Composite catalyst, method for manufacturing composite catalyst and application thereof

Abstract

A composite catalyst includes a carrier and noble metal particles supported by the carrier, wherein the carrier is a nitrogen-doped porous carbon composite material having a plurality of passages. The nitrogen-doped porous carbon composite material can include a nitrogen-doped porous carbon material and a plurality of metal oxide particles. The plurality of metal oxide particles can be uniformly distributed in the nitrogen-doped porous carbon material. The plurality of metal oxide particles can be partially exposed through the plurality of passages. The noble metal particles can be tightly combined with the exposed metal oxide particles to achieve recombination. And the noble metal particles can be at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles, or a combination thereof.

Claims

1. A method for manufacturing a composite catalyst comprising: dissolving a metal source in a solvent to obtain a premix; sequentially adding a nitrogen-containing biomass and a pore-forming agent to the premix, such that the metal source reacts with the pore-forming agent to obtain a mixture containing a metal precipitate, wherein the pore-forming agent is at least one of ammonium bicarbonate, ammonium carbonate, ammonium oxalate, ammonium hydrogen oxalate, oxalic acid, or a combination thereof, and a molar ratio of the metal source to the pore-forming agent is in a range of 1:1 to 1:20; treating the mixture by a first calcination at 500 degrees centigrade to 1200 degrees centigrade under an inert atmosphere to obtain a nitrogen-doped porous carbon composite material having a plurality of passages, wherein the nitrogen-doped porous carbon composite material comprises a nitrogen-doped porous carbon material and a plurality of metal oxide particles, the plurality of metal oxide particles are uniformly distributed in the nitrogen-doped porous carbon material, and a part of the plurality of metal oxide particles are exposed through the plurality of passages; and forming noble metal particles in the plurality of passages and combining noble metal atoms with oxide atoms of the exposed part of the plurality of metal oxide particles.

2. The method for manufacturing the composite catalyst of claim 1, wherein the forming the noble metal particles in the plurality of passages comprises: immersing the nitrogen-doped porous carbon composite material in a noble metal precursor solution; and treating the nitrogen-doped porous carbon composite material by a second calcination and a hydrogen reduction to obtain noble metal particles in the plurality of passages.

3. The method for manufacturing the composite catalyst of claim 2, wherein a noble metal precursor in the noble metal precursor solution is at least one of PdCl.sub.2, H.sub.2PdCl.sub.4, Pd(NO.sub.3).sub.2, Pd(NH.sub.3).sub.4(NO.sub.3).sub.2, H.sub.2PtCl.sub.6.Math.6H.sub.2O, [Pt(NH.sub.3).sub.4](NO.sub.3).sub.2, Na.sub.2PtCl.sub.4.Math.xH.sub.2O, H.sub.8C.sub.14N.sub.2Pt, PtCl.sub.4, Pt(C.sub.5H.sub.7O.sub.2).sub.2, C.sub.10H.sub.14O.sub.4Pt, (NH.sub.4).sub.2RuCl.sub.6, RuCl.sub.3, C.sub.15H.sub.21O.sub.6Ru, H.sub.12Cl.sub.6N.sub.3Rh, RhN.sub.3O.sub.9, RhCl.sub.3.Math.3H.sub.2O, IrCl.sub.3, Na.sub.2IrCl.sub.6.Math.6H.sub.2O, H.sub.2IrCl.sub.6.Math.xH.sub.2O, [CH.sub.3COCHC(O)CH.sub.3].sub.3Ir, NaAuCl.sub.4.Math.2H.sub.2O, HAuCl.sub.4.Math.XH.sub.2O, (NH.sub.4)AuCl.sub.4, or a combination thereof.

4. The method for manufacturing the composite catalyst of claim 2, wherein in the second calcination, a calcination temperature is in a range of 200 degrees centigrade to 500 degrees centigrade, a heating rate is in a range of 1 degree centigrade per minute to 20 degrees centigrade per minute, the time is in a range of 1 minute to 240 minutes; in the hydrogen reduction, a reduction temperature is in a range of 150 degrees centigrade to 500 degrees centigrade, a heating rate is in a range of 1 degree centigrade per minute to 20 degrees centigrade per minute, the time is in a range of 1 minute to 360 minutes, and a flow rate of hydrogen gas is in a range of 20 milliliters per minute to 200 milliliters per minute.

