CN110465298B - Catalyst for directly preparing long carbon chain compound from saccharide fermentation product ABE and preparation method thereof - Google Patents

Catalyst for directly preparing long carbon chain compound from saccharide fermentation product ABE and preparation method thereof Download PDF

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CN110465298B
CN110465298B CN201910809730.9A CN201910809730A CN110465298B CN 110465298 B CN110465298 B CN 110465298B CN 201910809730 A CN201910809730 A CN 201910809730A CN 110465298 B CN110465298 B CN 110465298B
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abe
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王威燕
刘嘉俊
杨运泉
仵奎
王超
杨晓峰
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Xiangtan University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/007—Mixed salts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/78—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with alkali- or alkaline earth metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/391—Physical properties of the active metal ingredient
    • B01J35/394—Metal dispersion value, e.g. percentage or fraction
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/32—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions without formation of -OH groups
    • C07C29/34—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions without formation of -OH groups by condensation involving hydroxy groups or the mineral ester groups derived therefrom, e.g. Guerbet reaction
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
    • C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
    • C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
    • C07C45/70—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction with functional groups containing oxygen only in singly bound form
    • C07C45/71—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction with functional groups containing oxygen only in singly bound form being hydroxy groups

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Abstract

The invention discloses a catalyst for directly preparing a long carbon chain compound by using a saccharide fermentation product ABE and a preparation method thereof. The catalyst consists of a carrier magnesium aluminum composite oxide/carbon and active components Co and Ni, and the preparation process comprises the following steps: firstly, adding activated carbon pretreated by nitric acid into a container filled with Na2CO3And then, dropwise adding a mixed solution of metal Mg and Al salts and a NaOH solution into the aqueous solution by adopting a precipitation method, controlling the pH value of the solution to be 9.5-10.5, pouring the reaction solution into a reaction kettle for hydrothermal crystallization after dropwise adding is finished, and preparing the Co-Ni/Mg-Al-O/C catalyst by filtering, impregnating, loading, calcining and reducing the precipitate by hydrogen. The catalyst has high catalytic activity on the condensation reaction of the carbohydrate fermentation product ABE, and the product is very favorable for preparing high-quality locomotive fuel oil by hydrodeoxygenation.

