CN101062483A - Novel selective hydrogenation catalyst and preparation method thereof - Google Patents
Novel selective hydrogenation catalyst and preparation method thereof Download PDFInfo
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- CN101062483A CN101062483A CN 200610076636 CN200610076636A CN101062483A CN 101062483 A CN101062483 A CN 101062483A CN 200610076636 CN200610076636 CN 200610076636 CN 200610076636 A CN200610076636 A CN 200610076636A CN 101062483 A CN101062483 A CN 101062483A
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Abstract
The invention relates to the selection of new hydrotreating catalyst, in order to solve existing porous metal carrier catalyst uneven bearing and looseness issue, putting forward a porous metal carrier in the middle with precious metal catalyst. The catalyst is made by pre-treating the porous metal to form a layer of compact oxidization layer, coating inorganic oxidization glue, forming the carrier middle using dipping to carry precious metal. It is fine in catalyst thermal conductive feature, even in active component distribution, high in diffusion, fast in bearing, fine in catalyst feature.
Description
Technical field
The present invention relates to a kind of alkynes and diolefin hydrogenate Catalysts and its preparation method.More particularly, the present invention relates to a kind of is the selection hydrogenation catalyst and preparation method thereof of carrier with porous metals.
Background technology
In the alkene production technology, as all containing a spot of alkynes and alkadienes in the olefin feedstock of productions such as steam cracking, catalytic pyrolysis, they can influence the further processing and utilization of alkene, therefore these impurity must be removed as far as possible, industrial employing is removed these impurity to select hydrogenation catalyst effectively with the method that alkynes and alkadienes carry out selective hydrogenation reaction.
CN 1279126A discloses a kind of selective acetylene hydrocarbon hydrogenation catalyst and preparation method thereof.This catalyst is with diatomite, SiO
2, Ti
2O
3, Al
2O
3Being carrier, is major catalyst with the palladium, and bismuth is a co-catalyst, by with contain palladium solution, bismuth-containing solution or and other co-catalysts soak altogether or the step impregnation carrier, make after drying, the roasting again.The adding of co-catalyst has obviously improved the catalytic activity and the selectivity of catalyst, has reduced green oil generating amount, has reduced carbon deposit, has prolonged catalyst life.
CN 1295880A discloses a kind of selection hydrogenation catalyst that is used for alkene fraction alkynes and alkadienes, it is carrier with the aluminium oxide, with palladium, platinum grade in an imperial examination VIII family metallic element is main active component, with rare earth element (as Se, La, Lu, Pr etc.) as co-catalyst.This catalyst have selectivity better, the advantage of active higher, good stability.
It is the C that is used for of carrier with the aluminium oxide that CN 1295879A discloses a kind of
2-C
7The selection hydrogenation catalyst of alkynes in the cut and diene.This catalyst is main active component with the group VIII metallic element, and alkali metals such as K, Rb in carrier, have been introduced, thereby improved activity of such catalysts, selectivity and stability, this is because alkali metal can reduce carrier surface acid and improve the active component distribution.
CN 1364855A discloses a kind of alkynes and diolefin hydrogenate catalyst, is carrier with the inorganic oxide, and palladium is main active component, and IB family is a co-catalyst.The characteristics of this catalyst are to resist sulphur and arsenic poisoning, are applicable to any H
2C with CO content
2-C
3The selective hydrogenation reaction of cut.
CN 1410515A discloses a kind of catalyst that hydrogenation is selected in C5 fraction that is used for, and this catalyst is carrier with the aluminium oxide, prepares by the order of successively flooding I B-group metal, group VIII metal and at least a alkali metal.This catalyst can be used in the C5 fraction selective hydrogenation reaction of gas phase or liquid phase.
CN 1321544A discloses a kind of multimetal reforming catalyst of selecting acetylene hydrogenation, this catalyst is a carrier with a kind of in aluminium oxide, silica or the titanium oxide, include a certain amount of Cu and Pd, and add among Bi, Zr, Pb, Ag, the Pt one or more as co-catalyst.
