WO2016029702A1 - 氢化触媒及其制造方法 - Google Patents

氢化触媒及其制造方法 Download PDF

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WO2016029702A1
WO2016029702A1 PCT/CN2015/076830 CN2015076830W WO2016029702A1 WO 2016029702 A1 WO2016029702 A1 WO 2016029702A1 CN 2015076830 W CN2015076830 W CN 2015076830W WO 2016029702 A1 WO2016029702 A1 WO 2016029702A1
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hydrogenation catalyst
noble metal
catalyst according
nickel
producing
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French (fr)
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陈志勇
王振乾
洪启源
黄麟翔
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    • 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
    • B01J23/892—Nickel and noble 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/42—Platinum
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    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
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    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/44—Palladium
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/462—Ruthenium
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    • 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
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/464—Rhodium
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    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/33—Electric or magnetic properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B01J35/45—Nanoparticles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/612—Surface area less than 10 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/16—Reducing
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/34—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation
    • B01J37/341—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation
    • B01J37/342—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of electric or magnetic fields, wave energy or particle radiation of electric, magnetic or electromagnetic fields, e.g. for magnetic separation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/30—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group
    • C07C67/303—Preparation of carboxylic acid esters by modifying the acid moiety of the ester, such modification not being an introduction of an ester group by hydrogenation of unsaturated carbon-to-carbon bonds
    • 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
    • B01J2235/00—Indexing scheme associated with group B01J35/00, related to the analysis techniques used to determine the catalysts form or properties
    • B01J2235/30—Scanning electron microscopy; Transmission electron microscopy
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/58—Fabrics or filaments
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2601/00—Systems containing only non-condensed rings
    • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
    • C07C2601/14—The ring being saturated

Definitions

  • the present invention relates to a hydrogenation catalyst and a method for producing the same, and more particularly to a hydrogenation catalyst having magnetic properties and a method for producing the same.
  • metal catalysts are often used in aromatic hydrogenation systems. Compared with other non-metal catalysts, they are not only clean and have low economic and environmental impact, but also noble metals such as palladium, rhodium, ruthenium and platinum. It has been confirmed that it is a catalytic catalyst having high activity in a hydrogen atmosphere.
  • Bayer Corporation mentioned in Chinese Patent Publication No. 101815575 published in 2010 that its catalyst is used in a gas phase reaction to hydrogenate nitrobenzene to aniline. This method was carried out by mixing 106.4 mg of palladium chloride (PdCl2), 6 ml of hydrochloric acid (HCl) and 294 ml of distilled water to obtain 300 ml of a solution of chloropalladium acid (H2PdCl4).
  • PdCl2 palladium chloride
  • HCl hydrochloric acid
  • H2PdCl4 chloropalladium acid
  • step (a) 15 ml of a H2PdCl4 solution was mixed with 31.5 ml of water and 3.5 ml of methanol, and 33.25 mg of polyvinylpyrrolidone (Polyvinylpyrrolidone, PVP-40) was added, and refluxed at 80 ° C for 3 hours, which is the step (a).
  • TEOS Tetraethoxysilane
  • NH3 ethanol-aqueous ammonia
  • step (b) An aqueous solution of Marlipal was prepared by dissolving 0.43 g of an alcohol-polyglycol ether (such as Marlipal) in 11 g of water.
  • the Pd-SiO2 nanoparticles obtained in the step (b) were dispersed in 40 g of ethanol and heated to 30 ° C, and the aqueous Maripalal solution was added to Pd-SiO 2 at 30 ° C, and 0.45 ml of zirconium n-butoxide was added thereto, and the mixture was stirred for 4 hours.
  • step (c) The liquid phase of the dispersion was replaced with water. Thereafter, calcination is carried out at 900 ° C, which is step (c).
  • the Pd-SiO2-ZrO2 particles obtained in the step (c) were stirred in 50 ml of a 1 mol sodium hydroxide (NaOH) solution for 3 hours, centrifuged and washed with 1 mol of a NaOH solution. Finally, it is dried at room temperature and is a Pd-ZrO2 catalyst.
  • NaOH sodium hydroxide
  • the catalyst was placed in a reactor with a hydrogen-nitrogen mixed atmosphere at a flow rate of 10 ml/min (mL/min) and 40 ml/min (mL/min), respectively, and a benzene feed flow rate of 0.5 ml/hr (mL). /hr), the conversion rate of benzene was 63% at a reaction temperature of 84 °C.
  • the above hydrogenation catalysts are all supported on alumina (Al2O3) or silica (SiO2). After the reaction, the catalyst and the product are separated by a filtration process, and the particles are too fine to be easily filtered.
  • alumina Al2O3
  • silica SiO2
  • platinum is a very rare and expensive metal catalyst for the general chemical reaction, in order to improve efficiency and save resources, the recovery of precious metal catalyst and its recovery efficiency are very important for process cost.
  • the main object of the present invention is to provide a hydrogenation catalyst, a nano-nickel wire having a high specific surface area of a noble metal catalyst, and to improve the catalytic ability of the hydrogenation catalyst by introduction of noble metal nanoparticles.
  • a secondary object of the present invention is to provide a method for producing a hydrogenation catalyst.
  • a chemical reduction reaction is used to induce a non-electroplating reduction in a simple magnetic field, and the nano nickel crystals are self-assembled into a one-dimensional nanowire structure to form a A carrier having magnetic properties.
  • noble metal nanoparticles are grown on the surface by reductant addition or auto-oxidation of nickel.
  • the manufacturing process is simple, and a complicated pre-processing step is not required, thereby saving process cost.
  • an embodiment of the present invention provides a hydrogenation catalyst comprising: a nano-nickel carrier; and a noble metal nanoparticle selected from the group consisting of palladium, platinum, rhodium, ruthenium or a mixture thereof, wherein the noble metal nanometer The microparticles are attached to the surface of the nanonickel support.
  • the nano-nickel support has a one-dimensional nanowire structure.
  • the nano nickel support has a specific surface area greater than or equal to 0.2 square meters per gram (m 2 /g).