5. The method for manufacturing the composite catalyst of claim 1, wherein the forming the noble metal particles in the plurality of passages comprises: immersing the nitrogen-doped porous carbon composite material in a noble metal precursor solution; and adding a reductant which reacts with a noble metal precursor of the noble metal precursor solution to obtain noble metal particles in the plurality of passages.

6. The method for manufacturing the composite catalyst of claim 5, wherein the noble metal precursor of the noble metal precursor solution is at least one of PdCl.sub.2, H.sub.2PdCl.sub.4, Pd(NO.sub.3).sub.2, Pd(NH.sub.3).sub.4(NO.sub.3).sub.2, H.sub.2PtCl.sub.6.Math.6H.sub.2O, [Pt(NH.sub.3).sub.4](NO.sub.3).sub.2, Na.sub.2PtCl.sub.4.Math.xH.sub.2O, H.sub.8C.sub.14N.sub.2Pt, PtCl.sub.4, Pt(C.sub.5H.sub.7O.sub.2).sub.2, C.sub.10H.sub.14O.sub.4Pt, (NH.sub.4).sub.2RuCl.sub.6, RuCl.sub.3, C.sub.15H.sub.21O.sub.6Ru, H.sub.12Cl.sub.6N.sub.3Rh, RhN.sub.3O.sub.9, RhCl.sub.3.Math.3H.sub.2O, IrCl.sub.3, Na.sub.2IrCl.sub.6.Math.6H.sub.2O, H.sub.2IrCl.sub.6.Math.xH.sub.2O, [CH.sub.3COCHC(O)CH.sub.3].sub.3Ir, NaAuCl.sub.4.Math.2H.sub.2O, HAuCl.sub.4.Math.XH.sub.2O, (NH.sub.4)AuCl.sub.4, or a combination thereof.

7. The method for manufacturing the composite catalyst of claim 5, wherein the reductant is at least one of NaBH.sub.4, HCOOH, and hydrazine hydrate, or a combination thereof, and a molar ratio of the reductant to the noble metal precursor of the noble metal precursor solution is in a range of 1:1 to 1000:1.

8. The method for manufacturing the composite catalyst of claim 1, wherein the metal source is at least one of cerium nitrate, zirconium nitrate, aluminum nitrate, or a combination thereof, the solvent is water, and the nitrogen-containing biomass is at least one of bamboo, chitin, carboxymethyl chitin, chitosan, carboxymethyl chitosan, glucosamine hydrochloride, or a combination thereof.

9. The method for manufacturing the composite catalyst of claim 1, wherein a mass ratio of the metal source to the nitrogen-containing biomass is in a range of 0.05:1 to 2:1.

10. The method for manufacturing the composite catalyst of claim 1, wherein a calcination time during the first calcination is in a range of 0.1 hour to 5 hours.

11. A composite catalyst manufactured by the method of claim 1 comprising a carrier and noble metal particles supported by the carrier, wherein the carrier is a nitrogen-doped porous carbon composite material having a plurality of passages, the nitrogen-doped porous carbon composite material comprises a nitrogen-doped porous carbon material and a plurality of metal oxide particles, the plurality of metal oxide particles are uniformly distributed in the nitrogen-doped porous carbon material, the plurality of metal oxide particles are partially exposed through the plurality of passages, noble metal atoms of the noble metal particles are tightly combined with oxide atoms of the exposed metal oxide particles to achieve recombination, and the noble metal particles are at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles, or a combination thereof.

12. The composite catalyst of claim 11, wherein the noble metal particles have a dispersity of 75% to 95% in the nitrogen-doped porous carbon composite material.

13. The composite catalyst of claim 11, wherein a weight percentage of the noble metal particles in the composite catalyst is in a range of 0.1% to 10%, a weight percentage of the metal oxide particles in the composite catalyst is in a range of 2% to 30%, a weight percentage of the nitrogen-doped porous carbon composite material in the composite catalyst is in a range of 60% to 97.9%, and a weight percentage of nitrogen element in the nitrogen-doped porous carbon composite material is in a range of 0.5% to 15%.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a scanning electron micrograph of a nitrogen-doped porous carbon composite material in embodiment 1.

(2) FIG. 2 is a transmission electron micrograph of a nitrogen-doped porous carbon composite material in embodiment 1.

(3) FIG. 3 is a transmission electron micrograph of a composite catalyst in embodiment 1.