Description

Catalyst for directly preparing long carbon chain compound from saccharide fermentation product ABE and preparation method thereof
Technical Field
The invention relates to the development and utilization of renewable energy sources, in particular to a catalyst for preparing a long-carbon-chain compound by condensing saccharide fermentation products (acetone, n-butanol and ethanol, ABE for short) and alcohol ketone and a preparation method thereof.
Background
The increasing exhaustion of fossil energy and the environmental pollution caused by the utilization of fossil energy are forcing the development of renewable alternative energy. The carbohydrate is a renewable biomass with wide sources, and can generate a mixture (ABE for short) of acetone, n-butanol and ethanol after fermentation under a mature process, but the mixture cannot be directly used as fuel oil due to the characteristics of the molecular structure and the element composition. If ABE is condensed, the carbon chain can be obviously prolonged, the carbon number in the molecular structure of the product is increased, and raw materials are provided for preparing high-quality locomotive fuel. Therefore, how to improve the condensation efficiency of ABE is the core of preparing the carbohydrate compound into renewable fuel oil, and the key point is to develop a cheap and efficient catalyst.
To date, a variety of condensation catalysts have been studied and prepared, such as Hyunjoo Lee et al [ chem. Eng. J. 2017, 313, 1486-]The condensation reaction between the saccharide fermentation product ABE was studied using Pd/C and CaO heterogeneous catalyst, and C was found5~C11The total yield of ketones and related alcohols is 78.1% (calculated on the basis of acetone), but the use amount of noble metal catalyst is large (the mass content of Pd is 5 wt%), and the cost is expensive. Tianweii Tan et al [ ACS Sustainable chem. Eng. 2017, 5, 8181-]Ni-MgO-SiO with hydrophobicity2The catalyst is used in the condensation reaction of ABE mixture, the average conversion rate reaches 81.8 percent, C5~C15The total yield of the ketones and the related alcohols reaches 72.9 percent, but the reaction temperature is higher (about 240 ℃), and the yield of the butyl butyrate serving as a byproduct is close to 16 percent, which is not beneficial to preparing the locomotive fuel. Recent literature reports [ J. Catal., 2015, 331: 193]The layered structure of hydrotalcite is beneficial to improving the dispersion of metal active components, and is often selected as a precursor of a composite oxide to improve the activity of the catalyst. Chinese invention CN201510492948.8 provides a SiO film2The modified hydrotalcite is used for preparing isophorone by acetone condensation, the reaction effect is improved, but the reaction effect is still not ideal enough, after 120 hours of reaction, the conversion rate of acetone is only 50.06% at most, and the yield of isophorone is only 23.73%.
Disclosure of Invention
The invention aims to provide a catalyst for directly preparing a long carbon chain compound from a saccharide fermentation product ABE and a preparation method thereof, the catalyst has higher condensation activity on the ABE, particularly has high selectivity on a target product of ketone and related alcohol, only generates a small amount of by-products, basically has no by-product butyl butyrate, is beneficial to preparing locomotive fuel by subsequent further catalytic hydrodeoxygenation, and simultaneously has magnetism and easy separation.
The technical scheme of the invention is as follows:
a catalyst for directly preparing long-carbon-chain compounds from saccharide fermentation product ABE is composed of carrier (Mg-Al composite oxide/carbon) and active components (Co and Ni).
The preparation method of the catalyst comprises the following steps:
(1) commercial activated carbon was pretreated with nitric acid and then added to Na-containing solution2CO3Preparing a solution (A) in the solution; preparing a mixed solution (B) from a magnesium salt and an aluminum salt; then 0.8-1.5 mol/L NaOH aqueous alkali (C) is prepared; simultaneously dropwise adding the solution (B) and the solution (C) into the solution (A), controlling the pH of a reaction solution to be 9.5-10.5, pouring the mixed suspension into a reaction kettle for hydrothermal crystallization after the precipitation reaction is finished, and finally carrying out suction filtration, washing and drying on a precipitate to obtain the magnesium-aluminum hydrotalcite/carbon;
(2) adding the magnesium-aluminum hydrotalcite/carbon carrier into a mixed solution of cobalt salt and nickel salt by adopting an impregnation method, and carrying out vacuum drying, calcining and hydrogen reduction to obtain the Co-Ni/Mg-Al-O/C catalyst.
Further, the mass content of carbon in the carrier is 5-95%, and the mass content of active components in the catalyst is 2-50%.
Furthermore, the molar ratio of Mg to Al in the carrier is 1-4: 1, and the molar ratio of Co to Ni as an active component is 0.05-20.
Further, the commercial activated carbon is pretreated by nitric acid, wherein the concentration of the nitric acid is 0.8-3.2 mol/L, the treatment time is 1-10 h, and the treatment temperature is 20-70 ℃.
Further, in the step (1), the hydrothermal crystallization is carried out for 2-12 hours at a temperature of 20-105 ℃.
Further, in the step (2), the inert atmosphere is calcined, wherein the calcining atmosphere is one or more of nitrogen, helium or argon, the temperature is 350-650 ℃, and the time is 2-10 hours.
Further, in the step (2), the cobalt salt is one or more than two of cobalt nitrate, cobalt sulfate, cobalt chloride and cobalt acetate; the nickel salt is one or more than two of nickel nitrate, nickel sulfate, nickel chloride and nickel acetate.
Further, in the step (2), the hydrogen is reduced at the temperature of 400-800 ℃ for 2-10 h.
The invention has the beneficial effects that:
according to the invention, magnesium aluminum hydrotalcite/carbon is taken as a carrier precursor, and the characteristic that the double-layer structure of hydrotalcite is beneficial to dispersing active components is utilized, cobalt and nickel are loaded on the carrier precursor, and then the Co-Ni/Mg-Al-O/C catalyst is obtained through calcination and hydrogen reduction.
Drawings
FIG. 1 is an X-ray powder diffraction pattern of the Co-Ni/Mg-Al-O/C catalyst obtained in example 1 of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following examples, but the present invention is not limited thereto.
The reagents used in the examples were all analytical grade.
Example 1