  • the precious metal nanoparticles comprise from 2.5 to 7% by weight of the hydrogenation catalyst.
  • the noble metal nanoparticles account for 1.5 to 2.5% of the atomic percentage of the hydrogenation catalyst.
  • the hydrogenation catalyst has a specific surface area greater than or equal to 3.0 square meters per gram (m 2 /g).
  • An embodiment of the present invention further provides a method for producing a hydrogenation catalyst, comprising the steps of: (1) preparing a nickel ion aqueous solution; and (2) adding a first reducing agent to the nickel ion aqueous solution to form a reaction solution.
  • the step (1) comprises formulating the aqueous nickel ion solution with nickel chloride and deionized water.
  • the first reducing agent is a hydrazine.
  • the aqueous nickel ion solution further comprises an adjuvant selected from the group consisting of acid methyl cellulose, sodium citrate, sodium hydroxide or a mixture thereof.
  • the weight percentage of the methylcellulose relative to the aqueous nickel ion solution is from 4 to 6%.
  • the step (1) further comprises a step (1a) of heating and stirring until the auxiliary agent is completely dissolved in the aqueous nickel ion solution.
  • the magnetic field is between 500 and 5000 Gauss (G).
  • the first preset time is 1 to 3 hours.
  • the step (4) formulates the aqueous solution of the noble metal ion with the chloride of the noble metal ion and hydrochloric acid.
  • the concentration of the hydrochloric acid is 10 N (mol/kg).
  • the noble metal ion aqueous solution further comprises an additive selected from the group consisting of sodium citrate, sodium hydroxide or a mixture thereof.
  • the step (4) further comprises a step (4a) of heating and stirring until the additive is completely dissolved in the noble metal ion aqueous solution.
  • the step (5) further comprises adding a second reducing agent to accelerate the formation of the noble metal nanoparticles.
  • the second reducing agent is a hydrazine.
  • the second preset time is 1 to 3 hours.
  • 1a to 1c are photographs (10 kV, 10,000, 50,000, 100,000 X) of a nano-nickel wire prepared according to an embodiment of the present invention, observed by a scanning electron microscope (SEM).
  • FIGS. 2a to 2b are photographs (10 kV, 1,000 to 100,000 X) observed by a scanning electron microscope (SEM) of a hydrogenation catalyst according to an embodiment of the present invention.
  • Figure 2a Nano-nickel wire growth platinum catalyst (from right to left, from bottom to top, each of 1,000, 30,000, 50,000, 100,000X);
  • Figure 2b nano-nickel wire growth palladium catalyst (from right to left, from bottom to bottom) Each is 1,000, 30,000, 50,000, 100,000X).
  • Figure 3 Comparison of catalytic effects of Pd/Ni hydrogenation catalyst on toluene at different pressures. ( ⁇ : 70 kg of hydrogen; ⁇ : 50 kg of hydrogen; helium: 70 kg of hydrogen, pure nano-nickel line catalyzed experimental control group)
  • Figure 4 is a graph of a catalytic product of a hydrogenation catalyst for a dimethyl terephthalate (DMT) analyzed by gas chromatography mass spectrometry (GC) according to an embodiment of the present invention.
  • DMT dimethyl terephthalate
  • GC gas chromatography mass spectrometry
  • Figure 5 is a graph of a catalytic product of a hydrogenation catalyst of Diphthyl Phthalate (DOP) of the invention as analyzed by gas chromatography (GC).
  • DOP Diphthyl Phthalate
  • a compound or “at least one compound” may include a plurality of compounds, including mixtures thereof;
  • % as referred to in the present specification means “percent by weight (wt%)" unless otherwise specified; (eg 10% to 11% of A) Unless otherwise specified, the upper and lower limits are included (ie 10% ⁇ A ⁇ 11%); if the value range does not define a lower limit (such as less than 0.2% of B, or B) below 0.2% means that the lower limit may be 0 (ie 0% ⁇ B ⁇ 0.2%); the proportional relationship of the "weight percentage" of each component may also be replaced by the proportional relationship of "parts by weight”.
  • the above terms are used to illustrate and understand the present invention and are not intended to limit the invention.
  • An embodiment of the invention provides a hydrogenation catalyst comprising: a nano-nickel (Ni) carrier; and a noble metal nanoparticle selected from the group consisting of palladium (Pd), platinum (Pt), ruthenium (Ru), rhodium (Rh) ) or a mixture thereof.
  • the noble metal nanoparticles are attached to at least a portion of the surface of the nano nickel support.
  • the noble metal nanoparticles can have the catalytic ability of a hydrogenation reaction, so that in a hydrogen atmosphere, an unsaturated carbon chain bond (mainly a double bond between two carbon atoms) can be converted into a saturated carbon-carbon single bond.
  • the nano-nickel support can be, for example, a nano-nickel wire having a one-dimensional nanowire structure.
  • the specific surface area thereof may be greater than or equal to 0.29 square meters / gram (m 2 / g), such as 0.30, 0.32 or 0.35 m 2 / g, but is not limited thereto.
  • the noble metal nanoparticles accounted for 2.5 to 7% by weight of the hydrogenation catalyst, and may be, for example, 2.9, 3.5 or 6.4%, but are not limited thereto.
  • the noble metal nanoparticles account for 1.5 to 2.5% of the hydrogenation catalyst, and may be, for example, 1.6, 2.1 or 2.3, but are not limited thereto.
  • the hydrogenation catalyst may have a specific surface area greater than or equal to 3.0 m 2 /G, preferably a high specific surface area of from 3.5 to 4.5 m 2 /g, such as 3.7 or 4.3%, but is not limited thereto.
  • a further embodiment of the present invention provides a method for producing a hydrogenation catalyst, which mainly comprises the steps of: (S1) preparing a nickel ion aqueous solution; (S2) adding a first reducing agent to the nickel ion aqueous solution to Forming a reaction solution; (S3) applying a magnetic field to the reaction solution for a first predetermined time to obtain a nano-nickel carrier; (S4) preparing a noble metal ion aqueous solution containing a noble metal ion selected from palladium Platinum, rhodium, ruthenium or a mixed ion thereof; and (S5) placing the nano-nickel support in the noble metal ion aqueous solution for a second predetermined time to connect a part of the surface of the nano-nickel support to a precious metal Nanoparticles.
