A catalyst carrier for dehydrogenation and its preparation method and application
By using alumina droplets with special preparation process as catalyst support in the dehydrogenation reaction, the problem of poor cocatalytic effect in the prior art is solved, the selectivity and yield of propylene is significantly improved, and high aromatic yields are also shown in the reforming reaction.
Patent Information
- Application Number
- CN202510010083.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-01-03
- Publication Date
- 2025-04-04
AI Technical Summary
The catalyst support used in the existing dehydrogenation reaction has a low cocatalytic effect, which affects the yield of the product.
A catalyst carrier for dehydrogenation is used, and its raw material includes alumina drip balls. Through a specific preparation method, it includes mixing aluminum powder with a nitric acid solution and adding a pore-forming agent and a capacity-expanding agent to form an aluminum sol, and after treatment through SnCl4 solution, it is drip balls through an oily ammonia column, dried and calcined to obtain alumina drip balls. At the same time, the mass ratio of SnCl4 in the SnCl4 solution to aluminum powder was defined to be 4.63:600, and the cocatalytic effect of the catalyst support was further improved through step-by-step drying and two-step roasting processes.
The cocatalytic effect of the catalyst support is significantly improved, the selectivity and yield of propylene is improved, and high aromatic yields are also shown in the reforming reaction.
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Figure CN119746838A_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the technical field of catalyst carriers, and in particular to a catalyst carrier for dehydrogenation and a preparation method and application thereof. Background Art
[0002] In chemical reactions, especially organic chemical reactions, catalysts often play a very important role. In order to improve the activity and stability of the catalyst, the catalyst is usually loaded on a carrier material. On the one hand, the catalyst carrier can support and disperse the active components, transfer mass, conduct electricity and heat, and on the other hand, the catalyst carrier also has a catalytic effect.
[0003] Catalyst carriers can be divided into carbon carriers and non-carbon carriers. Non-carbon carriers include oxides, carbides, and nitrides. Among them, oxides, especially alumina, are the most commonly used catalyst carriers because alumina not only has a high melting point but also has a transition phase in a wide temperature range.
[0004] Dehydrogenation reactions can produce many compounds, such as the dehydrogenation of propane to produce propylene. In most cases, in order to promote the reaction, the catalyst for the dehydrogenation reaction needs to be supported on an alumina carrier, but the catalytic effect of the existing catalyst carriers for dehydrogenation reactions is generally low, thus affecting the yield of the product. Summary of the invention
[0005] The present invention provides a catalyst carrier for dehydrogenation, a preparation method and application thereof, which solves the problem of poor catalytic effect of the catalyst carrier used for dehydrogenation reaction in the related art.
[0006] The technical solution of the present invention is as follows: A catalyst carrier for dehydrogenation, the raw material includes alumina drop balls, and the preparation method of the alumina drop balls includes the following steps: S1, after mixing aluminum powder and nitric acid solution, adding pore-forming agent and continuing to mix to obtain aluminum sol; S2, after mixing the aluminum sol and the expansion agent, adding SnCl4 solution and continuing to mix to obtain a mixed solution; S3, passing the mixed solution through an oil-ammonia column, separating the spheres, drying, and calcining to obtain alumina spheres.
[0007] As a further technical solution, the mass ratio of SnCl4 in the SnCl4 solution to the aluminum powder is 0.005~0.01:1.
[0008] As a further technical solution, the mass ratio of SnCl4 in the SnCl4 solution to the aluminum powder is 4.63:600.
[0009] The present invention limits the mass ratio of SnCl4 to aluminum powder in the SnCl4 solution to 4.63:600, thereby further improving the catalytic effect of the catalyst carrier.
[0010] As a further technical solution, the nitric acid solution consists of concentrated nitric acid and deionized water in a mass ratio of 1 to 1.5:5.
[0011] As a further technical solution, the mass concentration of the concentrated nitric acid is 98%.
[0012] As a further technical solution, the dosage of the aluminum powder and the nitric acid solution is calculated according to a mass ratio of concentrated nitric acid to aluminum powder of 0.05 to 0.075:1.
[0013] As a further technical solution, the mass ratio of the pore former to the aluminum powder is 0.3~0.4:1.
[0014] As a further technical solution, the mass ratio of the expansion agent to the aluminum powder is 0.05~0.1:1.
[0015] As a further technical solution, before passing through the oil-ammonia column, the mixed liquid is transferred to a syringe.
