CN115636739A - A kind of method of synthetic gas one-step process acetone - Google Patents

Abstract

A one-step method for producing acetone from synthesis gas, using synthesis gas (CO/H ₂ ) as a raw material, and preparing acetone-based products through CO hydrogenation reaction on a multifunctional composite catalyst in one step. Among them, the multifunctional composite catalyst has the catalytic function of methanol synthesis, methanol carbonylation, and acetic acid ketonylation to prepare acetone. The method comprises the following steps: 1) placing a catalyst in a reactor for pretreatment; 2) feeding synthesis gas for catalytic reaction to obtain acetone. The catalyst is compounded by the metal oxide with the function of producing methanol from syngas, the zeolite molecular sieve with the function of producing acetic acid from methanol carbonylation, and the supported metal oxide which can produce acetone from the ketoylation of acetic acid. The invention utilizes relay catalysis, shortens the reaction steps, improves the catalytic efficiency, realizes the selectivity of the target product acetone as high as 90% or more; does not need to separate intermediate products, consumes less energy in the overall process, has low cost, and has good application prospects.

Description

A kind of method of synthetic gas one-step process acetone

technical field

The invention relates to the field of chemical industry, in particular to a method for producing acetone by one-step synthesis gas, in particular to one-step production of acetone by CO hydrogenation on a multifunctional composite catalyst.

Background technique

The development of non-petroleum-based carbon-based resources to produce liquid fuels and high-value chemicals is of great significance. Among them, coal, biomass, natural gas, and shale gas are steam reformed or carbon dioxide reduced to obtain synthesis gas, and synthesis gas can be produced through catalytic conversion. fuels and high value chemicals. However, except for methanol and methane, the carbon number distribution of the synthesis gas conversion reaction products is relatively wide, so it is necessary to focus on how to regulate the products in a specific carbon number range or even realize the formation of a single product.

Studies in recent years have shown that syngas can be converted to gasoline, diesel, aviation kerosene, light olefins, aromatics, and C2 ₊ oxygenates with high selectivity by designing dual-functional catalysts, breaking through the selectivity limitation of syngas conversion. The highly selective synthesis of products in a specific carbon number range has been achieved. In order to achieve high selectivity of a single product, researchers have proposed the idea of relay catalysis, starting from syngas to produce C2 chemicals such as ethanol (Nat. Commun., 2020, 11:827-837) and ethylene ( Angew.Chem.Int.Ed., 2018,57:12012-12016), acetic acid (CN109908947A), and C3 chemicals such as methyl acetate (CN108774130A), etc.

As an important C3 chemical, acetone is widely used as a solvent in industries such as plastics, fibers, rubber, and spray paint, and can also be used as an important raw material for the production of high-value products such as bisphenol A, ketene, and methyl methacrylate. Acetone can also be used for chip surface cleaning and liquid chromatography eluent. The direct method of producing acetone from synthesis gas can only achieve acetone selectivity of 13.5% (Catal. Commun., 2009, 10: 468-471), and the selectivity of the remaining by-products is high. In 2014, a Chinese patent disclosed a process for producing acetone from syngas (CN104193606A). on the device. In this process, the methanol carbonylation reaction catalyst is a homogeneous catalyst involving noble metals and iodides, resulting in higher costs and corrosion to equipment. On the other hand, the indirect method needs to use different reactors, and all intermediate products need to be separated, resulting in large energy consumption and high cost of equipment.

Contents of the invention

The purpose of the present invention is to solve the above-mentioned problems in the prior art, to provide a method for producing acetone from syngas in one step, using relay catalysis, shortening the reaction steps, improving the catalytic efficiency, and realizing the selectivity of the target product acetone as high as 90% or more; no need to separate intermediate The product, the energy consumption of the overall process is less, the cost is low, and it has a good application prospect.