  • S1 preparing a nickel ion aqueous solution
  • S2 adding a first reducing agent to the nickel ion aqueous solution to Forming a
  • the method for producing a hydrogenation catalyst according to an embodiment of the present invention is first: (S1) preparing a nickel ion aqueous solution.
  • the aqueous nickel ion solution may be prepared using nickel ion salts and deionized water.
  • the nickel ion salt can be, for example, nickel chloride, nickel nitrate or nickel hydroxide.
  • the aqueous nickel ion solution may further comprise an adjuvant selected from the group consisting of acid methyl cellulose (CMC), sodium citrate, sodium hydroxide or a mixture thereof. The ratio of the acid methylcellulose added is relative to the aqueous nickel ion solution.
  • the percentage of the amount is 4 to 6%, and may be, for example, 4.5, 5 or 6%, but is not limited thereto.
  • the sodium citrate is added in a proportion of 5 to 9% by weight based on the aqueous nickel ion solution.
  • the sodium hydroxide is added in a proportion of 0.5 to 2% by weight based on the aqueous nickel ion solution.
  • the auxiliary agent added is a solid, it may further comprise a step (S1a), heating and stirring until the auxiliary agent is completely dissolved in the aqueous nickel ion solution.
  • the method for producing a hydrogenation catalyst according to an embodiment of the present invention is followed by: (S2) adding a first reducing agent to the aqueous nickel ion solution to form a reaction solution.
  • the first reducing agent can be, for example, a hydrazine or hydrogen peroxide.
  • the added ratio is from 3 to 9% by weight based on the aqueous nickel ion solution, and may be, for example, 3, 6, or 9%, but is not limited thereto.
  • the method for producing a hydrogenation catalyst according to an embodiment of the present invention is followed by: (S3) applying a magnetic field to the reaction solution to perform a reaction for a first predetermined time to obtain a nano-nickel carrier.
  • the magnetic field is 500 to 5000 Gauss (G).
  • the first preset time is 1 to 3 hours, and may be, for example, 1, 1.5, 2, or 2.5 hours, but is not limited thereto.
  • the method for producing a hydrogenation catalyst according to an embodiment of the present invention is followed by: (S4) preparing an aqueous solution of a noble metal ion comprising a noble metal ion selected from the group consisting of palladium, platinum, rhodium, ruthenium or a mixed ion thereof.
  • the noble metal ion aqueous solution may be prepared using the noble metal ion salt and hydrochloric acid.
  • the noble metal ion salt may be, for example, palladium chloride, palladium bromide, palladium nitrate or hexachloroplatinic acid.
  • the concentration of the hydrochloric acid may be, for example, 10 N (molar concentration, mol/kg), but is not limited thereto.
  • the noble metal ion aqueous solution may further comprise an additive selected from the group consisting of sodium citrate, sodium hydroxide or a mixture thereof.
  • the weight percentage of the sodium citrate added to the aqueous solution of the noble metal ion is 5 to 9%, and the weight percentage of the sodium hydroxide added to the aqueous solution of the noble metal ion is 0.5 to 2%.
  • the auxiliary agent added is a solid, it may further comprise a step (S4a): heating and stirring until the additive is completely dissolved in the noble metal ion aqueous solution.
  • the method for producing a hydrogenation catalyst according to an embodiment of the present invention is followed by: (S5) placing the nano-nickel carrier into the noble metal ion aqueous solution, performing a second predetermined time reaction, and connecting a portion of the surface of the nano-nickel carrier to a surface Precious metal nanoparticles.
  • the noble metal nanoparticles are formed by reducing the noble metal ions by the nano-nickel carrier (ie, using the two metal oxidation potential differences to auto-oxidize and reduce without adding an additional reducing agent, but the speed is slow), or A second reducing agent is added to the noble metal ion aqueous solution to accelerate the formation of the noble metal nanoparticles.
  • the second reducing agent can be, for example, a hydrazine or hydrogen peroxide. Further, the ratio of the second reducing agent to be added is from 3 to 9% by weight with respect to the noble metal ion solution, and may be, for example, 3, 6, or 9%, but is not limited thereto.
  • the second preset time is 1 to 3 hours, and may be, for example, 1, 1.5, 2, or 2.5 hours, but is not limited thereto.
  • the preparation method of the hydrogenation catalyst is merely an example, and is not intended to limit the composition of the hydrogenation catalyst and the method for producing the same.
  • the preparation of the nano-nickel carrier is first carried out: an aqueous solution is prepared by adding 1.2 g of nickel chloride and 50 ml of deionized water, and 2.5 g of acid methylcellulose (CMC) is added. It accounts for about 5% of the total. Next, 3.5 g of sodium citrate and 0.4 g of sodium hydroxide were sequentially added to the aqueous solution, and stirred at 80 ° C until the solid portion was completely dissolved. Next, 2 ml of hydrazine was added to form a mixed solution (a). The mixed solution (a) was placed in a fixed magnetic field, and a reduction reaction was carried out for 2 hours.
  • CMC acid methylcellulose
  • the CMC is removed by deionized water at 70 ° C, and the obtained nano nickel wire is stored in ethanol for use.
  • the manufactured nanonickel wire was observed by a scanning electron microscope (SEM) as shown in Figs. 1a to 1c.
  • the nano-nickel wire has a specific surface area of about 0.298 m 2 /g after calculation by the BET method (adsorption theory proposed by Stephen Brunauer, Paul Hugh Emmett, and Edward Teller, BET for short).
  • the nano-nickel is grown on the nano-platinum metal particles to complete the production of the Pt/Ni hydrogenation catalyst, and the process step is: disposing an aqueous solution of hexachloroplatinic acid with a platinum content of 0.4 g/100 ml. 7.5 ml of an aqueous solution of hexachloroplatinic acid and 20 ml of deionized water were mixed, 0.5 g of sodium citrate and 0.4 g of sodium hydroxide were added, and stirred at 60 ° C until dissolved to form a mixed solution (b). One gram of the nanonickel wire was added to the mixed solution (b), and 12 ml of hydrazine was added thereto for reduction for 2 hours.
