Process for efficiently synthesizing biological aviation kerosene precursor and catalyst regeneration method

Abstract

The invention belongs to the field of preparation of aviation kerosene from biomass, and particularly relates to a process for efficiently synthesizing a biological aviation kerosene precursor and a catalyst regeneration method. According to the method, 2-methyl furan (2-MF) and ketone compounds (cyclohexanone, methyl isobutyl ketone and acetone) are dehydrated to efficiently synthesize the C13 or C16 biological aviation kerosene precursor (BAKP), and the C13 or C16 biological aviation kerosene precursor (BAKP) is synthesized by regulating and controlling the concentration of small molecule ketone substances in reaction raw materials, the reaction temperature and the use amount of a catalyst. The problem that the yield of BAKP is low due to side reaction caused by hydrolysis ring opening of 2-MF at present is solved; according to the invention, BAKP is prevented from being hydrolyzed into ketone to initiate polymerization reaction, the blockage of catalyst pore channels is relieved, and the deactivation rate of the catalyst is slowed down. The catalyst is regenerated by using a solvent cleaning and low-temperature heat treatment scheme, so that cyclic regeneration of the organic solid acidic resin catalyst is realized.

Description

Technical Field

[0001] The invention belongs to the field of biomass-based aviation kerosene production, and in particular relates to a process for efficiently synthesizing a bio-aviation kerosene precursor and a catalyst regeneration method. Background Art

[0002] With the continuous increase in the world's air transport volume, the demand for aviation kerosene in various countries has grown rapidly, especially in China, which has a large population. Conventional aviation kerosene is not only heavily dependent on fossil energy, but also produces a large amount of greenhouse gas emissions, which cannot meet the sustainable development of the aviation industry. Bio-jet kerosene can effectively achieve greenhouse gas emission reduction and has received widespread attention. There are two routes for biomass to manufacture aviation kerosene. The first route is the Fischer-Tropsch synthesis route. This route first gasifies biomass to produce CO, CO2 and H2. After adjusting the carbon-hydrogen ratio, long-chain alkanes and olefins are generated through Fischer-Tropsch synthesis, and then through hydrogenation isomerization and distillation separation to produce aviation kerosene. The second route is to generate C5 and C6 platform compounds (2-methylfuran 2-MF, furfural, 5-hydroxymethylfuran) through the hydrolysis of cellulose and hemicellulose, and then extend the carbon chain through CC coupling to generate C8~C 16 The first scheme has a wide range of biomass sources, but it requires the long-chain compounds cellulose, hemicellulose, lignin and starch to be directly broken down into C1, and then regenerated into C8-C 16 The second solution does not break the carbon-carbon bonds in the biomass, retains the basic units of the biomass (C5-C6), has a short process route, and significantly reduces energy consumption.

[0003] In 2013, Zhang Tao, Li Shanshan and others reported in patent [CN 104689810 A] that the conversion rate of 2-MF was 14.1% under the conditions of using acidic titanium dioxide nanotubes as catalyst, 2-MF and acetone molar ratio of 2, reaction temperature of 50°C, and reaction time of 4h. 13 The yield is 5.0%. In 2014, Li Ning, Li Guangyi and others reported in patent [CN 104941680 A] that the conversion rate of 2-MF was 18.0% under the conditions of using glycerol solid acid as catalyst, 2-MF and acetone molar ratio of 2, reaction temperature of 50°C, reaction time of 2h, and C 13 The yield was 13.0%; using Nafion-212, the reaction temperature was 80°C, and the reaction time was 4h, the conversion rate of 2-MF was 58.4%, C 13The yield is 44.3%. In 2014, Li Ning, Li Shanshan and others reported in patent [CN 104971775 A] that the conversion rate of 2-MF was 65.8% under the conditions of using sodium lignin sulfonate derived phenolic resin solid acid as catalyst, 2-MF and acetone molar ratio of 2, reaction temperature of 50°C, reaction time of 24h, C 13 The yield was 53.1%.

