CN104258869A - Preparation method of catalyst for hydroxypivalaldehyde liquid phase hydrogenation preparation of neopentylene glycol - Google Patents
Preparation method of catalyst for hydroxypivalaldehyde liquid phase hydrogenation preparation of neopentylene glycol Download PDFInfo
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Abstract
The invention relates to a preparation method of a catalyst for hydroxypivalaldehyde liquid phase hydrogenation preparation of neopentylene glycol. The catalyst comprises 20-65wt% of copper oxide, 15-50wt% of alumina, 2-25wt% of zinc oxide, 0.1-5wt% of tin oxide, 0.5-25wt% of alkaline earth oxide and 0-20wt% of titanium oxide and/or zirconia. The compounds containing copper, aluminum, zinc, tin and alkaline earth metal are mixed to form a mixture aqueous solution according to a certain ratio, the solution and an alkaline precipitant are added into a nanometer oxide-containing dispersion liquid in parallel, the mixture undergoes a precipitation reaction, the reaction product is aged and filtered, and the filter residues are washed, dried, roasted and compressed to form a molded catalyst. The catalyst prepared by the method has high activity and good selectivity in hydroxypivalaldehyde liquid phase hydrogenation preparation of neopentylene glycol, can promote 1115 ester conversion, can effectively improve liquid-repellency, and has high catalyst intensity and good stability.
Description
Technical field
The invention belongs to catalysis technical field, be specifically related to the preparation method that the catalyst of neopentyl glycol is prepared in the special valeral liquid-phase hydrogenatin of a kind of hydroxyl.
Background technology
Neopentyl glycol (NPG) is a kind of important chemical intermediate, mainly for the production of powdery paints, mylar, plasticizer, lube oil additive, water soluble alkyd resin etc., be widely used in the fields such as automobile, weaving, medicine, coating and oil; Also can be used for aromatic hydrocarbons to be separated with the selection of cycloalkane, wide market.
The method of current industrial production neopentyl glycol has two kinds: sodium formate method and catalytic hydrogenation method.Sodium formate method is that the special valeral (HPA) of hydroxyl formaldehyde and isobutylaldehyde generated with formaldehyde, cannizzaro's reaction occurs to intersect under base catalysis, and generate neopentyl glycol and a large amount of byproduct formic acid sodium, aftertreatment technology is complicated, and cost is high; Catalytic hydrogenation method is that the special valeral of hydroxyl formaldehyde and isobutylaldehyde generated carries out catalytic hydrogenation, has that product yield is high, accessory substance is few, technological process is short, product purity is high, low cost and other advantages, has significant advantage.
Because of the special valeral poor heat stability of hydroxyl, its Hydrogenation generally carries out for neopentyl glycol process under liquid-phase condition, in order to avoid the special valeral of hydroxyl resolves into isobutylaldehyde and formaldehyde in a large number and causes reaction selectivity poor.Liquid-phase hydrogenatin reaction requires high to catalyst liquid-repellency and working strength.Hydroxyl special valeral hydrogenation catalyst mainly contains the noble metal catalysts such as Ni-based, copper base and palladium, and compared with Ni-based, noble metal catalyst, copper-based catalysts is used for HPA hydrogenation reaction and has the advantages such as activity and selectivity is high, cost is low.The special valeral hydrogenation catalyst of hydroxyl of open report is main mainly with copper-based catalysts prepared by the precipitation method, and catalyst needs to reduce before use.
Copper-chromium-Mn catalyst disclosed in US4855515 need carry out when being used for HPA hydrogenation at 160-170 DEG C, and the easy thermal decomposition of HPA causes NPG selective low.Catalyst copper source disclosed in CN102513107A adopts copper sulphate, carrier adopts diatomite, catalyst is the fine catalyst through pneumatic conveying drying, does not carry out compressing tablet or extruded moulding before using, this catalyst can in 150-170 DEG C of temperature range Hydrogenation for neopentyl glycol.Catalyst disclosed in CN102728370A consists of copper zinc-aluminium-titanium zirconium-hafnium-rhenium, and this catalyst has higher conversion ratio and selective, but in patent and the intensity of not mentioned catalyst and mechanical stability.CN102302937A discloses a kind of copper zinc-aluminium Mn catalyst for catalysis HPA Hydrogenation for NPG, this catalyst activity is high, good stability, also there is good hydrogenation capability to hydroxypivalyl hydroxypivalate simultaneously, the aldolisation catalyst such as a small amount of triethylamine can be tolerated, the intensity of not mentioned post catalyst reaction and filling in this patent.The Cu-series catalyst of above-mentioned open report all adopts the precipitation method to prepare, but mechanical stability when all not mentioned preformed catalyst uses in report and the intensity after using.