  • the nano-nickel wire-grown platinum catalyst was stored in acetone after repeated washing with deionized water.
  • the Pt/Ni hydrogenation catalyst produced was observed by SEM for its growth structure as shown in Fig. 2a. Further, the specific surface area of the Pt/Ni hydrogenation catalyst was calculated by the BET method to be 4.36 m 2 /g.
  • the platinum nanoparticles accounted for about 6.4% by weight of the Pt/Ni hydrogenation catalyst, and the atomic percentage was about 2.02%.
  • the nano-nickel is grown on the nanometer palladium metal particles to complete the manufacture of the Pd/Ni hydrogenation catalyst, and the process steps are: disposing 100 ml of 10N hydrochloric acid aqueous solution, and adding 1.77 g of palladium chloride to the aqueous hydrochloric acid solution. The mixture was stirred at 70 ° C until dissolved to prepare an aqueous palladium chloride solution. Next, 180 ml of an aqueous solution of palladium chloride was added, and 3 g of sodium citrate and 2.4 g of sodium hydroxide were added, and the mixture was stirred at 60 ° C until dissolved to form a mixed liquid (c).
  • nanonickel wire-grown palladium catalyst was stored in acetone after repeated washing with deionized water.
  • the Pd/Ni hydrogenation catalyst produced was observed by SEM for its growth structure as shown in Fig. 2b. Further, the specific surface area of the Pd/Ni hydrogenation catalyst calculated by the BET method was 3.77 m 2 /g.
  • the palladium nanoparticles accounted for about 2.93% by weight of the Pd/Ni hydrogenation catalyst, and the atomic percentage was about 1.64%.
  • FIG. 3 is a comparison diagram of the catalytic effect of Pd/Ni hydrogenation catalyst on toluene under different pressures. Its hydrogenation reaction formula is as follows:
  • the temperature is lowered, the hydrogen gas is vented, and the hydrogen in the reaction vessel is removed by nitrogen aeration (pressure 30 to 40 psi) for 10 to 15 minutes. Subsequently, the catalyst and the product were separated by a strong magnet, and the recovery rate was over 96%.
  • the Pd/Ni hydrogenation catalyst catalyzes the reaction of toluene to form methylcyclohexane.
  • the reaction temperature is 180 ° C
  • the hydrogen pressure is 70 Kg/cm 2
  • the toluene can be completely reacted to methylcyclohexane after 100 minutes.
  • the hydrogen pressure is 50 Kg/cm2
  • complete hydrogenation can also be achieved after 150 minutes of reaction.
  • a pure nano-nickel wire was used as the hydrogenation catalyst, the reaction hardly proceeded.
  • FIG. 4 is a map of a catalytic product of Pd/Ni hydrogenation catalyst catalyzed by Dimethyl Terephthalate (DMT) by gas chromatography (GC). Its hydrogenation reaction formula is as follows:
  • the hydrogen pressure was set to 60 kg/cm 2 and the reaction temperature was 200 ° C.
  • the remaining steps and reaction conditions were the same as the above-mentioned toluene hydrogenation reaction. After 180 minutes of reaction, the hydrogenation rate was 90% and the product purity was 97.36%. Catalyst recovery rate can reach more than 96%.
  • FIG. 5 is a map of a catalytic product of Pd/Ni hydrogenation catalyst catalyzed by Dioctyl Phthalate (DOP) by gas chromatography (GC). Its hydrogenation reaction formula is as follows:
  • the hydrogen pressure was set to 60 kg/cm2
  • the reaction temperature was 200 ° C
  • the remaining steps and reaction conditions were the same as the above-mentioned toluene hydrogenation reaction.
  • the hydrogenation rate can also reach 90% or more.
  • Catalyst recovery rate can reach more than 96%.
  • Pd/Ni hydrogenation catalyst catalyzed polystyrene except that the reactant was 5 g of polystyrene and 45 g of cyclohexane, the hydrogen pressure was set to 200 psi, the reaction temperature was 80 ° C, and the remaining steps and The reaction conditions are the same as those described above for the hydrogenation of toluene After the reaction for 30 minutes, the hydrogenation rate was confirmed to be 80% or more.
  • the hydrogenation catalyst and the method for producing the same according to the present invention can improve the catalytic ability of the hydrogenation catalyst by introducing the noble metal nanoparticles, and can easily recover the nanocatalyst by utilizing the magnetic properties of the catalyst itself. Solution It is difficult to reuse nano-catalysts and significantly reduce material costs. In addition, the manufacturing process of the hydrogenation catalyst is simple, no complicated pretreatment is required, and the process cost is saved.

