Catalyst composition for preparing O-phenylphenol and method for preparing O-phenylphenol with the catalyst composition

Abstract

A catalyst composition for preparing o-phenylphenol is provided. The catalyst composition includes a carrier; and a first active metal, a second active metal, and a catalytic promoter carried by the carrier. The first active metal is platinum, and the second active metal is selected from the first, second and third rows of transition metals of groups VIB and VIIIB. The present disclosure utilizes the carrier to carry the first active metal, the second active metal and the catalytic promoter so as to increase the selectivity of o-phenylphenol and the service life of a catalyst.

Claims

1. A catalyst composition for preparing o-phenylphenol, comprising: a carrier; and a first active metal, a second active metal and a catalytic promoter carried by the carrier, wherein the first active metal is platinum, the second active metal is selected from the group consisting of chromium, ruthenium, and nickel, and the catalytic promoter is selected from the group consisting of alkali metal sulfate, alkali metal carbonate, alkali metal nitrate and alkali metal hydroxide, and wherein a weight ratio of the second active metal to the first active metal is between 0.03 and 0.38.

2. The catalyst composition for preparing o-phenylphenol according to claim 1, wherein a weight ratio of the first active metal to the carrier is between 0.004 and 0.006.

3. The catalyst composition for preparing o-phenylphenol according to claim 1, wherein a weight ratio of the second active metal to the carrier is between 0.0002 and 0.0015.

4. The catalyst composition for preparing o-phenylphenol according to claim 3, wherein the weight ratio of the second active metal to the carrier is between 0.0005 and 0.0012.

5. The catalyst composition for preparing o-phenylphenol according to claim 1, wherein the catalytic promoter is at least one selected from the group consisting of potassium sulfate and potassium carbonate.

6. The catalyst composition for preparing o-phenylphenol according to claim 1, wherein a weight ratio of the catalytic promoter to the carrier is between 0.02 and 0.15.

7. The catalyst composition for preparing o-phenylphenol according to claim 1, wherein the carrier is at least one selected from the group consisting of SiO.sub.2, Al.sub.2O.sub.3, and Zr.sub.2O.sub.3.

8. A method for preparing o-phenylphenol, comprising: performing a dehydrogenation reaction of a cyclohexanone dimer in the presence of the catalyst composition according to claim 1.

9. The method for preparing o-phenylphenol according to claim 8, wherein the weight hourly space velocity (WHSV) of the cyclohexanone dimer in the dehydrogenation reaction is between 0.2 and 2.0.

10. The method for preparing o-phenylphenol according to claim 8, wherein a weight ratio of the first active metal to the carrier is between 0.004 and 0.006.

11. The method for preparing o-phenylphenol according to claim 8, wherein a weight ratio of the second active metal to the carrier is between 0.0002 and 0.0015.

12. The method for preparing o-phenylphenol according to claim 8, wherein the metal salt is at least one selected from the group consisting of potassium sulfate and potassium carbonate.

13. The method for preparing o-phenylphenol according to claim 8, wherein the metal hydroxide is an alkali metal hydroxide.

14. The method for preparing o-phenylphenol according to claim 8, wherein a weight ratio of the catalytic promoter to the carrier is between 0.02 and 0.15.

15. The method for preparing o-phenylphenol according to claim 8, wherein the carrier is at least one selected from the group consisting of SiO.sub.2, Al.sub.2O.sub.3, and Zr.sub.2O.sub.3.

Description

DETAILED DESCRIPTION

(1) The detailed description of the present disclosure is illustrated by the following specific examples. Persons skilled in the art can conceive the other advantages and effects of the present disclosure, based on the disclosure contained in the present specification. The present disclosure can also be implemented or applied by different embodiments. Each of the details in the present specification can be modified and altered in various ways, based on different perspectives and applications, without departing from the spirit of the disclosure of the present disclosure.

(2) As used herein, the expression first, second and third rows in groups VIB and VIIIB refers to the first row, second row transition, and third row in groups VIB and VIIIB in the periodic table.

(3) The conversion rate and selectivity described herein are calculated by the following formulas:
Conversion rate (%)={[addition amount of a cyclohexanone dimer (mol)residual amount of the cyclohexanone dimer after reaction (mol)]/addition amount of cyclohexanone dimer (mol)}100%;
Selectivity (%)={amount of OPP in a product (mol)/[addition amount of the cyclohexanone dimer (mol)residual amount of the cyclohexanone dimer after reaction (mol)]}100%; and
Reaction initiation=6 hours after the reaction starts.