In prior art, for the Cu-series catalyst of hydrogenation reaction, from being prepared into the processes such as need going through storage, filling, heating reduction, reaction that comes into operation, be subject to the effect of various inside or external force, when it is for liquid phase reactor, also the actual working strength of catalyst can be able to be made to decline to a great extent due to soaked with liquid, the reason such as swelling, cause catalyst in easily broken, the efflorescence of liquid-phase hydrogenatin system, cause reactor plugs, threaten commercial plant stable operation, affect catalyst life.
In prior art, adopt the anti-liquid ability of conventional Cu-series catalyst prepared by the precipitation method, catalyst is easily broken, efflorescence in running in reactor, will greatly affect device stable operation.Therefore the working strength and the stability that improve liquid phase aldehyde hydrogenation copper series catalysts are most important for the stable operation of guarantee commercial plant.
Summary of the invention
The invention provides the preparation method that the catalyst of neopentyl glycol is prepared in the special valeral liquid-phase hydrogenatin of a kind of hydroxyl, adopt the catalyst prepared of the method not only active high, selective good, can promote that 3-hydroxypivalic acid DOPCP (1115 ester) transforms, and there is excellent anti-liquid ability, reduction gone through by catalyst, liquid-phase hydrogenatin post reaction strength is high.
For achieving the above object, the technical solution used in the present invention is:
The special valeral Hydrogenation of hydroxyl, for a preparation method for the catalyst of neopentyl glycol, comprises the following steps:
(1) in reactor, add deionized water, then add nano-oxide, and stir, be made into the dispersion liquid of nano-oxide, described nano-oxide is selected from the one or two or more in nano aluminium oxide, nano-titanium oxide and nano zircite;
(2) copper-containing compound, aluminum contained compound, zinc compound, sn-containing compound and alkaline including earth metal compound are dissolved in the water, be configured to mixture aqueous solution, mixture aqueous solution and alkaline precipitating agent are instilled in the dispersion liquid of nano-oxide simultaneously and reacts, controlling reaction system pH in course of reaction is 5.0-8.0, reaction terminates rear use alkaline precipitating agent regulation system pH to 7.0-9.0, then aging, obtain slurry;
(3) slurry carried out filter, wash, dry, obtain filter cake;
(4) filter cake is carried out roasting, fragmentation, compression molding, obtain catalyst.
The temperature of the dispersion liquid of step of the present invention (1) is 60-90 DEG C.
The temperature of the course of reaction of step of the present invention (2) is 60-90 DEG C, and control reaction system pH is 5.5-7.0, and the time is 1-3h; Reaction terminates rear use alkaline precipitating agent and system pH is adjusted to 7.5-8.5; Aging temperature is 60-90 DEG C, and ageing time is 1-3h.
The baking temperature of step of the present invention (3) is 100 DEG C, and drying time is 12-24h.
The sintering temperature of step of the present invention (4) is 350-900 DEG C, and roasting time is 2-8h.
Copper-containing compound of the present invention is the one or two or more of copper nitrate, copper chloride and copper acetate; Aluminum contained compound is the one or two or more of aluminum nitrate, aluminium chloride and aluminium acetate; Zinc compound is the one or two or more of zinc nitrate, zinc chloride and zinc acetate; Sn-containing compound is selected from stannous acetate and/or stannous chloride; Described alkaline earth metal compound is selected from the one or two or more of the nitrate of magnesium, calcium and barium, chloride and acetate.
The particle diameter < 100nm of nano-oxide of the present invention, preferred 1-50nm, more preferably 20-40nm.