More than in each patent disclosed hydrogenation catalyst many be carrier with the inorganic oxide, with the group VIII metallic element is major catalyst, reduce carrier surface acid by adding different co-catalysts, increase the active component decentralization, to reach the purpose that improves catalyst selectivity, reduces green oil generating amount, prolongs catalyst life.Adopt the method for outer adding assistant to improve selection of catalysts, make Preparation of catalysts become complicated, also increased the cost of catalyst simultaneously.In addition, hydrogenation reaction is a strong exothermal reaction, and the reaction heat that produces in the course of reaction must be removed as early as possible, produces side reaction to avoid temperature runaway, and therefore the heat conductivility to catalyst requires than higher.And be mostly to adopt oxide in the above-mentioned patent as catalyst carrier, exist the problem of heat conductivility difference.
For solving the problem of above-mentioned catalyst heat conductivility difference, it is the preparing carriers catalyst that people propose with porous metals.For example, US6429337 discloses a kind of novel itrogenous organic substance hydrogenating reduction system amine catalyst for reaction.This catalyst is a carrier with the porous metals particle, by the aqueous slkali that utilizes transition metal porous carrier is carried out dip-coating, transition metal such as platinum, palladium, ruthenium, rhodium is carried on carrier surface is prepared from, and the decentralization of noble metal active component is less than 60%.This catalyst exists the low and firm inadequately problem of load of active component decentralization.
Summary of the invention
The present invention is the uneven and not firm problem of active constituent loading that the catalyst of carrier exists with porous metals in order to solve existing, elder generation load carriers intermediate layer, Catalysts and its preparation method of carried noble metal component on this carrier intermediate layer again on Lacunaris metal carrier have been proposed.
Concrete technical scheme is as follows.
A kind of selection hydrogenation catalyst that the present invention proposes is with load on the Lacunaris metal carrier carrier intermediate layer to be arranged, again the catalyst of carried noble metal component on this carrier intermediate layer;
Described Lacunaris metal carrier is a kind of of porous metals or metal alloy; Described carrier intermediate layer is the inorganic oxide carrier layer.
Gross weight based on catalyst, described Lacunaris metal carrier is preferably 95 weight %～97.9 weight %, described carrier intermediate layer is preferably 2 weight %～4 weight %, described noble metal component is preferably 0.1 weight %～1.0 weight %, and the decentralization of described noble metal component is preferably 50%～80%.
Described noble metal is preferably palladium, platinum, rhodium.
Described decentralization is meant the surface atom number of noble metal in the catalyst and the ratio of noble metal total atom number, is the parameter that is used for characterizing catalyst surface active component degree of scatter, can adopt conventional H
2Isothermal adsorption method is measured.
The porosity of described Lacunaris metal carrier is preferably 30%～80%, and the volume averaging aperture is preferably 5～100 μ m.
Described carrier intermediate layer is preferably SiO
2, TiO
2Or Al
2O
3
Selection hydrogenization catalyst preparation method of the present invention may further comprise the steps:
(1) preparation Lacunaris metal carrier: the porous metals of selecting are made required form and size;
(2) preliminary treatment Lacunaris metal carrier: porous metals are immersed cleaning in the washing lotion, oven dry; Porous metals are immersed in the strong oxidation liquid handled 10 minutes～2 hours, take out then, use washed with de-ionized water, drying;
(3) preparation carrier intermediate layer: the Lacunaris metal carrier that step (2) is obtained was immersed in the parent colloidal sol in carrier intermediate layer 0.5～2 hour, took out dryly, through roasting the parent of dipping was decomposed into oxide, made the carrier intermediate layer;
(4) carried noble metal component: use the mother solution of noble metal component noble metal component to be loaded on the carrier intermediate layer with infusion process, drying, roasting, reduction makes catalyst of the present invention.