(4) In addition, the weight ratio of the first active metal:the second active metal:the carrier:the catalytic promoter in the catalyst composition is measured by Varian 220FS Atomic absorption spectrometer, AAS), wherein the loading rate of the first active metal, the second active metal, and the catalytic promoter on the carrier are all greater than 92%.

(5) The present disclosure provides a catalyst composition for preparing OPP from a cyclohexanone dimer, and the catalyst composition includes a carrier; and a first active metal, a second active metal, and a promoter selected from a metal salt and a metal hydroxide carried by the carrier.

(6) In addition, for preparing the catalyst composition, platinum is used as the first active metal, a metal selected from the first, second and third rows of transition metals of groups VIB and VIIIB is used as the second active metal. The first active metal and the second active metal are carried by the carrier, such as, SiO.sub.2, Al.sub.2O.sub.3 and Zr.sub.2O.sub.3. Subsequently, in a solution environment, the catalyst promoter selected from a metal salt and a metal hydroxide is carried by the carrier, such that the catalyst composition is represented by the following formula (II):
[Pt+M+catalytic promoter]/-Al.sub.2O.sub.3(II)
wherein M is selected from the first, second and third rows of transition metals of groups VIB and VIIIB

(7) In one embodiment, platinum and the transition metals of groups VIB and VIIIB are carried by -aluminum oxide. After the -aluminum oxide is subjected to dehydration and calcination, in a solution environment, the catalytic promoter selected from a metal salt and a metal hydroxide is carried by the carrier. The obtained catalyst can be used for preparing OPP.

(8) In the catalyst composition of the present disclosure, the weight ratio of platinum as the first active metal to the carrier is between 0.004 and 0.006. The weight ratio of the second active metal selected from the first, second and third rows of transition metals of groups VIB and VIIIB to the carrier is between 0.0002 and 0.0015, preferably between 0.0005 and 0.0012. The weight ratio of the catalytic promoter to the carrier is between 0.02 and 0.15, preferably between 0.05 and 0.10.

(9) The present disclosure further provides a method for preparing OPP, including: performing a dehydrogenation reaction of a cyclohexanone dimer in the presence of the catalyst composition of the present disclosure.

(10) In one embodiment of the method for preparing OPP of the present disclosure, the weight ratio of the second active metal to the first active metal is between 0.03 and 0.38. In another embodiment, the weight ratio of the second active metal to the first active metal is between 0.08 and 0.3.

(11) In one embodiment of the method for preparing OPP of the present disclosure, the weight ratio of the first active metal to the carrier is between 0.004 and 0.006.

(12) In the above embodiments, the weight ratio of the second active metal to the carrier is between 0.0002 and 0.0015. In another embodiment, the weight ratio of the second active metal to the carrier is between 0.0005 and 0.0012.

(13) In one embodiment of the method for preparing OPP of the present disclosure, the second active metal is selected from the group consisting of chromium, ruthenium, iridium and nickel.

(14) In one embodiment of the method for preparing OPP of the present disclosure, the metal salt is alkali metal sulfate, alkali metal carbonate, or alkali metal nitrate. The examples of the catalytic promoter can be selected from at least one from the group consisting of potassium sulfate, potassium carbonate, and sodium nitrate.

(15) In one embodiment of the method for preparing OPP of the present disclosure, the metal hydroxide is an alkali metal hydroxide. The examples of the catalytic promoter can be potassium hydroxide.

(16) In one embodiment of the method for preparing OPP of the present disclosure, the weight ratio of the catalytic promoter to the carrier is between 0.02 and 0.15.

(17) In one embodiment of the method for preparing OPP of the present disclosure, the carrier is selected from at least one from the group consisting of SiO.sub.2, Al.sub.2O.sub.3, and Zr.sub.2O.sub.3.

(18) In one embodiment of the method for preparing OPP of the present disclosure, the WHSV in the dehydrogenation reaction is between 0.2 and 2.0.

Preparation Example 1: Preparation of a Catalyst Composition of the Present Disclosure

(19) 1.335 g of hexachloroplatinic acid and 0.619 g of chromium (III) nitrate nonahydrate were dissolved in 300 g of deionized water. 100 g of -aluminum oxide calcinated for 3 hours at 250 C. was added into the above solution of metal salts. The solution was impregnated until dried out by ultrasonication at 70 C., oven-dried, and dehydrated. After then, the solution was calcinated for 5 hours at 450 C. in the presence of nitrogen gas at a flow rate of 30 standard-state cubic centimeter per minute (sccm), followed by a reduction reaction for 5 hours at 360 C. in the presence of nitrogen gas at a flow rate of 30 sccm, and hydrogen gas at a flow rate of 10 sccm, A catalyst without a supported catalytic promoter was obtained.