Nano-oxide particle diameter needs within the specific limits, particle diameter is too large, and nano-oxide is difficult to be evenly distributed in the catalyst, and preformed catalyst stress in reduction process is concentrated and easily produces fine crack, easily broken through soaked with liquid rear catalyst, cause catalyst strength to decline; Particle diameter is too little, and nano-oxide not easily disperses and cost is high, can not improve catalyst strength and liquid-repellency energy further.
In dispersion liquid of the present invention, the solid content of nano-oxide is 0.1-5wt%, preferred 0.5-2wt%, with the total restatement of dispersion liquid.
Alkaline precipitating agent of the present invention is the one or two or more in sodium carbonate, potash, sodium acid carbonate, saleratus, NaOH, potassium hydroxide, ammonium carbonate, carbonic hydroammonium and ammoniacal liquor.
The consumption of nano-oxide of the present invention accounts for 0.5 ~ 20wt% of overall catalyst weight, preferred 1-10wt%, more preferably 2-5wt%.
When nano-oxide addition is too low, does not have enough nano-oxide induced precipitations to be accumulated into tight structure, can not structural re-enforcement be played, catalyst liquid-repellency energy cannot be improved; When nano-oxide addition is too many, nano-oxide can not fully be disperseed, and can affect catalyst strength on the contrary, causes catalyst liquid-repellency energy poor.
The catalyst composition adopting method of the present invention to prepare comprises: cupric oxide 20-65wt%, aluminium oxide 15-50wt%, zinc oxide 2-25wt%, tin oxide 0.1-5wt%, one or two or more 0.5-25wt% in magnesia, calcium oxide and barium monoxide, titanium oxide and/or zirconia 0-20wt%, by overall catalyst weight.
Preferably, catalyst composition of the present invention comprises: cupric oxide 40-63wt%, aluminium oxide 20-45wt%, zinc oxide 5-20wt%, tin oxide 0.2-3wt%, one or two or more 1-10wt% in magnesia, calcium oxide and barium monoxide, one or both 0-10wt% in titanium oxide and zirconia, by overall catalyst weight.
More preferably, catalyst composition of the present invention comprises: cupric oxide 42-60wt%, aluminium oxide 22-40wt%, zinc oxide 10-18wt%, tin oxide 0.5-2wt%, one or two or more 2-5wt% in magnesia, calcium oxide and barium monoxide, one or both 0-5wt% in titanium oxide and zirconia, by overall catalyst weight.
Tin add the decentralization and stability that improve copper in catalyst, the conversion of 1115 esters in raw material can be promoted.
Catalyst prepared by the method for the invention, nano-oxide is added in preparation process, induced precipitation particle is formed closely, stable structure, particle Interaction Force is strong, and nano-oxide plays the effect of structure reinforcing agent, make catalyst have high cohesive force, decrease the generation of catalyst fine crack in reduction process, make catalyst through soaked with liquid, to wash away and can not broken, efflorescence after reacting, still there is good intensity.
Catalyst of the present invention just possesses corresponding catalytic activity, for Hydrogenation for NPG after needing to carry out reduction activation.
The method of the reduction activation of catalyst of the present invention comprises: the mist volume space velocity 300-1000h keeping hydrogen and nitrogen
-1, first temperature of reactor is risen to 160-180 DEG C, the mechanical water of constant temperature 1-2h Removal of catalyst absorption, then passes into containing volume fraction 5v%H
2hydrogen and the gaseous mixture of nitrogen carry out prereduction 1h, progressively improve the ratio of hydrogen in hydrogen and nitrogen mixture afterwards to 10v%, 20v%, 50v%, 100%, control this process catalyst bed hot(test)-spot temperature and be no more than 220 DEG C, finally be warming up to 220 DEG C of reductase 12-5h under pure hydrogen atmosphere, obtain the catalyst of reduction-state.
The catalyst of reduction-state of the present invention is used for HPA Hydrogenation for NPG, and reaction pressure 3-5MPa, reaction temperature is 120-140 DEG C, H
2/ HPA mol ratio 2-20:1, catalyst treatment amount is 0.2-0.5g
hPA/ g
cat/ h.