0.9725g of sodium carbonate was weighed, dissolved in 35mL of ultrapure water (A), and 0.7656g of activated carbon pretreated with nitric acid (nitric acid concentration: 1mol/L, treatment time: 3 hours, treatment temperature: 50 ℃ C.) was poured into a 500mL three-necked flask, and vigorously stirred at room temperature for 20 min. Then 5.34g of magnesium nitrate and 2.87g of aluminum nitrate are weighed and dissolved in 35mL of ultrapure water (B) to be poured into a constant-pressure titration funnel at one side of the three-neck flask, 2.8g of sodium hydroxide is dissolved in 70mL of ultrapure water to be prepared into 1mol/L aqueous alkali (C) to be poured into a constant-pressure titration funnel at the other side of the three-neck flask, the solutions (B) and (C) are simultaneously dripped into the solution (A), the pH of the reaction solution is controlled to be 9.5-10.5, stirring is continued for 6h after the dripping is finished, then the mixture is poured into a hydrothermal kettle to be crystallized for 10h at 95 ℃, and finally, precipitates are filtered, washed and dried to obtain magnesium aluminum hydrotalcite/carbon, wherein the mass content of the carbon is 48 wt%. 1.36g of magnesium aluminum hydrotalcite/carbon is taken, added with mixed metal salt solution of cobalt nitrate and nickel nitrate for impregnation loading, then calcined for 4 hours at 500 ℃ in nitrogen atmosphere to obtain a catalyst precursor, and then reduced at 750 ℃ in hydrogen atmosphere to obtain Co-Ni/Mg-Al-O/C, wherein the mass content of the active component Co is 5wt%, and the mass content of Ni is 7.5 wt%. 14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the prepared catalyst are added into a high-pressure autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after the reaction is carried out for 20 hours, the acetone conversion rate reaches 71.2%, the total selectivity of the target product ketone and related alcohols reaches 91.5%, and the by-product butyl butyrate is basically not generated.
Example 2
The rest is the same as in example 1, except that: the carbon content is 5 percent, the active component mass content is 50 percent, and the molar ratio of the Co/Ni active component is 0.05.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 2 are added into a high-pressure autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, the acetone conversion rate reaches 60.2 percent after the reaction is carried out for 20 hours, the total selectivity of the target product ketones and related alcohols reaches 85.5 percent, and the by-product butyl butyrate is basically not generated.
Example 3
The rest is the same as in example 1, except that: the Mg/Al molar ratio is 4:1, the hydrogen reduction temperature is 400 ℃, and the reduction time is 2 h.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 2 are added into a high-pressure autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after 20 hours of reaction, the acetone conversion rate reaches 65.6%, the total selectivity of the target product ketones and related alcohols reaches 83.4%, and the by-product butyl butyrate is basically not generated.
Example 4
The rest is the same as in example 1, except that: the Mg/Al molar ratio is 1:1, the calcining temperature is 650 ℃, and the calcining time is 2 hours.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 4 are added into an autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after 20 hours of reaction, the acetone conversion rate reaches 56.6%, the total selectivity of the target product ketones and related alcohols reaches 75.5%, and the by-product butyl butyrate is basically not generated.
Example 5
The rest is the same as in example 1, except that: the condition of the pretreated active carbon is that the active carbon is treated by 0.8mol/L nitric acid at the temperature of 70 ℃ for 1h, the hydrogen reduction temperature is 800 ℃, and the time is 2 h.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 5 are added into a high-pressure autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after 20 hours of reaction, the acetone conversion rate reaches 63.5%, the total selectivity of the target product ketones and related alcohols reaches 84.8%, and a byproduct butyl butyrate is basically not generated.
Example 6
The rest is the same as in example 1, except that: the hydrothermal crystallization time is 12 hours, the crystallization temperature is 105 ℃, the calcination temperature is 350 ℃, and the calcination time is 10 hours.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 6 are added into an autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after 20 hours of reaction, the acetone conversion rate reaches 53.2%, the total selectivity of the target product ketones and related alcohols reaches 89.4%, and the by-product butyl butyrate is basically not generated.
Example 7
The rest is the same as in example 1, except that: the content of carbon is 95 percent, the molar ratio of Co/Ni is 20, the calcining temperature is 450 ℃, and the calcining time is 2 hours.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 7 are added into an autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, the acetone conversion rate is 41.3 percent after the reaction is carried out for 20 hours, the total selectivity of the target product ketones and related alcohols reaches 76.5 percent, and the by-product butyl butyrate is basically not generated.
Example 8
The rest is the same as in example 1, except that: the hydrogen reduction temperature is 400 ℃, and the reduction time is 10 h.
14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 8 are added into an autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, after 20 hours of reaction, the acetone conversion rate reaches 67.7%, the total selectivity of the target product ketones and related alcohols reaches 87.1%, and the by-product butyl butyrate is basically not generated.
Example 9
The catalyst was prepared exactly as in example 1. 26.58g of n-dodecane, 3g of acetone, 6g of n-butanol, 1g of ethanol and 1.89g of the catalyst prepared in example 9 are added into a high-pressure autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, the acetone conversion rate reaches 72.4 percent after the reaction is carried out for 20 hours, the total selectivity of the target product ketone and related alcohols reaches 90.8 percent, and the by-product butyl butyrate is basically not generated.
Example 10
The catalyst was prepared exactly as in example 1. 14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 10 are added into a high-pressure autoclave, a device is installed, the temperature is increased to 180 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.7MPa, the acetone conversion rate reaches 69.7 percent after the reaction is carried out for 20 hours, the total selectivity of the target product ketones and related alcohols reaches 84.6 percent, and the by-product butyl butyrate is basically not generated.
Example 11
The catalyst was prepared exactly as in example 1. 14.35g of n-dodecane, 1.58g of acetone, 3.24g of n-butanol, 0.55g of ethanol and 1g of the catalyst prepared in example 11 are added into an autoclave, a device is installed, the temperature is raised to 200 ℃, the rotation speed is adjusted to 900r/min, the nitrogen pressure is 1.3MPa, after 20 hours of reaction, the acetone conversion rate reaches 65.5%, the total selectivity of the target product ketones and related alcohols reaches 92.0%, and the by-product butyl butyrate is basically not generated.

