic acid gas phase hydrogenation prepares the method for alcohol, it is characterized in that, in fixed-bed reactor, carboxylic acid steam mixes with hydrogen-containing gas and is converted into alcohol and water after hydrogenation catalyst contact reacts, the mol ratio of hydrogen and carboxylic acid is 4:1 ~ 40:1, temperature of reaction is 180 ~ 350 DEG C, and reaction pressure is 0.3 ~ 8.0MPa, and the volume space velocity of carboxylic acid is 0.1 ~ 5.0h -1;
Described hydrogenation catalyst comprises following component:
(1) cobalt and boron, wherein cobalt metal content accounts for the 10wt% ~ 50wt% of overall catalyst weight, and boron accounts for the 0.1wt% ~ 20wt% of overall catalyst weight;
(2) oxide compound; Described oxide compound be selected from silicon oxide, diatomite, Calucium Silicate powder, zirconium white, titanium oxide one or more, its content accounts for the 10wt% ~ 80wt% of overall catalyst weight;
Described hydrogenation catalyst combines preparation by one or more in co-precipitation, deposition-precipitation, ammonia still process precipitation, sol-gel and ball milling method; The described carboxylic acid for hydrogenation is monocarboxylic acid.
2. carboxylic acid gas phase hydrogenation according to claim 1 prepares the method for alcohol, it is characterized in that, the molar ratio of hydrogen and carboxylic acid is 8:1 ~ 20:1, and temperature of reaction is 220 ~ 300 DEG C, and reaction pressure is 0.5 ~ 4.0MPa, and the volume space velocity of carboxylic acid is 0.2 ~ 2.0h -1.
3. carboxylic acid gas phase hydrogenation according to claim 1 prepares the method for alcohol, it is characterized in that, in described catalyzer, cobalt metal content accounts for the 15wt% ~ 45wt% of overall catalyst weight, and boron accounts for the 0.5wt% ~ 15wt% of overall catalyst weight.
4. carboxylic acid gas phase hydrogenation according to claim 1 prepares the method for alcohol, it is characterized in that, optionally adopt one or more elements in IB race, palladium, platinum, ruthenium, rhenium as auxiliary agent in described catalyzer, it accounts for the 0wt% ~ 10wt% of overall catalyst weight.
5. carboxylic acid gas phase hydrogenation according to claim 4 prepares the method for alcohol, it is characterized in that, described auxiliary agent is selected from one or more elements in silver, copper, palladium, ruthenium, rhenium.
6. carboxylic acid gas phase hydrogenation according to claim 5 prepares the method for alcohol, it is characterized in that, described auxiliary agent is selected from one or more elements in silver, copper and rhenium.
7. carboxylic acid gas phase hydrogenation according to claim 6 prepares the method for alcohol, it is characterized in that, described auxiliary agent is selected from silver and/or copper.
8. carboxylic acid gas phase hydrogenation according to claim 1 prepares the method for alcohol, it is characterized in that, optionally adds basic metal or alkaline-earth metal in described catalyzer, and its content accounts for the 0wt ~ 30wt% of catalyzer total amount.
9. carboxylic acid gas phase hydrogenation according to claim 8 prepares the method for alcohol, it is characterized in that, described basic metal or alkaline-earth metal be selected from potassium, sodium, calcium, magnesium, barium one or more, content accounts for the 0wt ~ 15wt% of catalyzer total amount.
10. carboxylic acid gas phase hydrogenation according to claim 1 prepares the method for alcohol, it is characterized in that, optionally adds thulium in described catalyzer, and its oxide content accounts for the 0wt ~ 8wt% of catalyzer total amount.
11. carboxylic acid gas phase hydrogenations according to claim 10 prepare the method for alcohol, it is characterized in that, described rare earth element is lanthanum or cerium, and its oxide content accounts for the 0wt ~ 5wt% of catalyzer total amount.
12. carboxylic acid gas phase hydrogenations according to claim 1 prepare the method for alcohol, it is characterized in that, optionally add one or more inorganic non-metallic elements in described catalyzer, its content accounts for the 0wt ~ 5wt% of catalyzer total amount.
13. carboxylic acid gas phase hydrogenations according to claim 12 prepare the method for alcohol, it is characterized in that, described inorganic non-metallic element is phosphorus or fluorine, and content accounts for the 0wt ~ 2wt% of catalyzer total amount.
14. carboxylic acid gas phase hydrogenations according to claim 1 prepare the method for alcohol, it is characterized in that, the described carboxylic acid for hydrogenation is a kind of in acetic acid, propionic acid, butyric acid, lactic acid, 3-hydroxy-propionic acid, phenylformic acid or their mixture.
15. carboxylic acid gas phase hydrogenations according to claim 14 prepare the method for alcohol, it is characterized in that, described carboxylic acid is acetic acid and/or propionic acid.
16. carboxylic acid gas phase hydrogenations according to claim 15 prepare the method for alcohol, it is characterized in that, described carboxylic acid is acetic acid.
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US4517391A (en) * 1982-06-04 1985-05-14 Basf Aktiengesellschaft Continuous preparation of ethanol
CN102149662A (en) * 2008-07-31 2011-08-10 国际人造丝公司 Ethanol production from acetic acid utillizing a cobalt catalyst
CN102271805A (en) * 2009-10-26 2011-12-07 国际人造丝公司 Processes for making ethanol from acetic acid

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4517391A (en) * 1982-06-04 1985-05-14 Basf Aktiengesellschaft Continuous preparation of ethanol
CN102149662A (en) * 2008-07-31 2011-08-10 国际人造丝公司 Ethanol production from acetic acid utillizing a cobalt catalyst
CN102271805A (en) * 2009-10-26 2011-12-07 国际人造丝公司 Processes for making ethanol from acetic acid

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