(20) 6.316 g of potassium sulfate was dissolved in 300 g of deionized water, and then the reduced catalyst was added into the aqueous solution of potassium sulfate. The solution was impregnated until dried out by ultrasonication at 70 C., oven-dried, and dehydrated. The catalyst composition of Preparation Example 1 was obtained, wherein the weight ratio of first active metal:second active metal:carrier:catalytic promoter was 0.5:0.08:100:6.

Preparation Examples 2 to 4: Preparation of Catalyst Compositions of the Present Disclosure by Using Different Second Active Metals

(21) These catalyst compositions were prepared in the same manner as in Preparation Example 1, except that 0.619 g of chromium (III) nitrate nonahydrate in Preparation Example 1 was replaced by 0.208 g of ruthenium (III) chloride trihydrate, 0.153 g of iridium (III) chloride hydrate, and 0.326 g of nickel (II) chloride hexahydrate in Preparation Examples 2 to 4, respectively. The weight ratio of first active metal:second active metal:carrier:catalytic promoter in Preparation Examples 2 to 4 was 0.5:0.08:100:6.

Preparation Examples 5 to 8: Preparation of Catalyst Compositions of the Present Disclosure by Using Second Active Metals in Different Amounts

(22) These catalyst compositions were prepared in the same manner as in Preparation Example 1, except that the addition amounts of chromium (III) nitrate nonahydrate in Preparation Examples 5 to 8 were 0.155 g, 0.388 g, 0.930 g and 1.161 g, respectively. Accordingly, the weight ratios of first active metal:second active metal:carrier:catalytic promoter in the catalyst compositions of Preparation Examples 5 to 8 became 0.5:0.02:100:6, 0.5:0.05:100:6, 0.5:0.12:100:6, 0.5:0.15:100:6, respectively.

Preparation Examples 9 to 11: Preparation of Catalyst Compositions of the Present Disclosure by Using Different Catalytic Promoters

(23) These catalyst compositions were prepared in the same manner as in Preparation Example 1, except that potassium sulfate in Preparation Example 1 was replaced by potassium carbonate, potassium hydroxide, and sodium nitrate in Preparation Examples 9 to 11, respectively. In Preparation Examples 9 to 11, the weight ratio of first active metal:second active metal:carrier:catalytic promoter was 0.5:0.08:100:6.

Preparation Examples 12 to 15: Preparation of Catalyst Compositions of the Present Disclosure by Using Catalytic Promoters in Different Amounts

(24) These catalyst compositions were prepared in the same manner as in Preparation Example 1, except that the addition amount (6.316 g) of potassium sulfate in Preparation Example 1 was adjusted to 2.105 g, 8.421 g, 11.579 g and 15.789 g in Preparation Examples 12 to 15, respectively. Accordingly, the weight ratios of first active metal:second active metal:carrier:catalytic promoter in the catalyst compositions of Preparation Examples 12 to 15 became 0.5:0.08:100:2, 0.5:0.08:100:8, 0.5:0.08:100:11, 0.5:0.08:100:15, respectively.

Comparative Example 1: Preparation of a Catalyst Composition without Using a Second Active Metal and Preparation of OPP

(25) 1.335 g of hexachloroplatinic acid was dissolved in 300 g of deionized water, and then 100 g of -aluminum oxide calcinated for 3 hours at 250 C. was added into the above solution of metal salts. The solution was impregnated until dried out by ultrasonication at 70 C., oven-dried, and dehydrated. After then, the solution was calcinated for 5 hours at 450 C. in the presence of nitrogen gas at a flow rate of 30 sccm, followed by a reduction reaction for 5 hours at 360 C. in the presence of nitrogen gas at a flow rate of 30 sccm, and hydrogen gas at a flow rate of 10 sccm. Subsequently, 6.316 g of potassium sulfate was dissolved in 300 g of deionized water, and then the reduced catalyst was added into the solution. The solution was then impregnated until dried out by ultrasonication at 70 C., oven-dried, and dehydrated.