To achieve the above object, the present invention adopts the following technical solutions:

A method for producing acetone from synthesis gas in one step, comprising placing a composite catalyst in a reactor for pretreatment, and then feeding synthesis gas to carry out a catalytic reaction to obtain acetone; the composite catalyst is composited in a multi-bed manner, Relay catalytic reaction, in which, the metal oxide catalyst for syngas to methanol is placed in the first bed, the zeolite molecular sieve for methanol carbonylation to acetic acid is placed in the second bed, and the supported metal oxide for ketone ketone to acetone is placed in the second bed. Third bed.

In the composite catalyst, the mass ratio of the metal oxide for the production of methanol from synthesis gas, the zeolite molecular sieve for the production of acetic acid by carbonylation of methanol, and the supported metal oxide for the production of acetone by ketoylation of acetic acid is 1:(0.5～4):( 0.5～4).

The metal oxides for methanol production from syngas are selected from Cu-ZnO-Al ₂ O ₃ , Pd-ZnO-Al ₂ O ₃ , ZnO-Cr ₂ O ₃ -Al ₂ O ₃ , ZnO-Cr ₂ O ₃ , ZnO -At least one of ZrO ₂ , CeO ₂ -ZrO ₂ , ZnO-Al ₂ O ₃ , ZnO-Ga ₂ O ₃ , ZnO-Fe ₂ O ₃ , In ₂ O ₃ -ZnO, In ₂ O ₃ -Al ₂ O ₃ A sort of.

The zeolite molecular sieve for the carbonylation of methanol to acetic acid is selected from at least one of MOR, FER, IWW, and MEL zeolite molecular sieves with an eight-membered ring topology.

The zeolite molecular sieve has a microporous structure, wherein the pore diameter of the micropores is 0.2-0.8 nm, and the pore volume of the micropores is 0.05-0.5 cm ³ /g.

The supported metal oxide for the preparation of acetone from acetic ketone is denoted as x wt.% MO _x /Y, wherein the range of x is 5% to 50%, and M is Ce, Mn, Zr, La, Pr, Nd Y is at least one of H-MOR, H-ZSM-5, Al ₂ O ₃ , SiO ₂ , TiO ₂ , MgO, and CaCO ₃ .

The pretreatment method of the composite catalyst is as follows: after the catalyst is installed on the fixed bed, fluidized bed or moving bed reactor, hydrogen gas or a mixture of hydrogen gas and inert gas is introduced, and the temperature is raised to 200～500℃, and keep it for 0.5～10h, then switch to inert gas purging for 0.1～5h.

The method of the catalytic reaction is as follows: After the composite catalyst is pretreated, the temperature is lowered to 30-200° C., and the synthesis gas is introduced, wherein the volume ratio of H and _CO is 1: (0.2-3), and then the temperature is raised to the reaction temperature. The temperature is 200-400°C, the reaction pressure is 0.5-7MPa, the space velocity of the synthesis gas is 500-15000h ^-1 , and the synthesis gas is reacted through the catalyst bed to obtain the product acetone

Compared with the prior art, the beneficial effects obtained by the technical solution of the present invention are:

1. The present invention is a new process of direct method. Acetone can be obtained by one-step method of synthesis gas. The process is simple. Relay catalysis is used to ensure the controllable progress of the reaction. There is no need to separate intermediate products. The overall process consumes less energy, greatly reduces equipment, and reduces costs. Can be mass-produced;

2. The present invention utilizes relay catalysis to couple syngas to methanol, methanol heterogeneous carbonylation to acetic acid, and acetic acid ketoylation to acetone, wherein the metal oxides used to synthesize methanol are mainly activated by CO hydrogenation to generate methanol intermediates, with hierarchical pores Zeolite molecular sieves are responsible for catalyzing the intermediate product methanol to further generate acetic acid, which is further converted to acetone with high selectivity on the supported metal oxide;

3. In the present invention, the catalyst for highly selective conversion of synthesis gas to acetone has better reaction performance, and under better reaction conditions, the selectivity of acetone is higher than 90%;

4. The catalyst of the present invention for producing acetone through highly selective conversion of synthesis gas has good stability, low price, high added value of the product, good economic benefits, and potential application prospects.