[0016] As a further technical solution, when passing through the oil-ammonia column, the distance between the needle outlet of the syringe and the hydrocarbon oil surface is 2-5 cm.
[0017] As a further technical solution, the height of the ammonia water in the oil-ammonia column is 1-6 m, and the height of the oil is 1-20 mm.
[0018] As a further technical solution, the oil includes one or more of solvent oil, white oil, and base oil.
[0019] As a further technical solution, the mass concentration of the ammonia water is 9%~11%.
[0020] As a further technical solution, the drying is specifically: first drying at 60-70°C for 3-4 hours, and then drying at 90-100°C for 3-4 hours.
[0021] The present invention adopts step-by-step drying, by first drying at 60-70° C. and then drying at 90-100° C., thereby further improving the catalytic effect of the catalyst carrier.
[0022] As a further technical solution, the calcination is specifically as follows: first calcining at 300-350°C for 2-3 hours, and then calcining at 650-700°C for 4.5-5 hours.
[0023] The present invention adopts a two-step calcination process, wherein the product is first calcined at 300-350° C. and then calcined at 650-700° C., thereby further improving the catalytic effect of the catalyst carrier.
[0024] As a further technical solution, the pore-forming agent includes one or more of starch, dextrin, and starch derivatives.
[0025] As a further technical solution, the starch derivative includes one or both of acid-modified starch and oxidized starch.
[0026] As a further technical solution, the expander is alcohol.
[0027] As a further technical solution, the alcohol includes one or more of ethanol, ethylene glycol, propylene glycol, isobutanol, and isopentanol.
[0028] As a further technical solution, the raw material also includes a monoisocyanate compound, and the mass ratio of the alumina drop ball to the monoisocyanate compound is 50:0.05~0.5.
[0029] The present invention uses a monoisocyanate compound and an alumina ball in combination. Since the monoisocyanate compound can react with the acidic group of the alumina ball, the acidity of the alumina ball is reduced. Although the monoisocyanate compound on the surface is decomposed by high temperature during the process of preparing the catalyst carrier into a catalyst, the acidic group of the alumina ball has been removed by the monoisocyanate compound during the process of preparing the catalyst carrier. After high temperature, the acidic group of the alumina ball will disappear, so that the acidity of the alumina ball is weakened, so that the prepared catalyst carrier can promote the reaction activity and selectivity of the catalyst to propane dehydrogenation to propylene, and further improve the catalyst carrier's catalytic effect.
[0030] The inventors found in experiments that when the monoisocyanate compound is replaced by a compound containing two or more isocyanate groups, the catalytic effect of the prepared catalyst carrier is relatively poor. Since it contains more active isocyanate groups, the propylene selectivity and propylene yield after application are similar to the results of Comparative Example 1.
[0031] As a further technical solution, the monoisocyanate compound may be any compound containing one isocyanate group, for example, it may be one or both of 2,5-dimethoxyphenyl isocyanate and 4-benzyloxyphenyl isocyanate.
[0032] As a further technical solution, the mass ratio of the alumina drop ball to the monoisocyanate compound is 50:0.1~0.3.
[0033] The present invention limits the mass ratio of the alumina drop ball to the monoisocyanate compound to 50:0.1-0.3, thereby further improving the catalytic effect of the catalyst carrier.
[0034] The present invention also proposes a method for preparing a catalyst carrier for dehydrogenation, comprising the following steps: dispersing aluminum oxide droplets evenly in a solvent, adding a monoisocyanate compound and mixing evenly, filtering, washing, and drying to obtain a catalyst carrier.
[0035] As a further technical solution, the solvent is dimethyl sulfoxide.
[0036] The present invention also proposes the use of the dehydrogenation catalyst carrier or the dehydrogenation catalyst carrier prepared by the preparation method in a dehydrogenation reaction or a reforming reaction.
[0037] The working principle and beneficial effects of the present invention are: The present invention provides a catalyst carrier for dehydrogenation, wherein the apparent bulk density ABD is 0.56±0.02 g / cc, the compressive strength (average value) is 40 N as measured by the method in HG / T 2783-2020, the particle diameter (average value) is 1.73 mm, the circularity is ≥0.96, and the specific surface area is 190-220 m 2 / g, and has a better catalytic promoter effect than the existing catalyst carrier for dehydrogenation reaction. When applied to propane dehydrogenation reaction, propylene selectivity and propylene yield can be significantly improved. In addition, the catalyst carrier provided by the present invention can also be used for reforming reaction. Compared with the existing catalyst carrier for reforming, it has a better catalytic promoter effect and can significantly improve the yield of aromatics when applied to reforming reaction. BRIEF DESCRIPTION OF THE DRAWINGS
[0038] The present invention will be further described in detail below in conjunction with the accompanying drawings and specific embodiments.