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Abstract

一种氢化触媒，包含：一纳米镍载体；以及一贵金属纳米微粒，选自于钯、铂、钌、铑或其混合物，连接于该纳米镍载体的表面上。所述氢化触媒的制造方法包括步骤：（1）配制一镍离子溶液；（2）在该镍离子水溶液中加入第一还原剂，以形成一反应溶液；（3）施加一磁场于该反应溶液，进行第一预设时间的反应，获得一纳米载体；（4）配置一贵金属离子水溶液；以及（5）将该纳米镍载体置入该贵金属离子水溶液中，使该纳米镍载体的至少一部分表面上连接一贵金属纳米微粒。

Description

氢化触媒及其制造方法 【技术领域】
本发明关于一种氢化触媒及其制造方法，特别是关于一种具有磁性的氢化触媒及其制造方法。
【背景技术】
一般而言在芳香族化合物氢化系统中常采用金属触媒，相较于其它非金属触媒的催化反应，不仅干净且具有较低的经济与环境冲击，此外贵金属如钯、钌、铑以及白金，都已被证实在氢气的环境下是具有高活性的催化触媒。
举例来说，拜耳公司在2005年发表的美国专利公告第6,841,626B1号中，使用贵金属铂(Pt)及钯(Pd)作为触媒，SiO2与Al2O3作为触媒载体，使用环己烷为溶剂，对聚苯乙烯进行氢化反应，Pt/SiO2在压力875巴(bar)，温度150℃下氢化率为98.4％，而Pd/Al2O3在压力100巴，温度200℃下氢化率为100％。
此外，拜耳公司在2010年发表的中国专利公告第101815575号提到，其触媒应用于气相反应中，可将硝基苯氢化为苯胺。该方法是将106.4毫克的氯化钯(PdCl2)、6毫升的盐酸(HCl)和294毫升的蒸馏水混合，得到300毫升的氯钯酸(H2PdCl4)溶液。将15毫升的H2PdCl4溶液与31.5毫升的水和3.5毫升的甲醇混合，添加33.25毫克的聚乙烯吡咯烷酮(Polyvinylpyrrolidone，PVP-40)，在80℃回流3小时，此为步骤(a)。将0.6毫升的四乙氧基硅烷(Tetraethoxysilane，TEOS)与7毫升的乙醇混合。将步骤(a)的混合溶液剧烈搅拌，然后添加乙醇-氨水(NH3)混合物。然后快速添加乙醇-TEOS混合物，在室温搅拌整晚，经无水乙醇清洗离心后获得Pd-SiO2纳米颗粒，此为步骤(b)。将0.43克的醇-聚乙二醇醚(如Marlipal)溶解在11克的水制备Marlipal水溶液。将步骤(b)得到的Pd-SiO2纳米颗粒分散到40克乙醇中，并加热到30℃，将Marlipal水溶液添加到30℃的Pd-SiO2中，加入0.45毫升正丁醇锆，搅拌4小时后，用水置换该分散体的液相。之后，经900℃锻烧，此为步骤(c)。将步骤(c)得到的Pd-SiO2-ZrO2颗粒在50毫升，1摩尔的氢氧化纳(NaOH)溶液中搅拌3小时，离心分离再以1摩尔的NaOH溶液洗涤。最后室温下干燥，为Pd-ZrO2触媒。
再者，朱月香等人在2011年发表的中国专利编号CN101289365中，将0.12克硝酸四氨合铂(Pt(NH3)4(NO3)2)和7.4克六水硝酸钴(Co(NO3)2.6H2O)溶于200毫升去离子水，加入3.5克的SiO2载体，搅拌2小时后，于95℃水浴中干燥，经550℃高温锻烧4小时后得到触媒。将触媒置入反应器中，反应器中为氢氮混合气氛，流量分别为10毫升/分(mL/min)和40毫升/分(mL/min)，苯进料流速0.5毫升/小时(mL/hr)，反应温度84℃时，苯的转换率为63％。
然而，上述氢化触媒都是将贵金属附载于氧化铝(Al2O3)或二氧化硅(SiO2)上，反应后需经过滤程序分离触媒及产物，当颗粒太细则有不易过滤的缺点。此外，由于白金对于普遍的化学反应是一种非常少见且昂贵的金属触媒，为了增进效益以及节省资源，对于贵金属触媒的回收及其回收效率对于制程成本来说是很重要的。
故，有必要提供一种氢化触媒及其制造方法，可轻易回收具有贵金属的纳米触媒，解决习用技术所存在的问题。
【发明内容】
本发明的主要目的在于提供一种氢化触媒，具有贵金属触媒高比表面积的纳米镍线，藉由贵金属纳米微粒的导入，提高氢化触媒的催化能力。利用此一具有磁性的氢化触媒于石化、高分子或特化品的高值化关键材料的生产制程中，能够轻易利用触媒本身具有的磁性来回收纳米触媒，解决纳米触媒难以重复利用的问题，大幅降低材料成本。
本发明的次要目的在于提供一种氢化触媒的制造方法，先利用化学还原反应，以简单的磁场诱导配合无电镀还原的方式，使奈米镍晶体自组装排列成一维奈米线结构，形成一具有磁性的载体。随后，再透过还原剂添加或镍的自身氧化还原在其表面成长贵金属纳米微粒。以本发明的氢化触媒的制造方法，其制造程序单纯，不需要复杂的前处理步骤，节省制程成本。
为达上述的目的，本发明的一实施例提供一种氢化触媒，其包含：一纳米镍载体；以及一贵金属纳米微粒，选自于钯、铂、钌、铑或其混合物，其中该贵金属纳米微粒连接于该纳米镍载体的表面上。
在本发明的一实施例中，该纳米镍载体具有一维纳米线结构。
在本发明的一实施例中，该纳米镍载体的比表面积大于或等于0.2平方米/克(m2/g)。
在本发明的一实施例中，该贵金属纳米微粒占该氢化触媒的重量百分比为2.5～7％。
在本发明的一实施例中，该贵金属纳米微粒占该氢化触媒的原子百分比为1.5～2.5％。
在本发明的一实施例中，该氢化触媒的比表面积大于或等于3.0平方米/克(m2/g)。
本发明的一实施例另提供一种氢化触媒的制造方法，其包括步骤：(1)配制一镍离子水溶液；(2)在该镍离子水溶液中加入一第一还原剂，以形成一反应溶液；(3)施加一磁场于该反应溶液，进行一第一预设时间的反应，获得一纳米镍载体；(4)配制一贵金属离子水溶液，其包含一贵金属离子选自于钯、铂、钌、铑或其混合离子；以及(5)将该纳米镍载体置入该贵金属离子水溶液中，进行一第二预设时间的反应，使该纳米镍载体的表面上连接一贵金属纳米微粒。