(4) FIG. 4 is an X-ray photoelectron spectroscopy of a nitrogen-doped porous carbon composite material and a composite catalyst in embodiment 1, wherein a is corresponding to the nitrogen-doped porous carbon composite material, and b is corresponding to the composite catalyst.

(5) FIG. 5 is a schematic view showing processes of selective hydrogenations using composite catalysts in the present disclosure.

DETAILED DESCRIPTION

(6) The technical solutions of the embodiments of the present disclosure are clearly and completely described below. It is obvious that the described embodiments are only a part and not all of the embodiments of the present disclosure. All other embodiments obtained by one skilled in the art based on the embodiments of the present disclosure without any creative efforts are within the scope of the present disclosure.

(7) The present disclosure provides a method for manufacturing a composite catalyst. The method includes the following steps:

(8) S1, dissolving a metal source in a solvent to obtain a premix;

(9) S2, sequentially adding a nitrogen-containing biomass and a pore-forming agent to the premix, such that the metal source reacts with the pore-forming agent to obtain a mixture containing a metal precipitate, wherein the pore-forming agent is at least one of ammonium bicarbonate, ammonium carbonate, ammonium oxalate, ammonium hydrogen oxalate, oxalic acid, or a combination thereof, and a molar ratio of the metal source to the pore-forming agent is in a range of 1:1 to 1:20;

(10) S3, treating the mixture by a first calcination at 500 degrees centigrade to 1200 degrees centigrade under an inert atmosphere to obtain a nitrogen-doped porous carbon composite material having a plurality of passages, wherein the nitrogen-doped porous carbon composite material comprises a nitrogen-doped porous carbon material and a plurality of metal oxide particles, the plurality of metal oxide particles are uniformly distributed in the nitrogen-doped porous carbon material, and a part of the plurality of metal oxide particles are exposed through the plurality of passages; and

(11) S4, forming noble metal particles in the plurality of passages and combining noble metal atoms with oxide atoms of the exposed part of the plurality of metal oxide particles.

(12) In the step S1, the metal source can play a role of carrying a noble metal catalyst. The metal source needs to be soluble in the solvent. In one embodiment, the metal source can be at least one of cerium nitrate, zirconium nitrate, aluminum nitrate, or a combination thereof, and the solvent can be water. A ratio of the metal source to the solvent is not limited. In one embodiment, a ratio of a mass of the metal source to a volume of the solvent can be 1 g:100 mL to 10 g:100 mL.

(13) The nitrogen-containing biomass can be at least one of bamboo, chitin, carboxymethyl chitin, chitosan, carboxymethyl chitosan, glucosamine hydrochloride, or a combination thereof. The nitrogen-containing biomass can include a nitrogen element and a carbon element as a nitrogen source and a carbon source, respectively. The nitrogen-containing biomass can be insoluble in the water.

(14) The metal source can react with a part of the pore-forming agent to form the metal precipitate. The metal precipitate can be formed by carbonate ions and metal ions. An excess part of the pore-forming agent can decompose during subsequent calcination to form a gas which plays a role of forming pore and results in the plurality of passages in the nitrogen-doped porous carbon material. In one embodiment, the mass ratio of the metal oxide to the nitrogen-containing biomass can be 0.05:1 to 2:1. In another embodiment, the mass ratio of the metal oxide to the nitrogen-containing biomass can be 0.5:1 to 2:1. There can be a continuous stirring for 0.1 hour to 10 hours during the reaction. The obtained mixture is actually a suspension, in which the metal precipitate formed and the nitrogen-containing biomass are insoluble in a solvent, but are evenly distributed in the mixture. So, the mixture is a suspension.

(15) It will be understood that the mixture can be dried before the first calcination step of S3, and a process of drying can be as following: drying at a temperature with a range of 60 degrees centigrade to 180 degrees centigrade.

(16) In step S3, the time of the first calcination can be in a range of 0.1 hour to 5 hours. In one embodiment, a process of the first calcination can be as follows: the temperature is raised to a range of 500 degrees centigrade to 1200 degrees centigrade at a heating rate of 2 degrees centigrade per minute to 30 degrees centigrade per minute, the mixture is calcined at the temperature of 500 degrees centigrade to 1200 degrees centigrade for 0.1 hour to 5 hours and finally naturally cooled to a room temperature. In another embodiment, the temperature of the first calcination can be from 600 degrees centigrade to 900 degrees centigrade.