[0039] Figure 1 This is a photo of the catalyst support prepared in Example 4 of the present invention; Figure 2 This is a SEM image of the catalyst support prepared in Example 4 of the present invention at 100 times magnification; Figure 3 This is a SEM image of the catalyst support prepared in Example 4 of the present invention at a magnification of 150; Figure 4 This is a SEM image of the catalyst support prepared in Example 4 of the present invention at 1000 times magnification; Figure 5 This is a SEM image at 50,000 times magnification of the catalyst support prepared in Example 4 of the present invention. DETAILED DESCRIPTION
[0040] The following will be combined with the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.
[0041] Example 1 (1) Preparation of nitric acid solution: 150 g of deionized water and 30 g of concentrated nitric acid with a mass concentration of 98% were weighed and mixed, and stirred for 5 min to obtain a nitric acid solution; (2) Preparation of aluminum sol: Weigh 600 g of aluminum powder and add it to the above nitric acid solution and stir and mix, wherein the aluminum powder is added for 10 min and stirred for 20 min, add 200 g of starch and continue stirring to form aluminum sol, wherein the starch is added for 3 min and stirred for 20 min, to obtain aluminum sol; (3) Preparing a mixed solution: After adding 60 g of ethanol to the above aluminum sol, add SnCl4 solution and continue mixing to obtain a mixed solution; wherein the SnCl4 solution is prepared by dropwise adding 4.63 g of SnCl4 into 10.15 g of deionized water and stirring evenly, the SnCl4 dropping time is 10 min, and the stirring time is 30 min; (4) Preparation of alumina drop balls: The mixed liquid was transferred to a syringe, and the distance between the needle outlet and the hydrocarbon oil surface was maintained at 4 cm to drop the balls. The spheres were separated, dried at 100°C for 7 h, and calcined at 650°C for 7.5 h to obtain alumina drop balls, which were catalyst carriers. The height of ammonia water in the oil-ammonia column was 4 meters, the height of oil was 10 mm, the concentration of ammonia water was 10 wt%, and the oil was white oil.
[0042] Example 2 (1) Preparation of nitric acid solution: 150 g of deionized water and 45 g of concentrated nitric acid with a mass concentration of 98% were weighed and mixed, and stirred for 5 min to obtain a nitric acid solution; (2) Preparation of aluminum sol: Weigh 600 g of aluminum powder and add it to the above nitric acid solution, stirring and mixing, wherein the aluminum powder is added for 10 min and stirred for 20 min, add 240 g of starch and continue stirring to form aluminum sol, wherein the starch is added for 3 min and stirred for 20 min, to obtain aluminum sol; (3) Preparing a mixed solution: adding 30 g of ethanol to the aluminum sol, and then adding a SnCl4 solution and continuing to mix to obtain a mixed solution; wherein the SnCl4 solution is prepared by dropwise adding 4.63 g of SnCl4 into 10.15 g of deionized water and stirring evenly, wherein the SnCl4 is added for 10 min and stirred for 30 min; (4) Preparation of alumina drop balls: The mixed liquid was transferred to a syringe, and the distance between the needle outlet and the hydrocarbon oil surface was maintained at 4 cm to drop the balls. The spheres were separated, dried at 100°C for 7 h, and calcined at 650°C for 7.5 h to obtain alumina drop balls, which were catalyst carriers. The height of ammonia water in the oil-ammonia column was 4 meters, the height of oil was 10 mm, the concentration of ammonia water was 10 wt%, and the oil was white oil.