[0004] In summary, the current synthesis of C 13 or C 16 There is a big contradiction between production efficiency and product yield in the bio-jet kerosene precursor (BAKP) method. Under low temperature conditions, the catalyst activity is low and the reaction time is long. When the temperature is increased, the catalyst activity increases, but it causes the 2-MF ring opening and side reactions. 13 The selectivity is reduced, the yield is reduced; the catalyst is easily deactivated, and the deactivated resin catalyst is easily sintered and difficult to regenerate at high temperature. Therefore, it is very urgent to develop a method for efficiently synthesizing BAKP and a catalyst regeneration process. Summary of the invention

[0005] Aiming at the problems that the catalyst activity is low at low temperature in the dehydration reaction of 2-MF and ketone compounds to prepare BAKP; the BAKP yield is low at high temperature, the catalyst is easily deactivated and the resin catalyst is difficult to regenerate. The present invention not only greatly improves the reaction rate by regulating the concentration of small molecular ketone substances in the reaction raw materials, the reaction temperature and the amount of catalyst used, but also promotes the generated water molecules and macromolecular BAKP to quickly leave the catalyst surface, reduces the occurrence of water-induced 2-MF and BAKP ring-opening side reactions under acidic site catalysis, improves the BAKP yield, and maintains the high activity of the catalyst; at the same time, the present invention also provides a regeneration process for the acidic resin catalyst in the BAKP synthesis reaction.

[0006] To achieve the above object, the technical solution of the present invention is as follows:

[0007] A process for efficiently synthesizing a bio-jet fuel precursor and a catalyst regeneration method, comprising the following steps:

[0008] 2-Methylfuran and ketone compounds are used as reaction raw materials, acid resin is used as catalyst, and dehydrating agent is added to carry out dehydration reaction; after the reaction is completed, solid-liquid separation is carried out, and the solid phase obtained after separation is the acid resin catalyst and the dehydrating agent, which are reused after solvent washing and thermal regeneration; the liquid phase obtained after separation is C 13 or C 16 A mixture of bio-jet fuel precursor, water, unreacted 2-methylfuran and ketone compounds is distilled to obtain the target product C. 13 or C 16The bio-jet fuel precursor is prepared by removing water from the obtained distillate, and then unreacted 2-methylfuran and ketone compounds are recovered.

[0009] Furthermore, the acidic resin is Amberlyst 15 (A15), Amberlyst 35 (A35) or Amberlyst 36 (A36). The above three acidic resins have large pore sizes, and the generated BAKP and water can easily diffuse from the catalyst pores into the solution. The amount of acidic resin used is 20 to 40 mmol H + / mol 2-MF, too little catalyst is used, the reaction time is long, the catalyst load is large, and side reactions are easily induced; too much catalyst is used, and the reaction TOF value is low.

[0010] Furthermore, the dehydrating agent is 3A or 4A molecular sieve. The synthesis of BAKP from 2-MF and ketone substances is a dehydration reaction, and the generated water triggers the ring-opening hydrolysis side reaction of 2-MF, and then the 2-MF trimerization side reaction occurs. Adding 3A or 4A molecular sieve to the reaction system can remove the generated water in time and hinder the occurrence of side reactions. The amount of dehydrating agent used is 20 to 40 g / mol 2-MF to remove the water generated by the reaction as much as possible.

[0011] Furthermore, the ketone compound is acetone, cyclohexanone or methyl isobutyl ketone. The above three ketones serve as both reactants and solvents, have relatively small molecular diameters, are easy to enter and exit the catalyst pores, have good solubility with 2-MF, BAKP and water, and are helpful to diffuse the BAKP and water generated by the reaction from the inside of the catalyst pores to the outside of the pores.

[0012] Furthermore, the molar ratio of the 2-methylfuran to the ketone compound is 1:2-5, preferably 1:2-3.