Detailed ways

In order to make the technical problems to be solved by the present invention, technical solutions and beneficial effects clearer and clearer, below in conjunction with embodiment, the catalyst and the application thereof of synthesis gas relay catalysis highly selective acetone system provided by the present invention are further described below, but this The invention is not limited thereby.

Example 1

Weigh 0.5g Cu-ZnO-Al ₂ O ₃ (Cu/Zn/Al molar ratio is 6:3:1) catalyst, 1.0g H-ZSM-35 (Si/Al=12) and 1.0g 10wt.%ZrO ₂ /Al ₂ O ₃ , loaded into a quartz tube, with 10wt.% ZrO ₂ /Al ₂ O ₃ in the lower layer, H-ZSM-35 in the second layer, and Cu-ZnO-Al ₂ O ₃ in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 230°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 2

Weigh 0.6g Pd-ZnO-Al ₂ O ₃ (Pd/Zn/Al molar ratio is 1.5:5.5:3) catalyst, 1.0g H-MOR (Si/Al=13) and 1.0g 20wt.%MnO ₂ / H-MOR, loaded into a quartz tube, with 20wt.% MnO ₂ /H-MOR in the lower layer, H-MOR in the second layer, and Pd-ZnO-Al ₂ O ₃ in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 3

Weigh 0.6g ZnO-ZrO ₂ (Zn/Zr molar ratio is 1:4) catalyst, 1.0g H-ZSM-35 (Si/Al=12) and 1.0 g 10wt.% La ₂ O ₃ /CaCO ₃ , pack into a quartz tube with 10wt.% La ₂ O ₃ /CaCO ₃ in the lower layer, H-ZSM-35 in the second layer, and ZnO-ZrO ₂ in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 4

Weigh 0.6g Cu-ZnO (Cu/Zn molar ratio is 3:2) catalyst, 1.0g H-ZSM-35 (Si/Al=12) and 1.0g 15wt.% La ₂ O ₃ /TiO ₂ , load In the quartz tube, 15wt.% La ₂ O ₃ /TiO ₂ is in the lower layer, H-ZSM-35 is in the second layer, and Cu-ZnO is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 5

Weigh 0.6g of ZnO-Al ₂ O ₃ (Zn/Al molar ratio is 1:2) catalyst, 1.0g of pyridine-modified H-MOR (Si/Al=13) is expressed as Py-H-MOR and 1.0g 10wt.% ZrO ₂ /MgO, loaded into a quartz tube, where 10wt.% ZrO ₂ /MgO is in the lower layer, Py-H-MOR is in the second layer, and ZnO-Al ₂ O ₃ is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 6

Weigh 0.6g of ZnO-Fe ₂ O ₃ (Zn/Fe molar ratio is 1:2) catalyst, 1.0g of pyridine-modified H-MOR (Si/Al=13) is expressed as Py-H-MOR and 1.0g 15wt.% CeO ₂ /H-ZSM-5, loaded into a quartz tube, where 15wt.% CeO ₂ /H-ZSM-5 is in the lower layer, Py-H-MOR is in the second layer, ZnO-Fe ₂ O ₃ is in the top floor. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 7

Weigh 0.6g of In ₂ O ₃ -ZrO ₂ (In/Zr molar ratio is 2:1) catalyst, 1.0g of selectively dealuminated H-MOR (Si/Al = 13) is expressed as H-MOR-DA- 12MR and 1.0g 10wt.% ZrO ₂ /H-MOR, packed into a quartz tube, where 10wt.% ZrO ₂ /H-MOR is in the lower layer, H-MOR-DA-12MR is in the second layer, In ₂ O ₃ - _ZrO2 is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 8