[0043] Example 3 (1) Preparation of nitric acid solution: 150 g of deionized water and 30 g of concentrated nitric acid with a mass concentration of 98% were weighed and mixed, and stirred for 5 min to obtain a nitric acid solution; (2) Preparation of aluminum sol: Weigh 600 g of aluminum powder and add it to the above nitric acid solution and stir and mix, wherein the aluminum powder is added for 10 min and stirred for 20 min, add 200 g of starch and continue stirring to form aluminum sol, wherein the starch is added for 3 min and stirred for 20 min, to obtain aluminum sol; (3) Preparing a mixed solution: After adding 60 g of ethanol to the above aluminum sol, add SnCl4 solution and continue mixing to obtain a mixed solution; wherein the SnCl4 solution is prepared by dropwise adding 4.63 g of SnCl4 into 10.15 g of deionized water and stirring evenly, the SnCl4 dropping time is 10 min, and the stirring time is 30 min; (4) Preparation of alumina drop balls: The mixed liquid was transferred to a syringe, and the distance between the needle outlet and the hydrocarbon oil surface was kept at 4 cm to drop the ball. The spheres were separated, dried at 60°C for 4 h, and then dried at 100°C for 3 h. After that, they were calcined at 650°C for 7.5 h to obtain alumina drop balls, which were catalyst carriers. The height of ammonia water in the oil-ammonia column was 4 meters, the height of oil was 10 mm, the concentration of ammonia water was 10 wt%, and the oil was white oil.
[0044] Example 4 (1) Preparation of nitric acid solution: 150 g of deionized water and 30 g of concentrated nitric acid with a mass concentration of 98% were weighed and mixed, and stirred for 5 min to obtain a nitric acid solution; (2) Preparation of aluminum sol: Weigh 600 g of aluminum powder and add it to the above nitric acid solution and stir and mix, wherein the aluminum powder is added for 10 min and stirred for 20 min, add 200 g of starch and continue stirring to form aluminum sol, wherein the starch is added for 3 min and stirred for 20 min, to obtain aluminum sol; (3) Preparing a mixed solution: After adding 60 g of ethanol to the above aluminum sol, add SnCl4 solution and continue mixing to obtain a mixed solution; wherein the SnCl4 solution is prepared by dropwise adding 4.63 g of SnCl4 into 10.15 g of deionized water and stirring evenly, the SnCl4 dropping time is 10 min, and the stirring time is 30 min; (4) Preparation of alumina drop balls: The mixed solution was transferred to a syringe, and the distance between the needle outlet and the hydrocarbon oil surface was kept at 4 cm to drop the ball. The spheres were separated, dried at 60°C for 4 h, then dried at 100°C for 3 h, calcined at 300°C for 3 h, and then calcined at 650°C for 4.5 h to obtain alumina drop balls, which are catalyst carriers (see photo). Figure 1 As shown in the SEM images Figures 2~5 As shown); in the oil-ammonia column, the height of the ammonia water is 4 meters, the height of the oil is 10 mm, the concentration of the ammonia water is 10 wt%, and the oil is white oil.
[0045] Example 5 The only difference from Example 4 is that the SnCl4 solution is prepared by dropping 3g SnCl4 into 10.15g deionized water and stirring evenly, the SnCl4 dropping time is 10min, and the stirring time is 30min.
[0046] Example 6 The only difference from Example 4 is that the SnCl4 solution is prepared by dropping 6 g SnCl4 into 10.15 g deionized water and stirring evenly, the SnCl4 dropping time is 10 min, and the stirring time is 30 min.
[0047] Example 7 The only difference from Example 4 is that the calcination at 300° C. for 3 h is changed to the calcination at 200° C. for 3 h.
[0048] Example 8 The only difference from Example 4 is that the calcination at 300° C. for 3 h is changed to the calcination at 400° C. for 3 h.
[0049] Example 9 The only difference from Example 4 is that the calcination at 600° C. for 3 h is changed from calcination at 650° C. for 4.5 h.
[0050] Example 10 The only difference from Example 4 is that the calcination at 650° C. for 4.5 h is changed to calcination at 700° C. for 3 h.
[0051] Embodiment 11 After 50 g of the aluminum oxide droplets prepared in Example 4 were evenly dispersed in 100 mL of dimethyl sulfoxide, 0.05 g of 2,5-dimethoxyphenyl isocyanate was added and stirred at 50° C. for 3 h, filtered, washed with ethanol, and dried to obtain a catalyst carrier.
[0052] Example 12 The only difference from Example 11 is that 0.1 g of 2,5-dimethoxyphenyl isocyanate is used.
[0053] Example 13 The only difference from Example 11 is that 0.3 g of 2,5-dimethoxyphenyl isocyanate is added.
[0054] Embodiment 14 The only difference from Example 11 is that 0.5 g of 2,5-dimethoxyphenyl isocyanate is added.