The selected Lacunaris metal carrier of the present invention can adopt powder metallurgic method preparation commonly known in the art, can select suitable Lacunaris metal carrier, for example porous aluminum, porous stainless steel.There is no particular limitation to the shape of Lacunaris metal carrier, can it be made needed shape and size according to the needs of commercial Application situation, different shape such as cylinder for example, and its diameter dimension can be 2～5mm, height dimension can be 0.5～5mm.
The mixture of one or more in the preferably volatile organic solvent of washing lotion described in the step (2) for example is hexane, pentane, heptane, absolute ethyl alcohol, acetone etc.Described strong oxidation liquid is strong basicity oxidation liquid preferably, for example is the aqueous solution of NaOH.According to the concrete condition of oxidation liquid, selective oxidation condition suitably, for example oxidizing temperature is preferably 120～150 ℃.
The parent colloidal sol in described carrier intermediate layer is preferably a kind of in silica, aluminium oxide, the titanium oxide sol, and the concentration of colloidal sol is preferably 3 weight %～8 weight %.There is no particular limitation to the method for preparing colloidal sol, for instance, can use methods such as adding acid or alkali generation colloidal sol in organic hydrolysis of alkoxide method, the mother solution, for example aluminum hydroxide sol is made in the aluminium isopropoxide hydrolysis, adding NaOH or potassium hydroxide solution are made aluminum hydroxide sol in liquor alumini chloridi, add hydrochloric acid and make aluminum hydroxide sol in sodium aluminate solution; Also can use the inorganic raw material method for hydrolysis, can be with the metallic aluminium digestion at hydrochloric acid or AlCl
3Make aluminum hydroxide sol in the solution, also can be with Al (NO
3)
3Soluble in water according to a certain ratio with acid, add an amount of dispersant, use dense HNO
3Or dense NH
3H
2The O regulator solution makes colloidal sol to certain initial pH value.
In step (4), the parent of described noble metal component can be any soluble precursor of noble metal component.For example, when noble metal component is palladium, can be inorganic salts, organic salt or the metal complex of palladium, its typical case is represented as: PdCl
2, Pd (NO
3)
2, H
2PdCl
4, [Pd (NH
3)
4] Cl
2Deng; When noble metal component was platinum, its slaine can be PtCl
2, Pt (NO
3)
2, H
2PtCl
4There is no particular limitation to the infusion process among the present invention, can adopt dipping method commonly known in the art, can adopt the equivalent impregnation method, also can adopt excessive infusion process.
Utilize preliminary treatment, on porous metals, form rough surface, load intermediate layer thereon again, combining between intermediate layer and matrix will be more firm, utilize the load place of intermediate layer as active component again, make catalyst.
The present invention adopts the carrier intermediate layer that porous metals are carried out the specific area that modification both can increase porous metals, also can provide the place for the load of catalytic active component, make catalytic active component can with the Lacunaris metal carrier strong bonded.
It is the bond strength that strengthens between intermediate layer and porous metals that the present invention carries out pretreated purpose to Lacunaris metal carrier.At first clean to remove the dirt that is attached to above the porous metals, form one deck compact oxide on the porous metals surface then, thereby can make in the middle of the carrier and more firm in combination between the porous metals.
Catalyst of the present invention can be used for the selective hydrogenation reaction of alkynes and alkadienes, for example is used for carbon three and selects acetylene hydrogenation reaction, carbon four to select the acetylene hydrogenation reaction.
Selection hydrogenation catalyst of the present invention has following advantage:
(1) selection hydrogenation catalyst employing of the present invention as catalyst carrier, has the catalytic activity height through the porous metals of modification, and selectivity is good, and green oil generating amount is few, the advantage that catalyst life is long.
(2) selection hydrogenation catalyst of the present invention is that the porous metals with modification are carrier, have high specific surface, excellent mechanical intensity and heat conductivility, be applied to promptly heat to be passed in the hydrogenation reaction of strong heat release, avoid the beds temperature runaway.