Claims (9)

1. A catalyst for catalyzing a saccharide fermentation product ABE to directly prepare a long carbon chain compound is characterized by comprising a carrier and active components, wherein the carrier is a magnesium-aluminum composite oxide/carbon, and the active components are Co and Ni;
the preparation method of the catalyst for directly preparing the long carbon chain compound by catalyzing the carbohydrate fermentation product ABE is characterized by comprising the following steps of:
(1) commercial activated carbon was pretreated with nitric acid and then added to Na-containing solution2CO3Preparing a solution (A) in the solution; preparing a mixed solution (B) from a magnesium salt and an aluminum salt; then preparing 1mol/L NaOH alkaline solution (C); simultaneously dropwise adding the solutions (B) and (C) into the solution (A), controlling the pH of a reaction solution to be 9.5-10.5, pouring the obtained mixed suspension into a reaction kettle for hydrothermal crystallization after the precipitation reaction is finished, and finally performing suction filtration, washing and drying on the precipitate to obtain the magnesium-aluminum hydrotalcite/carbon;
(2) adding the magnesium-aluminum hydrotalcite/carbon carrier into a mixed solution of cobalt salt and nickel salt by adopting an impregnation method, and carrying out vacuum drying, calcining in an inert atmosphere and hydrogen reduction to obtain the Co-Ni/Mg-Al-O/C catalyst.
2. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound as claimed in claim 1, which comprises the following steps:
(1) commercial activated carbon was pretreated with nitric acid and then added to Na-containing solution2CO3Preparing a solution (A) in the solution; preparing a mixed solution (B) from a magnesium salt and an aluminum salt; then preparing 1mol/L NaOH alkaline solution (C); simultaneously dropwise adding the solutions (B) and (C) into the solution (A), controlling the pH of a reaction solution to be 9.5-10.5, pouring the obtained mixed suspension into a reaction kettle for hydrothermal crystallization after the precipitation reaction is finished, and finally performing suction filtration, washing and drying on the precipitate to obtain the magnesium-aluminum hydrotalcite/carbon;
(2) adding the magnesium-aluminum hydrotalcite/carbon carrier into a mixed solution of cobalt salt and nickel salt by adopting an impregnation method, and carrying out vacuum drying, calcining in an inert atmosphere and hydrogen reduction to obtain the Co-Ni/Mg-Al-O/C catalyst.
3. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: the mass content of carbon in the carrier is 5-95%, and the mass content of active components in the catalyst is 2-50%.
4. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: the molar ratio of Mg to Al in the carrier is 1-4: 1, and the molar ratio of Co to Ni in the active component is 0.05-20.
5. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: the method is characterized in that commercial activated carbon is pretreated by nitric acid, the concentration of the nitric acid is 0.8-3.2 mol/L, the treatment time is 1-10 h, and the treatment temperature is 20-70 ℃.
6. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: in the step (1), the hydrothermal crystallization is carried out for 2-12 h at 20-105 ℃.
7. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: in the step (2), the inert atmosphere is calcined, wherein the inert atmosphere is one or more of nitrogen, helium and argon, the temperature is 350-650 ℃, and the time is 2-10 hours.
8. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: in the step (2), the cobalt salt is one or more than two of cobalt nitrate, cobalt sulfate, cobalt chloride and cobalt acetate; the nickel salt is one or more than two of nickel nitrate, nickel sulfate, nickel chloride and nickel acetate.
9. The method for preparing the catalyst for catalyzing the sugar fermentation product ABE to directly prepare the long carbon chain compound according to claim 2, wherein the method comprises the following steps: in the step (2), the hydrogen is reduced at the temperature of 400-800 ℃ for 2-10 h.
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