(17) In step S4, the noble metal particles can be at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles, or a combination thereof. A loading amount (i.e., mass fraction) of the noble metal particles in the composite catalyst can be regulated, which is not limited. There can be two methods for forming the noble metal particles in the plurality of passages of the nitrogen-doped porous carbon composite material: one is a dipping method, and the other is a liquid phase reduction method.

(18) The dipping method can be as follows: immersing the nitrogen-doped porous carbon composite material in the noble metal precursor solution; and subsequently treating the nitrogen-doped porous carbon composite material by the second calcination and hydrogen reduction in order. Noble metal particles can be formed in the plurality of passages of the nitrogen-doped porous carbon composite. In the second calcination of one embodiment, the temperature can be in a range of 200 degrees centigrade to 500 degrees centigrade, the heating rate can be in a range of 1 degree centigrade per minute to 20 degrees centigrade per minute, and the time is in a range of 1 minute to 240 minutes. In the hydrogen reduction, the temperature is in a range of 150 degrees centigrade to 500 degrees centigrade, the heating rate is in a range of 1 degree centigrade per minute to 20 degrees centigrade per minute, the time is in a range of 1 minute to 360 minutes, and a flow rate of hydrogen gas is in a range of 20 milliliters per minute to 200 milliliters per minute. In another embodiment, in the second calcination, the temperature can be in a range of 300 degrees centigrade to 500 degrees centigrade, the heating rate can be in a range of 5 degrees centigrade per minute to 10 degrees centigrade per minute, and the time can be in a range of 60 minutes to 120 minutes; in the hydrogen reduction, the temperature can be in a range of 200 degrees centigrade to 400 degree centigrade, the heating rate can be in a range of 5 degrees centigrade per minute to 10 degrees centigrade per minute, the time can be in a range of 60 minutes to 180 minutes, and the flow rate of hydrogen gas can be in a range of 40 milliliters per minute to 100 milliliters per minute.

(19) The liquid phase reduction method can be as follows: immersing the nitrogen-doped porous carbon composite material in a noble metal precursor solution; and adding a reductant which reacts with a noble metal precursor of the noble metal precursor solution to obtain noble metal particles in the plurality of passages.

(20) The noble metal precursor in the Noble metal precursor solution can be at least one of PdCl.sub.2, H.sub.2PdCl.sub.4, Pd(NO.sub.3).sub.2, Pd(NH.sub.3).sub.4(NO.sub.3).sub.2, H.sub.2PtCl.sub.6.Math.6H.sub.2O, [Pt(NH.sub.3).sub.4](NO.sub.3).sub.2, Na.sub.2PtCl.sub.4.Math.xH.sub.2O, H.sub.8C.sub.14N.sub.2Pt, PtCl.sub.4, Pt(C.sub.5H.sub.7O.sub.2).sub.2, C.sub.10H.sub.14O.sub.4Pt, (NH.sub.4).sub.2RuCl.sub.6, RuCl.sub.3, C.sub.15H.sub.21O.sub.6Ru, H.sub.12Cl.sub.6N.sub.3Rh, RhN.sub.3O.sub.9, RhCl.sub.3.Math.3H.sub.2O, IrCl.sub.3, Na.sub.2IrCl.sub.6.Math.6H.sub.2O, H.sub.2IrCl.sub.6.Math.xH.sub.2O, [CH.sub.3COCHC(O)CH.sub.3].sub.3Ir, NaAuCl.sub.4.Math.2H.sub.2O, HAuCl.sub.4.Math.XH.sub.2O, or (NH.sub.4)AuCl.sub.4, or a combination thereof.

(21) The reductant can be at least one of NaBH.sub.4, HCOOH, hydrazine hydrate, or a combination thereof. And a molar ratio of the reductant to the noble metal precursor of the noble metal precursor solution can be in a range of 1:1 to 1000:1.

(22) The present disclosure further provides a composite catalyst including a carrier and noble metal particles supported by the carrier. The carrier can be a nitrogen-doped porous carbon composite material having a plurality of passages. Noble metal particles can be distributed in the plurality of passages. The nitrogen-doped porous carbon composite material can include a nitrogen-doped porous carbon material a plurality of metal oxide particles. The plurality of metal oxide particles can be uniformly distributed in the nitrogen-doped porous carbon material. The plurality of metal oxide particles can be partially exposed through the plurality of passages. Noble metal atoms can be tightly combined with oxide atoms of the exposed metal oxide particles to achieve recombination. The noble metal particles are at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles. The noble metal particles can have a dispersity of 75% to 95% in the nitrogen-doped porous carbon composite material.