(26) 20 g of the obtained catalyst composition was filled in a fixed-bed reactor. The reaction was carried out in a continuous mode. A cyclohexanone dimer was fed into the reactor at a flow rate of 0.33 sccm, and hydrogen gas was also fed into the reactor as a carrier gas. The dehydrogenation reaction of the cyclohexanone dimer was performed at a vaporization temperature of 240 C., a reaction temperature of 360 C., and a reaction pressure of 1 atm. The product was collected after the reaction was performed for 6 hours, and it was analyzed by Shimadzu GC-2010 Plus gas chromatography. The result of the analysis is reported in Table 1.

Examples 1 to 15: Methods for Preparing OPP of the Present Disclosure

(27) 20 g of the catalyst compositions prepared from Preparation Examples 1 to 15 were filled in a fixed-bed reactor, respectively. The reaction was carried out in the continuous mode. A cyclohexanone dimer was fed into the reactor at a flow rate of 0.33 sccm, and hydrogen gas was also fed into the reactor as a carrier gas. The dehydrogenation reaction of cyclohexanone dimer was performed at a vaporization temperature of 240 C., a reaction temperature of 360 C., and a reaction pressure of 1 atm. The products were collected after the reaction was performed for 6 hours, and they were analyzed by Shimadzu GC-2010 Plus gas chromatography. The results of the analysis are reported in Tables 1 to 4.

(28) TABLE-US-00001 TABLE 1 Catalyst Second Conversion Selectivity composition active metal rate (%) (%) Comparative 99.98 87.45 Example 1 Example 1 Preparation chromium 100.00 92.44 Example 1 Example 2 Preparation ruthenium 100.00 91.48 Example 2 Example 3 Preparation iridium 100.00 90.13 Example 3 Example 4 Preparation nickel 100.00 91.06 Example 4

(29) Referring to Table 1, as compared with the catalyst of Comparative Example 1, the catalyst composition of the present disclosure had an excellent property of the conversion rate of the cyclohexanone dimer being 100% after 6 hours of reaction, due to that the carrier in the catalyst composition of the present disclosure carried the first and second active metals. Further, the catalyst composition of the present disclosure resulted in a selectivity greater than 90% under the condition of a conversion rate of 100%.

(30) TABLE-US-00002 TABLE 2 Weight ratio of second active Catalyst metal in catalyst Conversion Selectivity composition composition rate (%) (%) Example 5 Preparation 0.02 100.00 88.23 Example 5 Example 6 Preparation 0.05 100.00 89.25 Example 6 Example 1 Preparation 0.08 100.00 92.44 Example 1 Example 7 Preparation 0.12 100.00 89.31 Example 7 Example 8 Preparation 0.15 100.00 93.74 Example 8

(31) In the catalyst compositions from Preparation Examples 1, 5 to 8, the weight ratio of first active metal:carrier:catalytic promoter was fixed at 0.5:100:6, and the amount of second active metal was changed. The weight ratios of the second active metal in each Preparation Example are shown in Table 2.

(32) Referring to Table 2, as compared with Comparative Example 1 (see Table 1), when the weight ratio of the second active metal to the carrier in the catalyst composition of the present disclosure was between 0.0002 and 0.0015, not only that the conversion rate of the reactant was not be decreased, but also that the selectivity of the product could be maintained under the condition of a conversion rate of the reactant of 100%.

Comparative Example 2: Preparation of a Catalyst Composition without a Catalytic Promoter

(33) 1.335 g of hexachloroplatinic acid and 0.619 g of chromium (III) nitrate nonahydrate were dissolved in 300 g of deionized water. 100 g of -aluminum oxide calcinated for 3 hours at 250 C. was added into the above solution of metal salts. the solution was then impregnated until dried out by ultrasonication at 70 C., oven-dried, and dehydrated. After then, the catalyst was calcinated for 5 hours at 450 C. in the presence of nitrogen gas at a flow rate of 30 sccm, followed by a reduction reaction for 5 hours at 360 C. in the presence of nitrogen gas at a flow rate of 30 sccm and hydrogen gas at a flow rate of 10 sccm.

(34) 20 g of the obtained catalyst composition was filled in a fixed-bed reactor. The reaction was carried out in a continuous mode. A cyclohexanone dimer was fed into the reactor at a flow rate of 0.33 sccm, and hydrogen gas was also fed into the reactor as a carrier gas. The dehydrogenation reaction of cyclohexanone dimer was performed at a vaporization temperature of 240 C., a reaction temperature of 360 C., and a reaction pressure of 1 atm. The product was collected after the reaction was performed for 6 hours, and analyzed by Shimadzu GC-2010 Plus gas chromatography. The result of the analysis is reported in Table 3.