Weigh 0.6g of ZnO-Ga ₂ O ₃ (Zn/Ga molar ratio is 1:2) catalyst, 1.0g of H-MOR (Si/Al=13) decorated with metal Mn and selective dealumination, expressed as 1wt.%Mn /H-MOR-DA-12MR and 1.0g 20wt.% CeO ₂ /SiO ₂ , packed into a quartz tube, with 20wt.% CeO ₂ /SiO ₂ in the lower layer, 1wt.% Mn/H-MOR-DA-12MR In the second layer, ZnO- _Ga2O3 is _on top. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 280°C, the reaction pressure is 4MPa, the space velocity of the synthesis gas is 3000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 9

Weigh 0.6g of ZnO-ZrO ₂ (Zn/Zr molar ratio is 1:4) catalyst, 1.0g of selectively dealuminated H-MOR (Si/Al = 13) is expressed as H-MOR-DA-12MR and 1.0 g 15wt.% CeO ₂ /TiO ₂ , packed into a quartz tube, wherein 15wt.% CeO ₂ /TiO ₂ is in the lower layer, H-MOR-DA-12MR is in the second layer, and ZnO-ZrO ₂ is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 310°C, the reaction pressure is 5MPa, the space velocity of the synthesis gas is 2000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Example 10

Weigh 0.6g ZnO-Cr ₂ O ₃ (Zn/Cr molar ratio is 3:2) catalyst, 1.0g metal Mn-modified selective dealuminated H-MOR (Si/Al=13) expressed as 1wt.%Mn /H-MOR-DA-12MR and 1.0g 20wt.% CeO ₂ /Al ₂ O ₃ , packed into a quartz tube with 20wt.% CeO ₂ /Al ₂ O ₃ in the lower layer, 1wt.% Mn/H-MOR -DA-12MR on the second layer, ZnO- _{Cr2O3 on} the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 310°C, the reaction pressure is 6MPa, the space velocity of the synthesis gas is 1200h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 3. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Table 1 embodiment and comparative example catalyst performance evaluation result

Note: C _2-4 is C ₂ -C ₄ hydrocarbon, C ₅₊ is aliphatic hydrocarbon with carbon number ≥ 5, DME is dimethyl ether, EtOH is ethanol, MA is methyl acetate, EA is ethyl acetate, AA is acetic acid.

Comparative example 1

Weigh 0.6g of ZnO-ZrO ₂ (Zn/Al molar ratio is 1:4) catalyst, 0.2g of selectively dealuminated H-MOR (Si/Al = 13) is expressed as H-MOR-DA-12MR and 1.0 g 15wt.% CeO ₂ /TiO ₂ , packed into a quartz tube, wherein 15wt.% CeO ₂ /TiO ₂ is in the lower layer, H-MOR-DA-12MR is in the second layer, and ZnO-ZrO ₂ is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 310°C, the reaction pressure is 5MPa, the space velocity of the synthesis gas is 2000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

Comparative example 2

Weigh 0.6g of ZnO-ZrO ₂ (Zn/Zr molar ratio is 1:4) catalyst, 1.0g of selectively dealuminated H-MOR (Si/Al = 13) is expressed as H-MOR-DA-12MR and 0.2 g 15wt.% CeO ₂ /TiO ₂ , packed into a quartz tube, wherein 15wt.% CeO ₂ /TiO ₂ is in the lower layer, H-MOR-DA-12MR is in the second layer, and ZnO-ZrO ₂ is in the top layer. Introduce 10% H ₂ -Ar mixed gas, heat up to 260°C at a rate of 5°C/min for 1 hour, then switch to N ₂ purge for 1 hour, cool down to 200°C, and then carry out catalytic reaction. The reaction conditions are as follows: The reaction temperature is 310°C, the reaction pressure is 5MPa, the space velocity of the synthesis gas is 2000h ^-1 , and the volume ratio of H ₂ to CO in the synthesis gas is 2. The raw materials and products of the reaction were analyzed by gas chromatography through pipeline insulation. The specific catalytic performance is shown in Table 1.