(23) A weight percentage of the noble metal particles in the composite catalyst can be in a range of 0.1% to 10%. A weight percentage of the plurality of the metal oxide in the composite catalyst can be in a range of 2% to 30%. A weight percentage of the nitrogen-doped porous carbon composite material in the composite catalyst can be in a range of 60% to 97.9%. And a weight percentage of nitrogen element in the nitrogen-doped porous carbon composite material can be in a range of 0.5% to 15%.

(24) Referring to FIG. 5, the present disclosure also provides an application of the composite catalyst in a catalytic hydrogenation reaction. The composite catalyst can act as a catalyst in a selective hydrogenation reaction of an unsaturated ketone or a biotin precursor (X). And the unsaturated ketone is at least one of 6-methyl-5-hepten-2-one (I), 6,10-dimethyl-5-undecen-2-one (III), 6,10-dimethyl-5,9-undecenediene-2-one (V), 6,10,14-trimethyl-5-pentadecen-2-one (VI), 6,10,14-trimethyl-5,9-pentadecandien-2-one (VIII), 6,10,14-trimethyl-5,9,13-pentadecatrien-2-one (IX), or a combination thereof.

(25) The composite catalyst of the present disclosure and its application will be further described below by multiple embodiments.

Embodiment 1

(26) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(27) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 40 mL deionized water. Approximately 0.5 mL PdCl.sub.2 solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained. A theoretical loading amount (weight percentage) of Pd metal particles in the composite catalyst was 0.6%.

(28) An actual loading amount of Pd metal particles in the composite catalyst was about 0.59% measured by atomic emission spectroscopy, which was approximately consistent with the theoretical load amount of Pd metal particles in the composite catalyst.

(29) The nitrogen-doped porous carbon composite material was measured by a scanning electron microscopy, and the result was shown in FIG. 1. Referring to FIG. 1, a plurality of pores and passages can be clearly observed.

(30) The nitrogen-doped porous carbon composite was measured by a transmission electron microscopy, and the result was shown in FIG. 2. The composite catalyst was measured by a transmission electron microscopy, and the result was shown in FIG. 3. Comparing FIG. 2, the morphology of composite catalyst in FIG. 3 is substantially unchanged. It is difficult to see Pd metal particles in FIG. 3 because the size of Pd metal particles is very small and below 1 nm.

(31) The nitrogen-doped porous carbon composite and composite catalyst were measured by a X-ray photoelectron spectroscopy, and the result were shown in FIG. 4. Referring to FIG. 4, the curve a corresponding to nitrogen-doped porous carbon composite had no Pd diffraction characteristic peak. Compared with the standard card of Pd, the curve b corresponding to the compound catalyst was not obvious, which also confirmed the conclusion that Pd metal particles obtained in FIG. 3 were below 1 nm.

(32) Pd dispersion and specific surface area of the composite catalyst were measured by CO titration method, wherein CO titration method is a carbon monoxide adsorption test for measuring noble metal dispersion. The results were: the Pd dispersion of the composite catalyst was about 83%, and the specific surface area of the composite catalyst was about 135.3 m.sup.2 g.sup.1.

(33) For comparison, a comparative embodiment 1 was also provided. The method of the composite catalyst in the comparative embodiment 1 was substantially the same as that of the composite catalyst in embodiment 1, except that there was no carboxymethyl chitin, only Pd was supported by CeO.sub.2 to obtain a Pd/CeO.sub.2 catalyst having a specific surface area of only 5.6 m.sup.2 g.sup.1.

Embodiment 2

(34) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in about 30 mL water. After the indium nitrate hydrate was dissolved, about 3 g chitosan was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(35) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to about 40 mL deionized water. About 0.5 mL PdCl.sub.2 solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), composite catalyst was obtained.

(36) The method of the composite catalyst in embodiment 2 was substantially the same as that of the composite catalyst in embodiment 1, except that the nitrogen-containing biomass was the chitosan.