Pressure of the present invention is relative pressure.
Catalyst of the present invention is used for the special valeral liquid-phase hydrogenatin of hydroxyl and prepares in the process of neopentyl glycol, catalyst is not only active high, selective good, and there is good anti-liquid ability, run off without copper in icp analysis display hydrogenation liquid, post catalyst reaction profile is complete, breakage rate is low, side pressure strength is high, can promote that 1115 esters transform.
Detailed description of the invention
Below in conjunction with embodiment, the inventive method is described in detail, but be not limited to embodiment.
The side pressure strength of catalyst adopts granule strength tester to measure; catalyst hydrogenation liquid (20wt%NPG+40wt% methyl alcohol+40wt% water) soaks protection; in case catalyst is oxidized, measures 40 post catalyst reaction side pressure strengths, get its mean value.
In hydrogenation liquid, content of copper ion adopts Inductively coupled plasma optical emission spectrometer (ICP) to measure.
Embodiment 1
Add 3kg water in reactor, and add the nano-titanium oxide of 19.5g particle diameter at 20-40nm, stir.384.1g copper nitrate, 619.3g aluminum nitrate, 90.8g zinc nitrate, 2.92g stannous chloride, 51.4g calcium nitrate are dissolved in 2.7kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 60 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 60 DEG C, system pH is 6.0, the reaction time is 1h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.5, and at 70 DEG C aging 3h, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 350 DEG C of roasting 3h, be pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after carrying out fragmentation, obtain catalyst A.
Catalyst reduction: catalyst A is loaded in fixed bed hydrogenation reactor, loaded catalyst 200ml.Catalyst reduces before using under nitrogen and hydrogen mixed gas, keeps mist volume space velocity 300h in reduction process
-1, first temperature of reactor is risen to the mechanical water of 160 DEG C of constant temperature 2h Removal of catalyst absorption, then passes into containing volume fraction 5v%H
2hydrogen and the gaseous mixture of nitrogen carry out prereduction 1h, progressively improve the ratio of hydrogen in hydrogen and nitrogen mixture afterwards to 10v%, 20v%, 50v%, 100%, control this process catalyst bed hot(test)-spot temperature and be no more than 220 DEG C, be finally warming up to 220 DEG C under pure hydrogen atmosphere, reduce 3h.
Hydrogenating materials consists of other component (formaldehyde, isobutylaldehyde etc.) of 20wt%HPA, 0.7wt%1115 ester, 38.5wt% methyl alcohol, 40wt% water and 0.8wt%, at pressure 4Mpa, and temperature 140 DEG C, H
2/ HPA mol ratio 20:1, catalyst treatment amount is 0.4g
hPA/ g
catreact under the condition of/h.Get hydrogenation liquid at interval of 24h and measure content of copper ion in hydrogenation liquid.After reaction 500h, catalyst removed from reactor and use the stainless steel sub-sieve of aperture 4mm to sieve catalyst, and the catalyst granules quality calculating particle diameter < 4mm accounts for the ratio of catalyst gross mass, in this, as catalyst breakage rate.Adopt granule strength tester assaying reaction rear catalyst side pressure strength.In hydrogenation reaction result and hydrogenation liquid, average copper ion concentration is in table 1.Before and after reaction, COMPARATIVE CATALYST is in table 2.
Embodiment 2
Add 3kg water in reactor, and add the nano-titanium oxide of 11.7g particle diameter at 20-30nm, stir.530.4g copper nitrate, 358.6g aluminum nitrate, 90.8g zinc nitrate, 71.8g magnesium nitrate, 11.7g stannous chloride are dissolved in 2.5kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 80 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 80 DEG C, system pH is 5.5, the reaction time is 1.5h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.0, and aging 3h is continued at 70 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 500 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst B.
All the other conditions are with reference to embodiment 1.