(35) TABLE-US-00003 TABLE 3 Catalyst Catalytic Conversion Selectivity composition Promoter rate (%) (%) Comparative 100.00 71.26 Example 2 Example 1 Preparation K.sub.2SO.sub.4 100.00 92.44 Example 1 Example 9 Preparation K.sub.2CO.sub.3 100.00 85.60 Example 9 Example 10 Preparation KOH 100.00 84.72 Example 10 Example 11 Preparation NaNO.sub.3 99.97 80.12 Example 11

(36) In the catalyst compositions from Preparation Examples 1, 9 to 11, the weight ratio of first active metal:carrier:catalytic promoter was fixed at 0.5:0.08:100:6, and the amount of catalytic promoter was changed. The catalytic promoters in each of the Preparation Examples are shown in Table 3.

(37) Referring to Table 3, the selectivity of the catalyst composition of Comparative Example 2 without a catalytic promoter was already lower than 80% within 6 hours of reaction time, i.e., reaction initiation. Unlike Comparative Example 2, all of the catalyst compositions from each of the Examples of the present disclosure (in which the different catalytic promoters) were used have a conversion rate of the reactant of greater than 99.97%, and their catalytic activities are maintained.

(38) In addition, from Table 3, it can be seen that, as compared with Examples 10 and 11, when the catalytic promoter is alkali metal sulfate or alkali metal carbonate (for example, Examples 1 and 9), the catalyst composition of the present disclosure achieves a selectivity of the product of greater than 85.5% under the condition of a conversion rate of the product of 100%.

(39) TABLE-US-00004 TABLE 4 Weight ratio of catalytic promoter Catalyst in catalyst Conversion Selectivity composition composition rate (%) (%) Example 12 Preparation 2 100.00 81.17 Example 12 Example 1 Preparation 6 100.00 92.44 Example 1 Example 13 Preparation 8 100.00 94.09 Example 13 Example 14 Preparation 11 100.00 89.97 Example 14 Example 15 Preparation 15 100.00 89.99 Example 15

(40) In the catalyst compositions from Preparation Examples 1, 12 to 15, the weight ratio of first active metal:second active metal:carrier was fixed at 0.5:0.08:100, and the weight ratios of catalytic promoter were changed to be 2, 6, 8, 11 and 15, respectively. The catalytic promoters in each of the Preparation Examples are shown in Table 4.

(41) As shown in Table 4, as compared with Comparative Example 2 (see Table 3), when the weight ratio of the catalytic promoter to the carrier in the catalyst composition of the present disclosure was between 0.02 to 0.15, the conversion rate of the reactant was not be decreased, and the selectivity of the product could be maintained under the condition of a conversion degree of the reactant of 100%.

Examples 16 to 20: Methods for Preparing OPP of the Present Disclosure

(42) 20 g of the catalyst composition prepared from Preparation Example 1 was filled in a fixed-bed reactor. The reaction was carried out in the continuous mode. A cyclohexanone dimer was fed into the reactor at a flow rate of 0.33 sccm, and a hydrogen was also fed into the reactor as a carrier gas. The dehydrogenation reaction of cyclohexanone dimer was performed at a vaporization temperature of 240 C., a reaction pressure of 1 atm, and different reaction temperatures. The reaction temperatures in each of the Examples are shown in Table 5. The products were collected after the reaction was performed for 6 hours, and analyzed by Shimadzu GC-2010 Plus gas chromatography. The results of the analysis are reported in Table 5.

(43) TABLE-US-00005 TABLE 5 Reaction Conversion Selectivity temperature ( C.) rate (%) (%) Example 16 330 100.00 92.16 Example 17 345 100.00 91.25 Example 1 360 100.00 91.89 Example 18 370 100.00 91.58 Example 19 380 100.00 92.00 Example 20 400 100.00 91.34

(44) As shown in Table 5, when OPP was prepared by using the catalyst composition of the present disclosure, the suitable reaction temperature was 330 to 400 C., and high selectivity as well as a high conversion rate could be obtained. Also, within a broader range of reaction temperatures, the method of the present disclosure could result in a high conversion rate of the reactant. Meanwhile, the selectivity of the product could be maintained under the condition of a conversion degree of the reactant of 100%, and the excellent catalytic activity could be maintained under the conditions of different reaction temperatures.

(45) It can be seen that, in the method for preparing OPP of the present disclosure, the range of reaction temperature in the dehydrogenation reaction of cyclohexanone dimer was between 330 and 400 C.