(37) Pd dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Pd dispersion of the composite catalyst was about 81%, and the specific surface area of the composite catalyst was about 147.3 m.sup.2 g.sup.1.

Embodiment 3

(38) Approximately 1 g zirconium nitrate pentahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(39) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 40 mL deionized water. Approximately 0.5 mL PdCl.sub.2 solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(40) Pd dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Pd dispersion of the composite catalyst was about 79%, and the specific surface area of the composite catalyst was about 126.8 m.sup.2 g.sup.1.

Embodiment 4

(41) Approximately 1 g aluminum nitrate nonahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(42) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 40 mL deionized water. Approximately 0.5 mL PdCl.sub.2 solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(43) Pd dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Pd dispersion of the composite catalyst was about 76%, and the specific surface area of the composite catalyst was about 115.5 m.sup.2 g.sup.1.

Embodiment 5

(44) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g chitosan was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(45) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 60 mL deionized water. Approximately 0.5 mL PdCl.sub.2 solution with a molar concentration of about 10 mg/mL was slowly added dropwise and sonicated at about 25 degrees centigrade for about 30 minutes. Approximately 10.7 mL NaBH.sub.4 solution with a molar concentration of about 2 mg/mL was then slowly added and continued to sonicate for about 30 minutes. After filtered, washed with deionized water to neutral and placed in an oven of about 70 degrees centigrade for about 24 h, a composite catalyst was obtained.

(46) Pd dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Pd dispersion of the composite catalyst was about 89%, and the specific surface area of the composite catalyst was about 138.7 m.sup.2 g.sup.1.

Embodiment 6

(47) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(48) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 40 mL deionized water. Approximately 0.8 mL H.sub.2PtCl.sub.6.Math.6H.sub.2O solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(49) Pt dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Pt dispersion of the composite catalyst was about 91%, and the specific surface area of the composite catalyst was about 133.5 m.sup.2 g.sup.1.

Embodiment 7

(50) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(51) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 60 mL deionized water. Approximately 0.7 mL RuCl.sub.3 solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(52) Ru dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Ru dispersion of the composite catalyst was about 82%, and the specific surface area of the composite catalyst was about 133.9 m.sup.2 g.sup.1.

Embodiment 8

(53) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(54) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 60 mL deionized water. Approximately 1.1 mL H.sub.12Cl.sub.6N.sub.3Rh solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(55) Rh dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Rh dispersion of the composite catalyst was about 83%, and the specific surface area of the composite catalyst was about 139.2 m.sup.2 g.sup.1.

Embodiment 9

(56) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(57) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 60 mL deionized water. Approximately 0.9 mL H.sub.2IrCl.sub.6.Math.xH.sub.2O solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(58) Ir dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: the Ir dispersion of the composite catalyst was about 81%, and the specific surface area of the composite catalyst was about 128.4 m.sup.2 g.sup.1.

Embodiment 10

(59) Approximately 1 g cerium nitrate hexahydrate was weighed and dispersed in approximately 30 mL water. After the cerium nitrate hexahydrate was dissolved, approximately 3 g carboxymethyl chitin was added and stirred for about 1 hour. Then approximately 3 g ammonium bicarbonate was slowly added and stirred for about 1 hour to obtain a mixture. Then the temperature rose to about 80 degrees centigrade while stirring until dry. Then, the mixture was transferred to a crucible and underwent a calcination process in a nitrogen furnace. The calcination process was as follows: heating to about 1000 degrees centigrade at a heating rate of about 5 degrees centigrade per minute, calcining at about 1000 degrees centigrade for about 1 hour; then, naturally cooling to room temperature. The mixture calcined was ground to obtain a nitrogen-doped porous carbon composite.

(60) Approximately 0.5 g nitrogen-doped porous carbon composite material was weighed and added to approximately 60 mL deionized water. Approximately 0.6 mL HAuCl.sub.4.Math.XH.sub.2O solution with a molar concentration of about 10 mg/mL was slowly added dropwise, stirred at about 50 degrees centigrade for about 12 h, and placed in an oven of about 70 degrees centigrade for about 24 h. It was further calcined at about 300 degrees centigrade for about 1 h in the air. Finally, after a hydrogen reduction at about 300 degrees centigrade for about 1 h (wherein, a flow rate of hydrogen gas was about 50 milliliters per minute, heating rate was about 5 degrees centigrade per minute), a composite catalyst was obtained.