Embodiment 3
Add 3kg water in reactor, and add the nano zircite of 15.6g particle diameter at 20-30nm, stir.439.0g copper nitrate, 358.6g aluminum nitrate, 181.6g zinc nitrate, 33.2g barium nitrate, 5.84g stannous chloride are dissolved in 2.5kg water and configure mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 60 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 60 DEG C, system pH is 5.5, the reaction time is 2h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.7, and aging 3h is continued at 80 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 650 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst C.
All the other conditions are with reference to embodiment 1.
Embodiment 4
Add 3kg water in reactor, and add the nano-titanium oxide of 9.75g particle diameter at 20-40nm, stir.457.3g copper nitrate, 488.9g aluminum nitrate, 136.2g zinc nitrate, 32.8g calcium nitrate, 2.92g stannous chloride are dissolved in 2.7kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 85 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 85 DEG C, system pH is 6.7, the reaction time is 1h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 8.0, and aging 3h is continued at 85 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 600 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst D.
All the other conditions are with reference to embodiment 1.
Embodiment 5
Add 3kg water in reactor, and add 9.75g particle diameter at 20-30nm nano-titanium oxide, particle diameter at the 9.75g nano zircite of 20-40nm, stir.439.0g copper nitrate, 358.6g aluminum nitrate, 195.2g zinc nitrate, 28.5g calcium nitrate, 5.84g stannous chloride are made into mixed-salt aqueous solution in 2.5kg water, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 70 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 70 DEG C, system pH is 6.5, the reaction time is 2.5h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 8.5, and aging 3h is continued at 90 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 700 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst E.
All the other conditions are with reference to embodiment 1.
Embodiment 6
Add 3kg water in reactor, and add the nano aluminium oxide of 19.5g particle diameter at 20-30nm, stir.647.8g copper nitrate, 350.4g aluminum nitrate, 136.2g zinc nitrate, 16.6g barium nitrate, 5.84g stannous chloride are dissolved in 2.8kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 60 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 60 DEG C, system pH is 6.5, the reaction time is 2h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.5, and aging 3h is continued at 70 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 550 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst F.
All the other conditions are with reference in embodiment 1.
Comparative example 1
548.7g copper nitrate, 488.9g aluminum nitrate, 90.8g zinc nitrate are dissolved in 2.6kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution is heated to 70 DEG C.3000g water is added in stillpot.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 70 DEG C, system pH is 6.0, the reaction time is 1h.Adopt sodium carbonate liquor that system pH is adjusted to 8.5, and at 80 DEG C aging 2h, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 500 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst G.
All the other conditions are with reference to embodiment 1.
Comparative example 2
3kg water is added in reactor, 439.0g copper nitrate, 358.6g aluminum nitrate, 181.6g zinc nitrate, 33.2g barium nitrate, 5.84g stannous chloride are dissolved in 2.5kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 80 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 80 DEG C, system pH is 6.5, the reaction time is 1h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.5, and continue aging 3h at 80 DEG C after, add the nano zircite of 20g particle diameter at 20-40nm, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 700 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst H.
All the other conditions are with reference to embodiment 1.
Comparative example 3
Add 3kg water in reactor, and add the nano-titanium oxide of 91.6g particle diameter at 100-300nm, stir.384.1g copper nitrate, 358.6g aluminum nitrate, 90.8g zinc nitrate, 28.5g calcium nitrate, 2.92g stannous chloride are dissolved in 2.4kg water and are made into mixed-salt aqueous solution, by the sodium carbonate liquor being made into 20wt% soluble in water for sodium carbonate, respectively two kinds of solution are heated to 80 DEG C.Adopt the method for co-precipitation, two kinds of solution are instilled in reactor simultaneously, control precipitation process temperature in the kettle 80 DEG C, system pH is 5.5, the reaction time is 1h.After saline solution to be mixed adds, adopt sodium carbonate liquor that system pH is adjusted to 7.0, and aging 3h is continued at 70 DEG C, then filter, to wash and by filter cake at 110 DEG C of dry 12h, and in 500 DEG C of roasting 3h, by being pressed into 5*5mm cylinder (diameter 5mm, height 5mm) catalyst after the catalyst breakage after roasting, obtain catalyst I.
All the other conditions are with reference to embodiment 1.