[0055] Comparative Example 1 (1) Preparation of nitric acid solution: 150 g of deionized water and 30 g of concentrated nitric acid with a mass concentration of 98% were weighed and mixed, and stirred for 5 min to obtain a nitric acid solution; (2) Preparation of aluminum sol: Weigh 600 g of aluminum powder and add it to the above nitric acid solution and stir and mix, wherein the aluminum powder is added for 10 min and stirred for 20 min, add 200 g of starch and continue stirring to form aluminum sol, wherein the starch is added for 3 min and stirred for 20 min, to obtain aluminum sol; (3) Preparation of mixed solution: After adding 60 g of ethanol to the above aluminum sol, transfer it to a syringe, keep the distance between the needle outlet and the hydrocarbon oil surface at 4 cm to drop the ball, separate the spheres, dry them at 100°C for 7 hours, and calcine them at 650°C for 7.5 hours to obtain aluminum oxide drop balls, which are catalyst carriers; the height of ammonia water in the oil-ammonia column is 4 meters, the height of oil is 10 mm, the concentration of ammonia water is 10 wt%, and the oil is white oil.
[0056] Application Examples 1. Dehydrogenation reaction: (1) Weigh 0.171 g of stannous chloride dihydrate and dissolve it in 10 mL of hydrochloric acid solution. Add 9.8 g of the catalyst carrier while stirring and mix well. After soaking at 30°C for 12 h, dry at 100°C for 16 h and set aside. (2) Weigh 0.08 g of chloroplatinic acid hexahydrate and 0.207 g of potassium nitrate and dissolve them in 10 mL of water. Adjust the pH value to 3.0, add the above-mentioned materials while stirring and mix well. Soak at 30°C for 12 h, dry at 100°C for 16 h, and calcine in a muffle furnace at 600°C for 20 h to obtain a dehydrogenation catalyst.
[0057] Weigh 2 g of dehydrogenation catalyst and load it into the quartz tube of the fixed bed reactor. First, introduce hydrogen at a flow rate of 2 mL / s, raise the temperature to 650 °C, and activate for 2 h. Then, reduce the temperature to 600 °C, introduce a mixed gas of nitrogen at a flow rate of 0.5 mL / s and propane at a flow rate of 0.1 mL / s, and the total space velocity is 3600 h -1 . Use FID hydrogen flame ionization detector and gas chromatograph for online detection, and calculate propylene selectivity and propylene yield according to the following formula: Propylene selectivity = (amount of propylene produced / amount of propylene consumed in the reaction) × 100%; Propylene yield = (amount of propylene produced / total propane feed) × 100%; The results are recorded in Table 1.
[0058] Table 1 Propylene selectivity and propylene yield
[0059] It can be seen from Table 1 that, compared with Comparative Example 1, Example 1 adds SnCl4 solution during the preparation of the dehydrogenation catalyst carrier, while Comparative Example 1 does not add SnCl4 solution. The propylene selectivity and propylene yield of the dehydrogenation catalyst prepared from the catalyst carrier obtained in Example 1 are higher than those in Comparative Example 1, indicating that adding SnCl4 solution during the preparation of the dehydrogenation catalyst carrier can improve the catalytic effect of the dehydrogenation catalyst carrier.
[0060] The propylene selectivity and propylene yield of the dehydrogenation catalyst prepared from the catalyst support obtained in Example 3 are higher than those in Example 1, indicating that drying at 60-70°C and then at 90-100°C can further improve the catalytic effect of the catalyst support.
[0061] The propylene selectivity and propylene yield of the dehydrogenation catalyst prepared by the catalyst carrier obtained in Example 4 are higher than those in Examples 7 to 10, indicating that the two-step calcination process, first calcining at 300 to 350°C and then calcining at 650 to 700°C, can further improve the catalytic effect of the catalyst carrier.
[0062] The propylene selectivity and propylene yield of the dehydrogenation catalyst prepared by the catalyst carrier obtained in Example 4 are higher than those in Example 5 and Example 6, indicating that the mass ratio of SnCl4 to aluminum powder in the SnCl4 solution is 4.63:600, which can further improve the catalytic effect of the catalyst carrier.