(3) active component of selection hydrogenation catalyst of the present invention is scattered in the carrier intermediate layer, is evenly distributed, load is firm, the catalytic action of easier performance active component.
(4) catalyst of the present invention is made up of Lacunaris metal carrier, thin oxide film and oxide intermediate layer from the inside to surface, and thin oxide film and intermediate layer combine with carrier firmly, and no crack performance produces.
The specific embodiment
Further explain the present invention in the mode of embodiment below, but the present invention is not limited to these embodiment.
Embodiment 1
Is example with porous stainless steel as catalyst carrier, and selection hydrogenation catalyst of the present invention and preparation method thereof is described in detail in detail.
(1) preparation porous stainless steel carrier
Adopt that porosity is 40%, average pore size is 10 μ m, is of a size of the porous stainless steel disk (being provided by Antai Science and Technology Co., Ltd) of φ 6mm * 1.5mm as carrier, use earlier the hexane washing by soaking, again with the soaked in absolute ethyl alcohol washing, the oven dry back is stand-by after the taking-up;
(2) preliminary treatment of carrier
The Lacunaris metal carrier that cleaned immersed in the pretreatment fluid for preparing carry out preliminary treatment, pretreatment fluid is formed and the pretreating process condition is: weight percent concentration is 45% the NaOH aqueous solution, treatment temperature is 150 ℃, and the processing time is 60 minutes, takes out drying for standby;
(3) preparation aluminum hydroxide sol
Method according to organic hydrolysis of alkoxide makes aluminum hydroxide sol: under 80 ℃, aluminium isopropoxide and deionized water were mixed in 1: 90 in molar ratio, stir adding nitre acid for adjusting pH value to 3.0 after 1 hour, refluxed 6 hours down at 80 ℃, make aluminum hydroxide sol;
(4) coating colloidal sol
To immerse in the aluminum hydroxide sol that makes through pretreated porous stainless steel disc, and flood after 1 hour and take out, dry under the room temperature, place sintering furnace again, 1000 ℃ of following roastings 2 hours;
(5) supported palladium
The weight percent concentration of preparation palladium is the Pd (NO of 10mg/ml
3)
2Solution 10ml adopts excessive infusion process, supported palladium on the porous carrier after the modification, and drying is 4 hours under 120 ℃, again 500 ℃ of following roastings 2 hours, makes the catalyst that palladium content is 0.3wt%.
The percentage by weight of obtained catalyst is: carrier 96.5%, intermediate layer 3.2%, active component 0.3%.The volume averaging aperture of obtained catalyst is 8 μ m, and porosity is 35%, and dispersion degree of active components is 60%.
(6) evaluation of catalyst performance
Select for use C3 fraction that the selection hydrogenation catalyst of above-mentioned preparation is carried out activity rating.
Evaluating apparatus adopts micro fixed-bed reactor, and reactor is the stainless steel tube of φ 10mm * 2mm, high 18mm.
Earlier with H
2Be source of the gas, under 120 ℃ of temperature and pressure 0.1MPa, catalyst is activated 3 hours, be cooled to 40 ℃ again, with the flow of 80ml/h feed carbon three liquid charging stocks (mole is formed: propylene 92%, propine 2.3%, allene 1.2%, other 4.5%), then with H
2/ alkynes mol ratio 1.2 feeds hydrogen, reacts under gross pressure 2.2MPa.React after 4 hours,, adopt gas chromatograph to analyze from the reactor outlet sampling.Analysis result shows that the conversion ratio of propine/allene reaches 100%, and selectivity reaches 75%, and propene yield is greater than 100%.
Embodiment 2
Adopt porosity is 55%, average pore size is 20 μ m, be of a size of φ 6mm * 1.5mm porous stainless steel disk (providing) as carrier, use the hexane washing by soaking earlier, again with the soaked in absolute ethyl alcohol washing, dry after the taking-up by Antai Science and Technology Co., Ltd.The Lacunaris metal carrier that cleaned is immersed the NaOH aqueous solution that consists of 40wt%, and 150 ℃ of following processing times are 60 minutes, take out drying for standby.