Average copper ion concentration in table 1 hydrogenation reaction result and hydrogenation liquid
Note: " not detecting " represents average copper ion concentration < 0.1 μ g/ml in hydrogenation liquid
COMPARATIVE CATALYST before and after table 2 reacts
Even if * N/ Ke Shi catalyst strength unit 1 catalyst breakage applied force
From table 1, table 2, when using catalyst A to catalyst F, copper do not detected in hydrogenation liquid, the complete and side pressure strength of post catalyst reaction is more than 45N/ grain; And catalyst described in comparative example 1 to comparative example 3, post catalyst reaction is broken seriously, side pressure strength is low, and catalyst G and I occurs efflorescence so that cannot survey its side pressure strength, and in icp analysis display hydrogenation liquid, copper content is higher, illustrates that catalyst has obvious loss.Further, to catalyst F, catalyst A effectively can promote that 1115 esters transform.
Claims (11)
1. the special valeral Hydrogenation of hydroxyl is for a preparation method for the catalyst of neopentyl glycol, comprises the following steps:
(1) in reactor, add deionized water, then add nano-oxide, and stir, be made into the dispersion liquid of nano-oxide, described nano-oxide is selected from the one or two or more in nano aluminium oxide, nano-titanium oxide and nano zircite;
(2) copper-containing compound, aluminum contained compound, zinc compound, sn-containing compound and alkaline including earth metal compound are dissolved in the water, be configured to mixture aqueous solution, mixture aqueous solution and alkaline precipitating agent are instilled in the dispersion liquid of nano-oxide simultaneously and reacts, controlling reaction system pH in course of reaction is 5.0-8.0, reaction terminates rear use alkaline precipitating agent regulation system pH to 7.0-9.0, then aging, obtain slurry;
(3) slurry carried out filter, wash, dry, obtain filter cake;
(4) filter cake is carried out roasting, fragmentation, compression molding, obtain catalyst.
2. method according to claim 1, is characterized in that, the temperature of the dispersion liquid of described step (1) is 60-90 DEG C.
3. method according to claim 1, is characterized in that, the temperature of the course of reaction of described step (2) is 60-90 DEG C, and control reaction system pH is 5.5-7.0, and the time is 1-3h; Reaction terminates rear use alkaline precipitating agent and system pH is adjusted to 7.5-8.5; Aging temperature is 60-90 DEG C, and ageing time is 1-3h.
4. method according to claim 1, is characterized in that, the baking temperature of described step (3) is 100 DEG C, and drying time is 12-24h.
5. method according to claim 1, is characterized in that, the sintering temperature of described step (4) is 350-900 DEG C, and roasting time is 2-8h.
6. method according to claim 1, is characterized in that, described copper-containing compound is the one or two or more of copper nitrate, copper chloride and copper acetate; Aluminum contained compound is the one or two or more of aluminum nitrate, aluminium chloride and aluminium acetate; Zinc compound is the one or two or more of zinc nitrate, zinc chloride and zinc acetate; Sn-containing compound is selected from stannous acetate and/or stannous chloride; Described alkaline earth metal compound is selected from the one or two or more of the nitrate of magnesium, calcium and barium, chloride and acetate.
7. method according to claim 1, is characterized in that, the particle diameter < 100nm of described nano-oxide, preferred 1-50nm, more preferably 20-40nm.
8. method according to claim 1, is characterized in that, in described dispersion liquid, the solid content of nano-oxide is 0.1-5wt%, preferred 0.5-2wt%, with the total restatement of dispersion liquid.
9. method according to claim 1, is characterized in that, described alkaline precipitating agent is the one or two or more in sodium carbonate, potash, sodium acid carbonate, saleratus, NaOH, potassium hydroxide, ammonium carbonate, carbonic hydroammonium and ammoniacal liquor.
10. the method according to any one of claim 1-9, is characterized in that, the consumption of described nano-oxide accounts for 0.5 ~ 20wt% of overall catalyst weight, preferred 1-10wt%, more preferably 2-5wt%.