[0013] Furthermore, the dehydration reaction temperature is 40-100°C, preferably 50-80°C, and the time is 2-6 hours. If the reaction temperature is too low, the catalyst activity is too low; if the reaction temperature is too high, the ketone substances will be induced to undergo α, β hydroxyaldehyde condensation side reactions.

[0014] Furthermore, the solid-liquid separation method is filtration or centrifugation. The acidic resin catalyst and 3A and 4A molecular sieves are solid particles, which are insoluble in the reaction solution and can be easily separated from the solution by filtration or centrifugation.

[0015] Furthermore, the distillation conditions are: distillation pressure of -95 to 0 kpag, and distillation temperature of 50 to 110° C. Under the distillation conditions, the distillation bottom liquid is BAKP with high purity, and the gas phase condensate is unreacted 2-MF, ketone compounds and water generated by the reaction.

[0016] Furthermore, the solvent cleaning and thermal regeneration method is: ultrasonic cleaning with acetone, methanol or chloroform for 0.5 to 3 hours, and then drying for 2 to 24 hours at a pressure of -90 to 0 kPag and a temperature of 90 to 110°C to remove water and polymer compounds generated by the catalyst adsorption reaction and restore the activity of the catalyst.

[0017] Compared with the prior art, the present invention has the following beneficial effects:

[0018] (1) The present invention significantly increases the reaction rate and reduces the occurrence of side reactions, thereby increasing C 13 and C 16 The yield.

[0019] (2) The present invention helps the generated macromolecular target product BAKP and water to quickly desorb from the catalyst surface, hindering the continued hydrolysis and ring opening of BAKP to generate macromolecular ketone substances, and alleviating the chain reaction of macromolecular ketone substances with 2-MF to form polymers and block the catalyst pores, causing catalyst deactivation.

[0020] (3) The present invention solves the problem of recycling and regenerating the acid resin catalyst after deactivation. After the activity of the acid resin catalyst decreases, it can be restored by washing with acetone, methanol or chloroform, and drying at normal pressure or negative pressure at low temperature. It has little effect on the structure of the catalyst and has good reusability. Taking the reaction of acetone and 2-MF as an example, the 2-MF conversion rate was 97% at 70°C for 5 hours, and C 13 The yield was 91.5%. After the catalyst was used for the second time, the 2-MF conversion rate could still reach 96.8% under the same reaction conditions. 13 The yield was 90.8%.

[0021] (4) The reaction raw materials used in the present invention are commercialized acetone, cyclohexanone, methyl isobutyl ketone and biomass-based 2-MF, which have low raw material costs and significant economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 C is generated by the reaction of acetone and 2-MF in Example 5 13 H NMR spectrum.

[0023] Figure 2 C is generated by the reaction of acetone and 2-MF in Example 5 13 C NMR spectrum. DETAILED DESCRIPTION

[0024] In order to facilitate the understanding of the present invention, the present invention will be described more fully below. However, the present invention can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, the purpose of providing these embodiments is to make the understanding of the disclosure of the present invention more thorough and comprehensive.

[0025] In the following examples: the conversion rate is the conversion rate of 2-methylfuran; when the reactant is acetone, the yield is C 13 When the reactants are methyl isobutyl ketone and cyclohexanone, the yields are two kinds of C 16 The yield.

[0026] Example 1

[0027] Amberlyst 15 (acid amount: 20 mmol H) catalyst was added to 0.125 mol 2-MF and 0.375 mol acetone. + / mol 2-MF), and dehydrating agent 3A molecular sieve (dosage: 30g / mol 2-MF), the reaction was carried out at 70°C for 5h. The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0028] Example 2

[0029] The difference from Example 1 is that the catalyst is replaced by Amberlyst 35 (acid amount: 20 mmol H + The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0030] Example 3

[0031] The difference from Example 1 is that the catalyst is replaced by Amberlyst 36 (acid amount: 5 mmol H + The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0032] Example 4