(61) Au dispersion and specific surface area of the composite catalyst were measured by CO titration method. The results were: Au dispersion of the composite catalyst was about 88%, and the specific surface area of the composite catalyst was about 137.3 m.sup.2 g.sup.1.

(62) Referring to FIG. 5, the processes of the hydrogenation reaction in the following embodiments were showed.

Embodiment 11

(63) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(64) Approximately 50 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 15 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 99%. Further, a conversion and selectivity of the Pd/CeO.sub.2 catalyst of the comparative embodiment 1 were about 68% and about 99%, respectively. Thus, the highly dispersed composite catalyst in embodiment 1 has greatly improved the selectivity of the catalyst while maintaining the activity of the catalyst.

Embodiment 12

(65) The composite catalyst catalyzes a selective hydrogenation of 6,10-dimethyl-5-undecen-2-one (III) by following process.

(66) Approximately 50 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 15 mmol 6,10-dimethyl-5-undecen-2-one (III) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6,10-dimethyl-5-undecen-2-one (III) was about 100%, and a selectivity of 6,10-dimethyl-undecyl-2-one (IV) was about 99%.

Embodiment 13

(67) The composite catalyst catalyzes a selective hydrogenation of 6,10-dimethyl-5,9-undecenediene-2-one (V) by following process.

(68) Approximately 50 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. About 10 mmol 6,10-dimethyl-5,9-undecenediene-2-one (V) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of 2 MPa, a reaction temperature of 30 degrees centigrade and reaction time of 4 hours. A conversion of 6,10-dimethyl-5,9-undecenediene-2-one (V) was 100%, and a selectivity of 6,10-dimethyl-undecyl-2-one (IV) was 99%.

Embodiment 14

(69) The composite catalyst catalyzes a selective hydrogenation of 6,10,14-trimethyl-5-pentadecen-2-one (VI) by following process.

(70) Approximately 50 mg Composite catalyst obtained in Embodiment 1 was added to a 50 mL autoclave. Approximately 15 mmol 6,10,14-trimethyl-5-pentadecen-2-one (VI) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6,10,14-trimethyl-5-pentadecen-2-one (VI) was about 100%, and a selectivity of 6,10,14-trimethyl-pentadecan-2-one (VII) was about 99%.

Embodiment 15

(71) The composite catalyst catalyzes a selective hydrogenation of 6,10,14-trimethyl-5,9-pentadecandien-2-one (VIII) by following process.

(72) Approximately 50 mg Composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 10 mmol 6,10,14-trimethyl-5,9-pentadecandien-2-one (VIII) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6,10,14-trimethyl-5,9-pentadecandien-2-one (VIII) was about 100%, and a selectivity of 6,10,14-trimethyl-pentadecan-2-one (VII) was about 99%.

Embodiment 16

(73) The composite catalyst catalyzes a selective hydrogenation of 6,10,14-trimethyl-5,9,13-pentadecatrien-2-one (IX) by following process.

(74) Approximately 50 mg Composite catalyst obtained in Embodiment 1 was added to a 50 mL autoclave. Approximately 5 mmol 6,10,14-trimethyl-5,9,13-pentadecatrien-2-one (IX) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 3 hours. A conversion of 6,10,14-trimethyl-5,9,13-pentadecatrien-2-one (IX) was about 100%, and a selectivity of 6,10,14-trimethyl-pentadecan-2-one (VII) was about 98%.

Embodiment 17

(75) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(76) Approximately 50 mg composite catalyst obtained in embodiment 6 was added to a 50 mL autoclave. Approximately 4 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 40 degrees centigrade and reaction time of about 4 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 98%.

Embodiment 18

(77) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(78) Approximately 50 mg composite catalyst obtained in embodiment 7 was added to a 50 mL autoclave. Approximately 2 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 40 degrees centigrade and reaction time of about 5 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 97%.

Embodiment 19

(79) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(80) Approximately 50 mg composite catalyst obtained in embodiment 8 was added to a 50 mL autoclave. Approximately 15 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 99%.

Embodiment 20

(81) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(82) Approximately 50 mg composite catalyst obtained in embodiment 9 was added to a 50 mL autoclave. Approximately 15 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 99%.