The catalyst that 11. methods according to any one of claim 1-10 are obtained, it is characterized in that, by overall catalyst weight, catalyst composition comprises: cupric oxide 20-65wt%, aluminium oxide 15-50wt%, zinc oxide 2-25wt%, tin oxide 0.1-5wt%, one or two or more 0.5-25wt% in magnesia, calcium oxide and barium monoxide, titanium oxide and/or zirconia 0-20wt%;
Preferential oxidation copper 40-63wt%, aluminium oxide 20-45wt%, zinc oxide 5-20wt%, tin oxide 0.2-3wt%, the one or two or more 1-10wt% in magnesia, calcium oxide and barium monoxide, one or both 0-10wt% in titanium oxide and zirconia;
More preferably cupric oxide 42-60wt%, aluminium oxide 22-40wt%, zinc oxide 10-18wt%, tin oxide 0.5-2wt%, the one or two or more 2-5wt% in magnesia, calcium oxide and barium monoxide, one or both 0-5wt% in titanium oxide and zirconia.
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| CN106582660A (en) * | 2016-12-05 | 2017-04-26 | 万华化学集团股份有限公司 | Preparation method of catalyst for preparing alcohol through aldehyde hydrogenation |
| CN108187689A (en) * | 2016-12-08 | 2018-06-22 | 万华化学集团股份有限公司 | A kind of hydrogenation catalyst and preparation method thereof and a kind of method for preparing 1,2- pentanediols |
| CN109482192A (en) * | 2018-11-30 | 2019-03-19 | 万华化学集团股份有限公司 | A kind of hydrogenation of acetophenone prepares the preparation method and application of the catalyst of alpha-phenyl ethyl alcohol |
| CN111874940A (en) * | 2020-07-13 | 2020-11-03 | 滁州学院 | Preparation method and application of tubular tin dioxide and carbon-coated tubular tin dioxide nanocomposite |
| CN113926460A (en) * | 2021-11-23 | 2022-01-14 | 鲁西催化剂有限公司 | Hydroxypivalaldehyde hydrogenation catalyst, and preparation method and application thereof |
| CN115894169A (en) * | 2022-07-28 | 2023-04-04 | 沾化瑜凯新材料科技有限公司 | Production process of high-purity neopentyl glycol |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582660A (en) * | 2016-12-05 | 2017-04-26 | 万华化学集团股份有限公司 | Preparation method of catalyst for preparing alcohol through aldehyde hydrogenation |
| CN106582660B (en) * | 2016-12-05 | 2019-04-23 | 万华化学集团股份有限公司 | A kind of aldehyde add hydrogen prepare alcohol catalyst preparation method |
| CN108187689A (en) * | 2016-12-08 | 2018-06-22 | 万华化学集团股份有限公司 | A kind of hydrogenation catalyst and preparation method thereof and a kind of method for preparing 1,2- pentanediols |
| CN109482192A (en) * | 2018-11-30 | 2019-03-19 | 万华化学集团股份有限公司 | A kind of hydrogenation of acetophenone prepares the preparation method and application of the catalyst of alpha-phenyl ethyl alcohol |
| CN109482192B (en) * | 2018-11-30 | 2021-09-07 | 万华化学集团股份有限公司 | Preparation method and application of catalyst for preparing alpha-phenylethyl alcohol by acetophenone hydrogenation |
| CN111874940A (en) * | 2020-07-13 | 2020-11-03 | 滁州学院 | Preparation method and application of tubular tin dioxide and carbon-coated tubular tin dioxide nanocomposite |
| CN113926460A (en) * | 2021-11-23 | 2022-01-14 | 鲁西催化剂有限公司 | Hydroxypivalaldehyde hydrogenation catalyst, and preparation method and application thereof |
| CN113926460B (en) * | 2021-11-23 | 2022-05-27 | 鲁西催化剂有限公司 | Hydroxypivalaldehyde hydrogenation catalyst, and preparation method and application thereof |
| CN115894169A (en) * | 2022-07-28 | 2023-04-04 | 沾化瑜凯新材料科技有限公司 | Production process of high-purity neopentyl glycol |
| CN115894169B (en) * | 2022-07-28 | 2024-01-30 | 沾化瑜凯新材料科技有限公司 | Production process of high-purity neopentyl glycol |
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