[0033] The difference from Example 1 is that the catalyst is replaced by Amberlyst 36 (acid amount: 10 mmol H + The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0034] Example 5

[0035] The difference from Example 1 is that the catalyst is replaced by Amberlyst 36 (acid amount: 20 mmol H + The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0036] Example 6

[0037] The difference from Example 1 is that the catalyst is replaced by Amberlyst 36 (acid amount: 40 mmol H +The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0038] Example 7

[0039] The difference from Example 1 is that the catalyst is replaced by Amberlyst 36 (acid amount: 50 mmol H + The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0040] Comparative Example 1

[0041] The difference from Example 1 is that 3A molecular sieve is not added, and the catalyst is replaced by Amberlite-732 (acid amount: 20 mmol H + / mol 2-MF). The conversion rate, yield, selectivity and TOF value of the reaction are shown in Table 1.

[0042] Table 1: Effects of different catalysts and usage on the reaction

[0043]

[0044] (Note: Table 1 a Acid amount: 5mmol H + / mol 2-MF, b Acid amount: 10mmol H + / mol 2-MF, c Acid content: 40mmolH + / mol2-MF, d Acid amount: 50mmol H + / mol 2-MF, remaining acid amount: 20mmol H + / mol 2-MF).

[0045] As can be seen from Table 1, the Amberlite-732 resin with a high water content in Comparative Example 1 has low activity and selectivity. The pores of the A15, A35 and A36 acidic resins that are almost free of water gradually increase, and their activity and selectivity gradually increase. + The activity and selectivity of the catalyst are higher when the 2-MF content is in the range of 20 to 40 mmol per mole.

[0046] Example 8

[0047] The difference from Example 5 is that the water removal agent is 3A molecular sieve (dosage: 10 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 2.

[0048] Example 9

[0049] The difference from Example 5 is that the water removal agent is 3A molecular sieve (dosage: 20 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 2.

[0050] Example 10

[0051] The difference from Example 5 is that the water removal agent is replaced by 4A molecular sieve (dosage: 30 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 2.

[0052] Embodiment 11

[0053] The difference from Example 5 is that the water removal agent is 3A molecular sieve (dosage: 40 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 2.

[0054] Example 12

[0055] The difference from Example 5 is that the water removal agent is 3A molecular sieve (dosage: 50 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 2.

[0056] Table 2: Effect of dehydrating agent dosage on reaction

[0057]

[0058] (Note: Table 2 a : The dehydrating agent is 4A molecular sieve, and the rest are 3A molecular sieve)

[0059] It can be seen from Table 2 that both 3A and 4A molecular sieves can quickly remove the water generated by the reaction. When the molecular sieve is used in an amount of 20 to 40 g / mol 2-MF, the water generated by the reaction can be effectively removed to maintain the activity and selectivity of the catalyst.

[0060] Example 13

[0061] The difference from Example 1 is that the catalyst is replaced by Amberlyst 35 (acid amount: 20 mmol H + / mol2-MF), the water scavenger was replaced by 4A molecular sieve (dosage: 30 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 3.

[0062] Embodiment 14

[0063] The difference from Example 13 is that acetone is replaced by methyl isobutyl ketone. The conversion rate, yield and selectivity of the reaction are shown in Table 3.

[0064] Embodiment 15

[0065] The difference from Example 13 is that acetone is replaced by cyclohexanone. The conversion rate, yield and selectivity of the reaction are shown in Table 3.

[0066] Table 3: Reaction of 2-methylfuran with different ketone compounds

[0067]

[0068] As can be seen from Table 3, in the alkylation reaction with 2-methylfuran, the order of reactivity and selectivity of different ketone compounds is: acetone>methyl isobutyl ketone>cyclohexanone.