The present invention uses relay catalysis to couple syngas to methanol, methanol heterogeneous carbonylation to acetic acid, and acetic acid ketonylation to acetone, wherein the metal oxides used to synthesize methanol are mainly activated to hydrogenate CO to generate methanol intermediates, and multi-stage pore zeolite molecular sieves It is responsible for catalyzing the intermediate product methanol to further generate acetic acid, and the acetic acid is further highly selectively converted into acetone on the supported metal oxide, and the selectivity of acetone is higher than 90%; the catalyst for the high-selective conversion of synthesis gas to acetone in the present invention has good stability, The price is low, the product has high added value, has good economic benefits, and has potential application prospects.

Claims (8)

1. A method for syngas one-step system of acetone, characterized in that: the composite catalyst is placed in the reactor, pre-treated, then feeds the synthesis gas, carries out the catalytic reaction, and obtains acetone; the composite catalyst adopts multiple Composite in bed mode, relay catalytic reaction, in which, the metal oxide catalyst for syngas to methanol is placed in the first bed, the zeolite molecular sieve for methanol carbonylation to acetic acid is placed in the second bed, and the ketone for acetic acid to produce acetone The supported metal oxide is placed in the third bed. 2. the method for a kind of synthesis gas one-step method for producing acetone as claimed in claim 1, is characterized in that: in described composite catalyst, the metal oxide of synthesis gas production methanol, the zeolite molecular sieve and acetate ketone of methanol carbonylation production acetic acid The mass ratio of the supported metal oxides for the production of acetone is 1:(0.5-4):(0.5-4). 3. A method for producing acetone from syngas in one step as claimed in claim 1, characterized in that: the metal oxides for the synthesis gas to methanol are selected from Cu-ZnO-Al ₂ O ₃ , Pd-ZnO-Al ₂ O ₃ , ZnO-Cr ₂ O ₃ -Al ₂ O ₃ , ZnO-Cr ₂ O ₃ , ZnO-ZrO ₂ , CeO ₂ -ZrO ₂ , ZnO-Al ₂ O ₃ , ZnO-Ga ₂ O ₃ , ZnO-Fe At least one of ₂ O ₃ , In ₂ O ₃ -ZnO, and In ₂ O ₃ -Al ₂ O ₃ . 4. The method for producing acetone by one-step method of synthesis gas as claimed in claim 1, characterized in that: the zeolite molecules for the production of acetic acid by the carbonylation of methanol are selected from MOR, FER, IWW, MEL types with eight-membered ring topology At least one of zeolite molecular sieves. 5. A method for producing acetone from syngas in one step as claimed in claim 4, characterized in that: the zeolite molecular sieve has a microporous structure, wherein the pore diameter of the micropores is 0.2 to 0.8 nm, and the pore volume of the micropores is 0.05 nm. ~0.5 cm ³ /g. 6. the method for a kind of synthesis gas one-step method for producing acetone as claimed in claim 1, is characterized in that: the loaded metal oxide of described acetic acid ketoylation system acetone is marked as xwt.%MO _x /Y, wherein x The range is 5% to 50%, M is at least one of Ce, Mn, Zr, La, Pr, Nd, Y is H-MOR, H-ZSM-5, Al ₂ O ₃ , SiO ₂ , TiO ₂ , At least one of MgO, CaCO ₃ . 7. the method for a kind of synthetic gas one-step process acetone as claimed in claim 1, is characterized in that, the method for described pretreatment is: after installing catalyst on fixed bed, fluidized bed or moving bed reactor, pass into For hydrogen or a mixture of hydrogen and inert gas, the temperature is raised to 200-500°C at a rate of 1-10°C/min, and kept for 0.5-10h, and then switched to inert gas for 0.1-5h. 8. A method for preparing acetone from syngas in one step as claimed in claim 1, characterized in that the catalytic reaction method is as follows: after the composite catalyst is pretreated, the temperature is reduced to 30-200° C. gas, wherein the volume ratio of H ₂ to CO is 1:(0.2~3), and then the temperature is raised to a reaction temperature of 200~400°C, a reaction pressure of 0.5~7MPa, and a synthesis gas space velocity of 500~15000h ^-1 . The product acetone is obtained through catalyst bed reaction.