Prepare aluminum hydroxide sol according to the method among the embodiment 1.To immerse in the aluminum hydroxide sol that makes through pretreated porous stainless steel disc, and flood after 1.5 hours and take out, dry under the room temperature, place sintering furnace again, 1000 ℃ of following roastings 2 hours.The percentage by weight of obtained catalyst is: carrier 96%, intermediate layer 3.5%, active component 0.5%.The volume averaging aperture of obtained catalyst is 18 μ m, and porosity is 50%, and dispersion degree of active components is 65%.
Carry out activity rating in the micro fixed-bed reactor of embodiment 1, reaction unit and condition are with embodiment 1.Feed carbon three liquid charging stocks (mole is formed: propylene 94.0%, propine 2.0%, allene 1.2%, other is 2.8% years old) with the flow of 100ml/h, then with H
2/ alkynes mol ratio 1.1 feeds hydrogen, reacts under gross pressure 2.2MPa.React after 4 hours,, adopt gas chromatograph to analyze from the reactor outlet sampling.Analysis result shows that the conversion ratio of propine/allene reaches 100%, and selectivity reaches 80%, and propene yield is greater than 100%.
Claims (8)
1. select hydrogenation catalyst for one kind, it is characterized in that, described selection hydrogenation catalyst is elder generation's load carriers intermediate layer, catalyst of carried noble metal component on this carrier intermediate layer again on Lacunaris metal carrier;
Described Lacunaris metal carrier is a kind of of porous metals or porous metals alloy; Described carrier intermediate layer is the inorganic oxide carrier layer.
2. selection hydrogenation catalyst as claimed in claim 1, it is characterized in that, gross weight based on catalyst, described Lacunaris metal carrier is 95 weight %～97.9 weight %, described carrier intermediate layer is 2 weight %～4 weight %, described noble metal component is 0.1 weight %～1.0 weight %, and the decentralization of described noble metal component is 50%～80%.
3. selection hydrogenation catalyst as claimed in claim 1 or 2 is characterized in that, the porosity of described Lacunaris metal carrier is 30%～80%, and the volume averaging aperture is 5～100 μ m.
4. selection hydrogenation catalyst as claimed in claim 1 or 2 is characterized in that, described carrier intermediate layer is SiO
2, TiO
2Or Al
2O
3
5. selection hydrogenation catalyst as claimed in claim 1 or 2 is characterized in that, described noble metal component is palladium, platinum or rhodium.
6. the described selection hydrogenization catalyst preparation method of claim 1 is characterized in that described preparation method may further comprise the steps:
(1) preparation Lacunaris metal carrier: the porous metals of selecting are made required form and size;
(2) preliminary treatment Lacunaris metal carrier: porous metals are immersed cleaning in the washing lotion, oven dry; Porous metals are immersed in the strong oxidation liquid handled 10 minutes～2 hours, take out then, use washed with de-ionized water, drying;
(3) preparation carrier intermediate layer: the Lacunaris metal carrier that step (2) is obtained was immersed in the colloidal sol of parent in carrier intermediate layer 0.5～2 hour, took out dryly, through roasting the colloidal sol of dipping was decomposed into oxide, made the carrier intermediate layer;
(4) load active component: use active component parent solution with infusion process with active constituent loading on the carrier intermediate layer, drying, roasting, reduction makes catalyst of the present invention.
7. preparation method as claimed in claim 6 is characterized in that, is one or more mixture in the volatile organic solvent in washing lotion described in the step (2), and described strong oxidation liquid is strong basicity oxidation liquid, and oxidizing temperature is 120～150 ℃.
8. preparation method as claimed in claim 6 is characterized in that, the colloidal sol of the parent in described carrier intermediate layer is a kind of in aluminium oxide, silica, the titanium oxide sol, and the concentration of colloidal sol is 3 weight %～8 weight %.