[0069] Example 16

[0070] The difference from Example 1 is that the molar ratio of 2-MF to acetone is 1:1 (2-MF 0.125 mol), the reaction temperature is 80°C, the reaction time is 2 h, and the catalyst is replaced by Amberlyst 36 (acid amount: 20 mmol H + / mol 2-MF), the water scavenger was replaced with 4A molecular sieve (dosage: 30 g / mol 2-MF). The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0071] Embodiment 17

[0072] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 1:2. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0073] Embodiment 18

[0074] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 1:3. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0075] Embodiment 19

[0076] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 1:4. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0077] Embodiment 20

[0078] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 1:5. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0079] Embodiment 21

[0080] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 1:6. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0081] Comparative Example 2

[0082] The difference from Example 16 is that the molar ratio of 2-MF to acetone is 2: 1. The conversion rate, yield and selectivity of the reaction are shown in Table 4.

[0083] Table 4: Effect of 2-MF to acetone molar ratio on the reaction

[0084]

[0085] It can be seen from Table 4 that when the acetone concentration in Comparative Example 2 is low, the activity and selectivity of the catalyst are low; with the increase of acetone content, the reaction activity and selectivity of the catalyst are increased, and when the molar ratio of 2-MF to acetone is less than 1:5, increasing the acetone content has little effect on the reaction.

[0086] Embodiment 22

[0087] The difference from Example 5 is that the reaction temperature is 40° C. The conversion rate, yield and selectivity of the reaction are shown in Table 5.

[0088] Embodiment 23

[0089] The difference from Example 5 is that the reaction temperature is 50° C. The conversion rate, yield and selectivity of the reaction are shown in Table 5.

[0090] Embodiment 24

[0091] The difference from Example 5 is that the reaction temperature is 60° C. The conversion rate, yield and selectivity of the reaction are shown in Table 5.

[0092] Embodiment 25

[0093] The difference from Example 5 is that the reaction temperature is 80° C. The conversion rate, yield and selectivity of the reaction are shown in Table 5.

[0094] Table 5: Effect of different reaction temperatures on the reaction

[0095]

[0096] It can be seen from Table 5 that as the reaction temperature increases, the catalyst activity increases, but the selectivity gradually decreases. The highest BAKP yield of 91.5% can be obtained at 70°C for 5 h.

[0097] Embodiment 26

[0098] The reaction conditions were the same as those in Example 5. After the reaction was completed, the catalyst and the liquid phase were separated by filtration, and the separated liquid phase was distilled. The distillate was partially recovered to replace the acetone in the next reaction. The distillation conditions were: normal pressure, 110° C. The conversion rate, yield and selectivity of the reaction are shown in Table 6.

[0099] Embodiment 27

[0100] The difference from Example 26 is that the distillate was recovered twice, and the distillation conditions were: -50 kPag, 60° C. The conversion rate, yield and selectivity of the reaction are shown in Table 6.

[0101] Embodiment 28

[0102] The difference from Example 26 is that the distillate was recovered three times and the distillation conditions were: -95 kPag, 50° C. The conversion rate, yield and selectivity of the reaction are shown in Table 6.

[0103] Table 6: Recycling of unreacted materials

[0104]

[0105] Note: Table 6 a : Distillation pressure: normal pressure, temperature: 110℃, b : Distillation pressure -50kpag, temperature 60℃, c : Distillation pressure -95kpag, temperature 50℃.

[0106] It can be seen from Table 6 that a large amount of unreacted acetone and a small amount of 2-methylfuran can be recovered by atmospheric pressure or negative pressure distillation, and the reuse of the distillate has little effect on the reaction.