在本发明的一实施例中，该步骤(1)以氯化镍和去离子水配制该镍离子水溶液。
在本发明的一实施例中，该第一还原剂为联胺。
在本发明的一实施例中，该镍离子水溶液另包含一辅助剂，其选自于酸甲基纤维素、柠檬酸钠、氢氧化钠或其混合物。
在本发明的一实施例中，该甲基纤维素相对于该镍离子水溶液的重量百分比为4～6％。
在本发明的一实施例中，该步骤(1)另包含一步骤(1a)：加热并搅拌至该辅助剂完全溶解于该镍离子水溶液中。
在本发明的一实施例中，该磁场为500～5000高斯(G)。
在本发明的一实施例中，该第一预设时间为1～3小时。
在本发明的一实施例中，该步骤(4)以该贵金属离子的氯化物和盐酸配制该贵金属离子水溶液。
在本发明的一实施例中，该盐酸的浓度为10N(摩尔/公斤)。
在本发明的一实施例中，该贵金属离子水溶液另包含一添加剂，其选自于柠檬酸钠、氢氧化钠或其混合物。
在本发明的一实施例中，该步骤(4)另包含一步骤(4a)：加热并搅拌至该添加剂完全溶解于该贵金属离子水溶液。
在本发明的一实施例中，该步骤(5)另包含添加一第二还原剂，以加速该贵金属纳米微粒的形成。
在本发明的一实施例中，该第二还原剂为联胺。
在本发明的一实施例中，该第二预设时间为1～3小时。
【附图说明】
图1a至1c：本发明一实施例所制备的纳米镍线以扫描式电子显微镜(Scanning Electron Microscope，SEM)观察的照片(10kV，10,000、50,000、100,000X)。
图2a至2b：本发明一实施例的氢化触媒以扫描式电子显微镜(Scanning Electron Microscope，SEM)观察的照片(10kV，1,000～100,000X)。其中图2a：纳米镍线成长白金触媒(从右至左，从下到上各为1,000、30000、50000、100,000X)；图2b：纳米镍线成长钯触媒(从右至左，从下到上各为1,000、30000、50000、100,000X)。
图3：Pd/Ni氢化触媒在不同压力下对甲苯的催化效果比较图。(■：70公斤氢气；●：50公斤氢气；▽：70公斤氢气，纯纳米镍线催化的实验对照组)
图4：本发明一实施例的氢化触媒对于对苯二甲酸二甲酯(Dimethyl Terephthalate，DMT)的催化产物以气相层析质谱仪(GC)分析的图谱。
图5：发明一实施例的氢化触媒对于邻苯二甲酸二辛酯(Dioctyl Phthalate，DOP)的催化产物以气相层析仪(GC)分析的图谱。
【具体实施方式】
为了让本发明的上述及其它目的、特征、优点能更明显易懂，下文将特举本发明较佳实施例，并配合所附附图，作详细说明如下。再者，本发明所提到的单数形式“一”、“一个”和“所述”包括复数引用，除非上下文另有明确规定。例如，术语“一化合物”或“至少一种化合物”可以包括多个化合物，包括其混合物；本发明文中提及的「％」若无特定说明皆指「重量百分比(wt％)」；数值范围(如10％～11％的A)若无特定说明皆包含上、下限值(即10％≦A≦11％)；数值范围若未界定下限值(如低于0.2％的B，或0.2％以下的B)，则皆指其下限值可能为0(即0％≦B≦0.2％)；各成份的「重量百分比」的比例关系亦可置换为「重量份」的比例关系。上述用语是用以说明及理解本发明，而非用以限制本发明。
本发明的一实施例提供一种氢化触媒，其包含：一纳米镍(Ni)载体；以及一贵金属纳米微粒，选自于钯(Pd)、铂(Pt)、钌(Ru)、铑(Rh)或其混合物。其中，该贵金属纳米微粒连接于该纳米镍载体的至少一部分表面上。该贵金属纳米微粒可具有氢化反应的催化能力，因此在氢气环境中，能使不饱和的碳链键结(主要为两碳原子间双键)被转变为饱和的碳-碳单键。该纳米镍载体可例如是具有一维纳米线(nanowire)结构的纳米镍线。该纳米镍载体为纳米镍线时，其比表面积可大于或等于0.29平方米/克(m2/g)，例如0.30、0.32或0.35m2/g，然不限于此。较佳的，该贵金属纳米微粒占该氢化触媒的重量百分比为2.5～7％，可例如是2.9、3.5或6.4％，然不限于此。较佳的，该贵金属纳米微粒占该氢化触媒的原子百分比为1.5～2.5％，可例如是1.6、2.1或2.3，然不限于此。此外，该氢化触媒可具有大于或等于3.0m2/G的比表面积，较佳的具有介于3.5～4.5m2/g的高比表面积，例如3.7或4.3％，然不限于此。
再者，本发明的再一实施例提供一种氢化触媒的制造方法，其主要包括步骤：(S1)配制一镍离子水溶液；(S2)在该镍离子水溶液中加入一第一还原剂，以形成一反应溶液；(S3)施加一磁场于该反应溶液，进行一第一预设时间的反应，获得一纳米镍载体；(S4)配制一贵金属离子水溶液，其包含一贵金属离子选自于钯、铂、钌、铑或其混合离子；以及(S5)将该纳米镍载体置入该贵金属离子水溶液中，进行一第二预设时间的反应，使该纳米镍载体的一部分表面上连接一贵金属纳米微粒。本发明将于下文逐一详细说明该实施例的上述各步骤的实施细节及其原理。
本发明实施例的氢化触媒的制造方法首先为：(S1)配制一镍离子水溶液。在本步骤中，可用镍离子盐类和去离子水调制该镍离子水溶液。该镍离子盐可例如是氯化镍、硝酸镍或氢氧化镍。此外，该镍离子水溶液可另包含一辅助剂，选自于酸甲基纤维素(CMC)、柠檬酸钠、氢氧化钠或其混合物。该酸甲基纤维素所添加的比例，以相对于该镍离子水溶液而言，其重 量百分比为4～6％，可例如是4.5、5或6％，然不限于此。该柠檬酸钠所添加的比例，以相对于该镍离子水溶液而言，其重量百分比5～9％。该氢氧化钠所添加的比例，以相对于该镍离子水溶液而言，其重量百分比0.5～2％。若所添加的该辅助剂为固体，则可另包含一步骤(S1a)，加热并搅拌至该辅助剂完全溶解于该镍离子水溶液中。