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| CNB200610076636XA CN100531912C (en) | 2006-04-27 | 2006-04-27 | Novel selective hydrogenation catalyst and preparation method thereof |
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|---|---|---|---|
| CNB200610076636XA CN100531912C (en) | 2006-04-27 | 2006-04-27 | Novel selective hydrogenation catalyst and preparation method thereof |
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| CN101062483A true CN101062483A (en) | 2007-10-31 |
| CN100531912C CN100531912C (en) | 2009-08-26 |
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| US20100125158A1 (en) * | 2008-11-19 | 2010-05-20 | Antoine Negiz | Methods for Selective Hydrogenation Performance Using a Layered Sphere Catalyst With New Formulations |
| CN103030503A (en) * | 2011-09-29 | 2013-04-10 | 中国石油化工股份有限公司 | Method for preparing propylene by using methanol |
| CN105521828A (en) * | 2015-12-14 | 2016-04-27 | 谭陆翠 | Supporter for chemical industry |
| CN105536880A (en) * | 2015-12-14 | 2016-05-04 | 谭陆翠 | Petroleum catalyst carrier |
| RU2601751C1 (en) * | 2015-11-11 | 2016-11-10 | Федеральное государственное бюджетное учреждение науки Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук | Method for selective hydrogenation of acetylene hydrocarbons |
| CN108855128A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | A kind of selective hydrogenation catalyst and preparation method thereof |
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| US6309758B1 (en) * | 1999-05-06 | 2001-10-30 | W. R. Grace & Co.-Conn. | Promoted porous catalyst |
| CN1142026C (en) * | 1999-06-23 | 2004-03-17 | 中国石油化工集团公司 | Composite ZSM-5 zeolite-porous metal material and its preparing process |
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| CN103030503B (en) * | 2011-09-29 | 2015-04-08 | 中国石油化工股份有限公司 | Method for preparing propylene by using methanol |
| RU2601751C1 (en) * | 2015-11-11 | 2016-11-10 | Федеральное государственное бюджетное учреждение науки Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук | Method for selective hydrogenation of acetylene hydrocarbons |
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| CN105536880A (en) * | 2015-12-14 | 2016-05-04 | 谭陆翠 | Petroleum catalyst carrier |
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| CN108855128A (en) * | 2017-05-15 | 2018-11-23 | 中国石油天然气股份有限公司 | A kind of selective hydrogenation catalyst and preparation method thereof |
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| CN114585599A (en) * | 2019-12-03 | 2022-06-03 | 中国石油化工股份有限公司 | Method for preparing mono-olefin by hydrogenation of diolefin |
| CN112892612B (en) * | 2019-12-03 | 2023-01-17 | 中国石化集团金陵石油化工有限责任公司 | Catalyst for hydrocarbon conversion reaction |
| RU2800754C1 (en) * | 2019-12-03 | 2023-07-27 | Синопек Цзиньлин Петрокемикал Ко., Лтд. | Method for producing monoolefin by hydrogenation of diolefin |
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| CN114682250A (en) * | 2020-12-29 | 2022-07-01 | 国家能源投资集团有限责任公司 | Ceramic fiber filter tube catalyst and stepwise preparation method thereof |
| CN114682250B (en) * | 2020-12-29 | 2023-09-05 | 国家能源投资集团有限责任公司 | Ceramic fiber filter tube catalyst and stepwise preparation method thereof |
| CN113979788A (en) * | 2021-11-23 | 2022-01-28 | 亚细亚建筑材料股份有限公司 | Self-cleaning super-hydrophilic ceramic material and preparation method thereof |
| CN113979788B (en) * | 2021-11-23 | 2023-10-03 | 亚细亚建筑材料股份有限公司 | Self-cleaning super-hydrophilic ceramic material and preparation method thereof |
| CN116212950A (en) * | 2021-12-02 | 2023-06-06 | 惠生工程（中国）有限公司 | Metal porous heat-conducting catalyst system and method for preparing glycolide at low temperature and low pressure |
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