[0063] The propylene selectivity and propylene yield of the dehydrogenation catalyst prepared by the catalyst carrier obtained in Examples 11 to 14 are higher than those in Example 4, indicating that the catalytic promoter effect of the catalyst carrier can be further improved by using the monoisocyanate compound and the alumina drop balls in combination. In addition, the propylene selectivity and propylene yield of the dehydrogenation catalyst prepared by the catalyst carrier obtained in Examples 12 to 13 are higher than those in Examples 11 and 14, indicating that the mass ratio of the alumina drop balls to the monoisocyanate compound is 50:0.1 to 0.3, which can further improve the catalytic promoter effect of the catalyst carrier.
[0064] 2. Reforming reaction: The catalyst carrier obtained in Example 4 was used to prepare a reforming catalyst by a conventional method. The active components in the reforming catalyst also included Pt, Eu and Ce, wherein the mass content of Pt was 0.33%, the mass content of Eu was 0.33%, and the mass content of Ce was 0.18%.
[0065] 28g of reforming catalyst was weighed and loaded into a fixed bed reactor, and reduced with hydrogen at 500℃. Straight-run naphtha was used as the raw material, and the reaction conditions were 0.7MPa, 500℃, hydrogen / oil volume ratio 800:1, and feed volume space velocity 2h -1 The reaction was carried out under the conditions of , wherein the raw material properties are: density (20°C): 0.7274 g / mL, distillation range: initial distillation point 86°C / 50% 109°C / final distillation point 151°C, composition: chain alkanes 55.7wt% / cycloalkanes 41.38wt% / aromatics 2.92wt%, aromatics potential content: 41.59wt%.
[0066] The results are recorded in Table 2.
[0067] Table 2 Aromatic hydrocarbon yield
[0068] It can be seen from Table 2 that the catalyst support provided in Example 4 of the present invention is applied to the reforming reaction and has a high aromatics yield. The effects of the catalyst supports provided in the other embodiments in the reforming reaction are similar to those in Example 4. When the catalyst support obtained in Comparative Example 1 is applied to the reforming reaction, the overall aromatics yield in each time period is 1% to 2% lower than that in the embodiment, at about 62%. When other existing catalyst supports are applied to the reforming reaction, the overall aromatics yield in each time period is much lower than that in the embodiment.
[0069] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.
Claims
1. A catalyst carrier for dehydrogenation, characterized in that: The raw materials include alumina drop balls, and the preparation method of the alumina drop balls includes the following steps: S1, after mixing aluminum powder and nitric acid solution, adding pore-forming agent and continuing to mix to obtain aluminum sol; S2, after mixing the aluminum sol and the expansion agent, adding SnCl4 solution and continuing to mix to obtain a mixed solution; S3, passing the mixed solution through an oil-ammonia column, separating the spheres, drying, and calcining to obtain alumina spheres.
2. A dehydrogenation catalyst carrier according to claim 1, characterized in that: The drying is specifically as follows: first drying at 50-70°C, and then drying at 90-110°C.
3. A dehydrogenation catalyst carrier according to claim 2, characterized in that: The calcination is specifically as follows: first calcining at 250-350°C, and then calcining at 600-700°C.
4. A dehydrogenation catalyst carrier according to claim 1, characterized in that: The pore-forming agent includes one or more of starch, dextrin, and starch derivatives.
5. A catalyst carrier for dehydrogenation according to claim 1, characterized in that: The expander is alcohol.
6. A catalyst carrier for dehydrogenation according to claim 5, characterized in that: The alcohols include one or more of ethanol, ethylene glycol, glycerol, isobutyl alcohol, and isopentanol.
7. A catalyst carrier for dehydrogenation according to claim 1, characterized in that: The raw materials also include a monoisocyanate compound, and the mass ratio of the alumina drop ball to the monoisocyanate compound is 50:0.05-0.
5.
8. A catalyst carrier for dehydrogenation according to claim 7, characterized in that: The mass ratio of the aluminum oxide drop ball to the monoisocyanate compound is 50:0.1-0.
3.
9. The method for preparing a catalyst carrier for dehydrogenation according to claim 7 or 8, characterized in that: The following steps are involved: After the aluminum oxide droplets are evenly dispersed in the solvent, the monoisocyanate compound is added and mixed evenly, filtered, washed and dried to obtain a catalyst carrier.
10. Use of the dehydrogenation catalyst carrier according to any one of claims 1 to 8 or the dehydrogenation catalyst carrier prepared by the preparation method according to claim 9 in a dehydrogenation reaction or a reforming reaction.