[0107] Embodiment 29

[0108] The reaction conditions were the same as those in Example 5. After the reaction was completed, the catalyst and the liquid phase were separated by centrifugation, and the solid phase obtained after separation was ultrasonically cleaned with 10 mL of acetone for half an hour, and then dried at -90 kPag and 80° C. for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0109] Embodiment 30

[0110] The difference from Example 29 is that the drying is carried out at -80 kPag and 90°C for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0111] Embodiment 31

[0112] The difference from Example 29 is that the drying is carried out at -50 kPag and 100°C for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0113] Embodiment 32

[0114] The difference from Example 29 is that the drying is carried out at -50 kPag and 110°C for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0115] Embodiment 33

[0116] The difference from Example 29 is that the drying is carried out at -50 kPag and 120°C for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0117] Embodiment 34

[0118] The difference from Example 29 is that the drying is carried out at -50 kPag and 130°C for 12 hours. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0119] Embodiment 35

[0120] The difference from Example 29 is that acetone was replaced by methanol and the mixture was dried at -50 kPag and 100°C for 12 h. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0121] Embodiment 36

[0122] The difference from Example 29 is that acetone is replaced by chloroform and the mixture is dried at -50 kPag and 100°C for 12 h. The conversion rate, yield and selectivity of the reaction are shown in Table 7.

[0123] Table 7: Effect of catalyst and dehydrating agent (regenerated 5 times) regeneration conditions on the reaction

[0124]

[0125] As can be seen from Table 7, the catalyst can be restored to activity after being washed with acetone, methanol and chloroform and dried for 12 hours at a pressure of -50 kpag and a temperature of 90-110°C. When the temperature is lower than 90°C, water adsorbed on the acid sites of the catalyst is difficult to desorb, which reduces the utilization rate of the acid sites. When the temperature is higher than 120°C, the catalyst is easy to sinter and block the pores, making it difficult for reactants and products to enter and exit the pores, thereby reducing the activity of the catalyst.

[0126] The above description is only for better explaining the embodiments of the present invention, and is not intended to limit the present invention. Any modification or equivalent substitution that does not depart from the spirit and scope of the present invention shall fall within the scope of the present invention.

Claims

1. A process for efficiently synthesizing bio-jet fuel precursor and a catalyst regeneration method, characterized in that: The following steps are involved: 2-Methylfuran 2-MF and ketone compounds are used as reaction raw materials, acid resin is used as catalyst, and dehydrating agent is added to carry out dehydration reaction; after the reaction is completed, solid-liquid separation is carried out, and the solid phase obtained after separation is the acid resin catalyst and the dehydrating agent, which are reused after solvent washing and thermal regeneration; the liquid phase obtained after separation is C 13 or C 16 A mixture of bio-jet fuel precursor, water, unreacted 2-methylfuran and ketone compounds is distilled to obtain the target product C. 13 or C 16 The bio-jet fuel precursor is prepared by removing water from the obtained distillate, and then unreacted 2-methylfuran and ketone compounds are recovered.

2. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The acidic resin is Amberlyst 15, Amberlyst 35 or Amberlyst 36, and the amount used is 20-40 mmol H + / mol 2-MF.

3. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The dehydrating agent is 3A or 4A molecular sieve, and the usage amount is 20-40 g / mol 2-MF.

4. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The ketone compound is acetone, cyclohexanone or methyl isobutyl ketone.

5. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The molar ratio of the 2-methylfuran to the ketone compound is 1:2-5.

6. A process for efficiently synthesizing bio-jet fuel precursor and a catalyst regeneration method according to claim 5, characterized in that: The molar ratio of the 2-methylfuran to the ketone compound is 1:2-3.

7. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The temperature of the dehydration reaction is 40-100° C. and the time is 2-6 hours.

8. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The solid-liquid separation method is filtration or centrifugation.

9. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The distillation conditions are: distillation pressure of -95 to 0 kpag, and distillation temperature of 50 to 110°C.

10. The process for efficiently synthesizing bio-jet fuel precursor and the catalyst regeneration method according to claim 1, characterized in that: The method of solvent cleaning and thermal regeneration is: ultrasonic cleaning with acetone, methanol or chloroform for 0.5 to 3 hours, and then drying at a pressure of -90 to 0 kPag and a temperature of 90 to 110° C. for 2 to 24 hours.

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