Embodiment 21

(83) The composite catalyst catalyzes a selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(84) Approximately 50 mg composite catalyst obtained in embodiment 10 was added to a 50 mL autoclave. Approximately 2 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 50 degrees centigrade and reaction time of about 6 hours. A conversion of 6-methyl-5-hepten-2-one (I) was about 100%, and a selectivity of 6-methyl-2-heptanone (II) was about 97%.

Embodiment 22

(85) The composite catalyst catalyzes a selective hydrogenation of the biotin precursor (X) by following process.

(86) Approximately 200 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 2 mmol biotin precursor (X) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 40 degrees centigrade and reaction time of about 3 hours. A conversion of biotin precursor (X) was about 100%, and a selectivity of biotin (XI) was about 99%.

Embodiment 23

(87) The composite catalyst catalyzes a selective hydrogenation of the biotin precursor (X) by following process.

(88) Approximately 200 mg composite catalyst obtained in embodiment 6 was added to a 50 mL autoclave. Approximately 2 mmol biotin precursor (X) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 50 degrees centigrade and reaction time of about 3 hours. A conversion of biotin precursor (X) was about 100%, and a selectivity of biotin (XI) was about 99%.

Embodiment 24

(89) The composite catalyst catalyzes an application performance of the selective hydrogenation of 6-methyl-5-hepten-2-one (I) by following process.

(90) Approximately 50 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 15 mmol 6-methyl-5-hepten-2-one (I) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 30 degrees centigrade and reaction time of about 4 hours. After the reaction, the composite catalyst was taken out by centrifugation, washed three times with ethanol, and dried under vacuum at about 40 degrees centigrade. The composite catalyst was continued to catalyze the selective hydrogenation of 2-methyl-3-butyn-2-ol (I). The results of the application were shown in Table 1. The result was the performance of the composite catalyst was stable, and the activity and selectivity of the composite catalyst was maintained after about 60 times of application.

(91) TABLE-US-00001 TABLE 1 Conversion of one Selectivity of Raw of 6-methyl-5- 6-methyl-2- material hepten-2-one (I) heptanone Hydrogenation selectivity Times (%) (II) (%) selectivity (%) (%) 1 100 99 <1 <1 3 100 99 <1 <1 6 100 99 <1 <1 9 100 99 <1 <1 12 100 99 <1 <1 15 100 99 <1 <1 20 100 99 <1 <1 25 100 99 <1 <1 30 100 99 <1 <1 35 100 99 <1 <1 40 100 99 <1 <1 45 100 99 <1 <1 50 100 99 <1 <1 55 100 99 <1 <1 60 99 99 <1 <1

Embodiment 25

(92) The composite catalyst catalyzes an application performance of the selective hydrogenation of biotin precursor (X) by following process.

(93) Approximately 200 mg composite catalyst obtained in embodiment 1 was added to a 50 mL autoclave. Approximately 2 mmol biotin precursor (X) and about 5 mL ethanol were added. The reaction was taken under a hydrogen pressure of about 2 MPa, a reaction temperature of about 40 degrees centigrade and reaction time of about 3 hours. After the reaction, the composite catalyst was taken out by centrifugation, washed three times with ethanol, and dried under vacuum at about 40 degrees centigrade. The composite catalyst was continued to catalyze the selective hydrogenation of biotin precursor (X). The results of the application were shown in Table 2. The result was the performance of the composite catalyst was stable, and the activity and selectivity of the composite catalyst was maintained after about 35 times of application.

(94) TABLE-US-00002 TABLE 2 Conversion of one of biotin precursor Selectivity of Esterification product Times (X) (%) biotin (XI) (%) electivity (%) 1 100 99 <1 3 100 99 <1 6 100 99 <1 9 100 99 <1 12 100 99 <1 15 100 99 <1 20 100 99 <1 25 100 99 <1 30 99 99 <1 35 98 99 <1

(95) The technical features of the above-described embodiments may be combined in any combination. For the sake of brevity of description, all possible combinations of the technical features in the above embodiments are not described. However, as long as there is no contradiction between the combinations of these technical features, all should be considered as within the scope of this disclosure.

(96) The above-described embodiments are merely illustrative of several embodiments of the present disclosure, and the description thereof is relatively specific and detailed, but is not to be construed as limiting the scope of the disclosure. It should be noted that a number of variations and modifications may be made by those skilled in the art without departing from the spirit and scope of the disclosure. Therefore, the scope of the disclosure should be determined by the appended claims.