Examples 21 to 27: Methods for Preparing OPP of the Present Disclosure

(46) 20 g of the catalyst composition prepared from Preparation Example 1 was filled in a fixed-bed reactor. The reaction was carried out in the continuous mode. A cyclohexanone dimer was fed into the reactor with different flow rates by standard-state cubic centimeter per minute (sccm), and hydrogen gas was also fed into the reactor as a carrier gas. The dehydrogenation reaction of cyclohexanone dimer was performed at a vaporization temperature of 240 C., a reaction temperature of 360 C., and a reaction pressure of 1 atm. More specifically, the flow rates in Examples 21 to 27 were 0.10 sccm, 0.20 sccm, 0.26 sccm, 0.40 sccm, 0.46 sccm, 0.56 sccm, and 0.66 sccm, respectively; and they can be converted into weight hourly space velocities (Weight Hourly Space Velocity, WHSV) of 0.3 h.sup.1, 0.6 h.sup.1, 0.8 h.sup.1, 1.2 h.sup.1, 1.4 h.sup.1, 1.7 h.sup.1, and 2.0 h.sup.1, respectively. The flow rates for feeding the cyclohexanone dimer in each of Examples are reported in Table 6. The products were collected after the reaction was performed for 6 hours, and they were analyzed by Shimadzu GC-2010 Plus gas chromatography. The results of the analysis are reported in Table 6.

(47) TABLE-US-00006 TABLE 6 WHSV Conversion Selectivity (h.sup.1) rate (%) (%) Example 21 0.3 100.00 93.87 Example 22 0.6 100.00 93.69 Example 23 0.8 100.00 93.82 Example 1 1.0 100.00 91.89 Example 24 1.2 100.00 89.65 Example 25 1.4 100.00 86.25 Example 26 1.7 100.00 86.66 Example 27 2.0 99.99 82.24

(48) As shown in Table 6, when OPP is prepared by using the catalyst composition of the present disclosure, the suitable range of WHSVs was broader, such that high conversion rates are obtained for all of the reactions. Further, the selectivity of the product could be maintained under the condition of 99.99% of the conversion rate of the reactant. Also, the excellent catalytic activity of the catalyst composition of the present disclosure could be maintained under the condition of a broad range of WHSVs of the reactant.

(49) In the method for preparing OPP of the present disclosure, the WHSV in the dehydrogenation reaction was between 0.3 and 2.0, and preferably between 0.3 and 1.4.

(50) Moreover, in Example 21, by collecting the product and analyzing it with gas chromatography after a continuous reaction for 2400 hours, it is found that the conversion rate of the cyclohexanone dimer was still maintained at 100%. Further, the selectivity of OPP was 90.69%, under the condition of a conversion degree of the cyclohexanone dimer of 100%.

(51) It can be seen that, after 2400 hours of reaction, the catalyst composition of the present disclosure resulted in a conversion rate maintained at 100%, and a selectivity of greater than 90%. Also, the catalytic activity was still high after 2400 hours of reaction.

(52) From the above, as compared with the drawbacks in the prior art, the catalyst composition of the present disclosure employs a carrier that carries platinum, a metal selected from the first, second and third rows of transition metals of groups VIB and VIIIB, and a catalytic promoter at the same time, so as to effectively increase the dispersity of the active metal platinum on the catalyst and maintain a high conversion rate for a long time, and thereby increasing the catalytic activity.

(53) Furthermore, by using a combination of the first active metal, the second active metal and the catalytic promoter with the specific amounts, and adjusting the amount of the catalytic promoter, the catalyst composition of the present disclosure can effectively decrease the acidity of the catalyst. When a dehydrogenation reaction is performed by using the catalyst composition of the present disclosure, the service life of the catalyst can be effectively and significantly increased, such that the catalyst composition of the present disclosure has a certain level of stability, and thereby being useful for industrial production.

(54) Moreover, the method for preparing OPP of the present disclosure results in a broader range of the weight ratios of the reactant to the catalyst, such that it can be suitably applied in different fixed-bed reactors or different processing conditions. Thus, the method of the present disclosure exhibits a broad range of industrial applications.

(55) The features and functions of the present disclosure have been elucidated in the foregoing detailed descriptions. Those skilled in the art will appreciate that modifications and variations according to the spirit and principle of the present disclosure may be made. All such modifications and variations are considered to fall within the spirit and scope of the present disclosure as defined by the appended claims.