本发明实施例的氢化触媒的制造方法接着为：(S2)在该镍离子水溶液中加入一第一还原剂，以形成一反应溶液。该第一还原剂可例如为联胺或双氧水。此外，所添加的比例相对于该镍离子水溶液的重量百分比为3～9％，可例如是3、6或9％，然不限于此。
本发明实施例的氢化触媒的制造方法接着为：(S3)施加一磁场于该反应溶液，进行一第一预设时间的反应，获得一纳米镍载体。在本步骤中，该磁场为500～5000高斯(G)。该第一预设时间为1～3小时，可例如是1、1.5、2或2.5小时，然不限于此。
本发明实施例的氢化触媒的制造方法接着为：(S4)配制一贵金属离子水溶液，其包含一贵金属离子选自于钯、铂、钌、铑或其混合离子。在本步骤中，可用该贵金属离子盐类和盐酸配制该贵金属离子水溶液。该贵金属离子盐可例如是氯化钯、溴化钯、硝酸钯或六氯铂酸。该盐酸的浓度可例如是10N(重量摩尔浓度，摩尔/公斤)，然不限于此。该贵金属离子水溶液可另包含一添加剂，选自于柠檬酸钠、氢氧化钠或其混合物。所添加的该柠檬酸钠相对于该贵金属离子水溶液的重量百分比为5～9％，所添加的该氢氧化钠相对于该贵金属离子水溶液的重量百分比为0.5～2％。若所添加的该辅助剂为固体，则可另包含一步骤(S4a)：加热并搅拌至该添加剂完全溶解于该贵金属离子水溶液。
本发明实施例的氢化触媒的制造方法接着为：(S5)将该纳米镍载体置入该贵金属离子水溶液中，进行一第二预设时间的反应，使该纳米镍载体的一部分表面上连接一贵金属纳米微粒。在本步骤中，该贵金属纳米微粒藉由该纳米镍载体还原该贵金属离子而形成(即利用两金属氧化电位差自身氧化还原，而不用额外添加还原剂，但速度较慢)，或可在该贵金属离子水溶液中添加一第二还原剂，以加速该贵金属纳米微粒的形成。该第二还原剂可例如为联胺或双氧水。此外，该第二还原剂所添加的比例相对于该贵金属离子溶液，具有重量百分比为3～9％，可例如是3、6或9％，然不限于此。该第二预设时间为1～3小时，可例如是1、1.5、2或2.5小时，然不限于此。
为使本发明的氢化触媒及其制造方法更明确，请参考下文所述的实际制造流程。然所述氢化触媒的配制方式仅为范例，并非用于限制该氢化触媒的组成及其制造方法。
在本发明一较佳实施例中，首先进行该纳米镍载体的制备：以1.2克的氯化镍与50毫升的去离子水配制成水溶液，加入2.5克的酸甲基纤维素(CMC)，其占总量约为5％。接着在水溶液中依序加入3.5克的柠檬酸钠和0.4克的氢氧化钠，于80℃搅拌至固体部分完全溶解。 接着加入2毫升的联胺，形成混合液(a)。将该混合液(a)置入一固定磁场中，进行还原反应2小时。待反应完成后，以70℃去离子水移除CMC，获得的纳米镍线则保存于乙醇中备用。所制造的纳米镍线以扫描式电子显微镜(Scanning Electron Microscope，SEM)观察，如图1a至1c所示。该纳米镍线以BET法(Stephen Brunauer、Paul Hugh Emmett、Edward Teller所提出的吸附理论，简称BET)计算后，具有比表面积约为0.298m2/g。
接着，在该纳米镍在线成长纳米铂金属微粒，完成Pt/Ni氢化触媒的制造，其流程步骤为：配置六氯铂酸水溶液，铂含量为0.4g/100ml。取7.5毫升的六氯铂酸水溶液和20毫升的去离子水混合，加入0.5克的柠檬酸钠和0.4克的氢氧化钠，于60℃搅拌至溶解，形成混合液(b)。将1克的纳米镍线加入混合液(b)中，并加入12毫升的联胺，进行还原2小时。待反应完成后，以去离子水反复清洗后，将纳米镍线成长铂触媒保存于丙酮中。所制造的Pt/Ni氢化触媒以SEM观察其生长结构，如图2a所示。此外，经由BET法计算该Pt/Ni氢化触媒的比表面积为4.36m2/g。铂纳米微粒占该Pt/Ni氢化触媒的重量百分比约为6.4％，原子百分比约为2.02％。
可选择的，在该纳米镍在线成长纳米钯金属微粒，完成Pd/Ni氢化触媒的制造，其流程步骤为：配置10N盐酸水溶液100毫升，取1.77克的氯化钯加入该盐酸水溶液中，于70℃下搅拌至溶解，制备氯化钯水溶液。接着取180毫升的氯化钯水溶液，加入3克的柠檬酸钠及2.4克的氢氧化钠，于60℃下搅拌至溶解，形成混合液(c)。将1克的纳米镍线加入混合液(c)中，并加入12毫升的联胺，进行还原2小时。待反应完成后，以去离子水反复清洗后，将纳米镍线成长钯触媒保存于丙酮中。所制造的Pd/Ni氢化触媒以SEM观察其生长结构，如图2b所示。此外，经由BET法计算该Pd/Ni氢化触媒的比表面积为3.77m2/g。钯纳米微粒占该Pd/Ni氢化触媒的重量百分比约为2.93％，原子百分比约为1.64％。
为验证本发明所提供的氢化触媒进行氢化反应的催化效果，进行了下述实验及氢化产物分析。
请参考图3，其为Pd/Ni氢化触媒在不同压力下对甲苯的催化效果比较图。其氢化反应式如下：
Figure PCTCN2015076830-appb-000001
首先，取50克的甲苯至于反应容器中，加入Pd/Ni氢化触媒或纯纳米镍线(对照组)，含量为甲苯的5％。以每分钟1000转的转速搅拌，通入氮气曝气(压力30～40psi)10～15分钟去除反 应容器中的氧气。氮气曝气后，通入氢气曝气(压力30～40psi)10～15分钟去除反应容器中的氮气。氢气压力分别设定为70Kg/cm2、50Kg/cm2，反应温度为180℃，在反应进行不同时间时进行取样，以气相层析仪(GC)分析氢化度。反应完成后降温，泄除氢气，通入氮气曝气(压力30～40psi)10～15分钟去除反应容器中的氢气。随后，以强力磁铁分离触媒与产物，回收率可达96％以上。
从图3可见，Pd/Ni氢化触媒催化甲苯生成甲基环己烷反应，反应温度在180℃时，当氢气压力在70Kg/cm2时，甲苯在100分钟后可完全反应成甲基环己烷，而当氢气压力在50Kg/cm2时，亦可在反应150分钟后达到完全氢化。而使用纯纳米镍线作为氢化触媒时，反应几乎没有进行。
请继续参考图4，其为Pd/Ni氢化触媒催化对苯二甲酸二甲酯(Dimethyl Terephthalate，DMT)的催化产物以气相层析仪(GC)分析的图谱。其氢化反应式如下：
Figure PCTCN2015076830-appb-000002
除了反应物为7.5克的DMT与42.5克的乙酸乙酯，氢气压力设定为60Kg/cm2，反应温度为200℃，其余步骤及反应条件与上述甲苯氢化反应相同。在反应180分钟后，氢化率90％，产物纯度为97.36％。触媒回收率可达96％以上。
请继续参考图5，其为Pd/Ni氢化触媒催化邻苯二甲酸二辛酯(Dioctyl Phthalate，DOP)的催化产物以气相层析仪(GC)分析的图谱。其氢化反应式如下：
Figure PCTCN2015076830-appb-000003
除了反应物为50克的DOP，氢气压力设定为60Kg/cm2，反应温度为200℃，其余步骤及反应条件与上述甲苯氢化反应相同。在反应完全后，氢化率亦可达到90％以上。触媒回收率可达96％以上。
此外，利用Pd/Ni氢化触媒催化聚苯乙烯(polystyrene)，除了反应物为5克的聚苯乙烯和45克的环己烷，氢气压力设定为200psi，反应温度为80℃，其余步骤及反应条件与上述甲苯氢化反应相同。在反应30分钟后，确认其氢化率为80％以上。
相较于习知技术，依照本发明所提供的氢化触媒及其制造方法，由于藉由贵金属纳米微粒的导入，提高氢化触媒的催化能力，且能轻易利用触媒本身具有的磁性来回收纳米触媒，解 决纳米触媒难以重复利用的问题，大幅降低材料成本。此外，氢化触媒的制造步骤单纯，不需要复杂的前处理，节省制程成本。
虽然本发明已以较佳实施例揭露，然其并非用以限制本发明，任何熟习此项技艺的人士，在不脱离本发明的精神和范围内，当可作各种更动与修饰，因此本发明的保护范围当视后附的申请专利范围所界定者为准。

Claims (21)

  1. 一种氢化触媒，其特征在于，其包含：
    一纳米镍载体；以及
    一贵金属纳米微粒，选自于钯、铂、钌、铑或其混合物，其中该贵金属纳米微粒连接于该纳米镍载体的表面上。
  2. 如权利要求1所述的氢化触媒，其特征在于，该纳米镍载体具有一维纳米线结构。
  3. 如权利要求1所述的氢化触媒，其特征在于，该纳米镍载体的比表面积大于或等于0.2平方米/克。
  4. 如权利要求1所述的氢化触媒，其特征在于，该贵金属纳米微粒占该氢化触媒的重量百分比为2.5～7％。
  5. 如权利要求1所述的氢化触媒，其特征在于，该贵金属纳米微粒占该氢化触媒的原子百分比为1.5～2.5％。
  6. 如权利要求1所述的氢化触媒，其特征在于，该氢化触媒的比表面积大于或等于3.0平方米/克。
  7. 一种氢化触媒的制造方法，其特征在于，其包括步骤：
    (1)配制一镍离子水溶液；
    (2)在该镍离子水溶液中加入一第一还原剂，以形成一反应溶液；
    (3)施加一磁场于该反应溶液，进行一第一预设时间的反应，获得一纳米镍载体；
    (4)配制一贵金属离子水溶液，其包含一贵金属离子选自于钯、铂、钌、铑或其混合离子；以及
    (5)将该纳米镍载体置入该贵金属离子水溶液中，进行一第二预设时间的反应，使该纳米镍载体的表面上连接一贵金属纳米微粒。
  8. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该步骤(1)以氯化镍和去离子水配制该镍离子水溶液。
  9. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该镍离子水溶液另包含一辅助剂，其选自于酸甲基纤维素、柠檬酸钠、氢氧化钠或其混合物。
  10. 如权利要求9所述的氢化触媒的制造方法，其特征在于，该酸甲基纤维素相对于该镍离子水溶液的重量百分比为4～6％。
  11. 如权利要求9所述的氢化触媒的制造方法，其特征在于，该步骤(1)另包含一步骤(1a)：加热并搅拌至该辅助剂完全溶解于该镍离子水溶液中。
  12. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该第一还原剂为联胺。
  13. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该磁场为500～5000高斯。
  14. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该第一预设时间为1～3小时。
  15. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该步骤(4)以该贵金属离子的氯化物和盐酸配制该贵金属离子水溶液。
  16. 如权利要求15所述的氢化触媒的制造方法，其特征在于，该盐酸的浓度为10摩尔/公斤。
  17. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该贵金属离子水溶液另包含一添加剂，其选自于柠檬酸钠、氢氧化钠或其混合物。
  18. 如权利要求17所述的氢化触媒的制造方法，其特征在于，该步骤(4)另包含一步骤(4a)：加热并搅拌至该添加剂完全溶解于该贵金属离子水溶液。
  19. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该步骤(5)另包含添加一第二还原剂，以加速该贵金属纳米微粒的形成。
  20. 如权利要求19所述的氢化触媒的制造方法，其特征在于，该第二还原剂为联胺。
  21. 如权利要求7所述的氢化触媒的制造方法，其特征在于，该第二预设时间为1～3小时。
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